METHOD OF CYCLIC USE OF STRAW IN THE PULPATION AND PAPER MANUFACTURING PROCESS

专利摘要:
method of cyclical use of straw in the pulping and papermaking process. the present invention relates to a method of cyclical use of straw in a pulping and papermaking process that comprises the following steps of: obtaining the straw raw material for pulping and its residues through load preparation; obtain the primary pulp by digesting the straw raw material according to the ammonium sulfite method; obtain the pulp and concentrated black liquid by extruding the primary pulp; obtaining the paper pulp for the preparation of a paper product and the black liquid substance diluted by washing and post-processing; mixing the concentrated black liquid substance and the diluted black liquid substance, and then evaporation and concentration; obtaining the contaminated condensate by recovering the evaporated liquid, and using a residual concentrate as a raw material for fertilizer or the concentrated black liquid substance for the preparation of a fertilizer; mix the contaminated condensate with one or more of the group of the residual material obtained from the filler preparation, a culture by-product or organic waste, and obtain the base material or fertilizer by fermenting the contaminated condensate or sulfite nitrogen source. ammonium, or use of contaminated condensate for flue gas desulfurization, in which ammonia and flue gas are reacted to obtain ammonium sulphite as a digesting agent; and use the recycled water from the intermediate phase water processing in the corresponding phases in the integral pulping process.
公开号:BR112012023453B1
申请号:R112012023453-6
申请日:2011-03-11
公开日:2020-07-14
发明作者:Hongfa Li；Mingxin Song；Songtao CHEN；Jihui Yang；Liangjin Guo
申请人:Shandong Tralin Paper Co., Ltd；
IPC主号:

专利说明:

Field of the Invention
[001] The present invention relates to a method of cyclic use in pulping and papermaking processes with straw. Background of the Invention
[002] For the manufacture of paper with straw as specified in the prior art, the raw materials used are mainly the straws from plants of the annual grass family and mallow family. The applied papermaking process generally consists of cutting straw, sorting, undressing, digesting, washing, sorting and cleaning, bleaching, washing, tapping and making paper.
[003] In the prior art, the ammonium sulfite method is used for the preparation of non-wood fiber raw material pulp. It is characterized by smooth digestion, in order to avoid the damage of strong alkali on the fibers, increase the resistance of the pulp, increase the yield, reduce the damage of the broken end of the papers, and achieve a high rate of finished products.
[004] After the straw raw material in question is digested in ammonium sulfite, cellulose is extracted as the raw material for papermaking. The remaining black liquid substance can be used as a fertilizer. However, since the water content in the digested black liquid substance of ammonium sulfite is high, storage and transport are not convenient.
[005] CN200510086269 discloses a method for the preparation of commercial organic fertilizer without residual liquid substance from pulping and papermaking by the ammonium sulfite method; Comprehensive Treatment Technology for Papermaking Wastewater by Ammonium Sulfite Method (Environment And Sustainable Development, Page 36 to Page 37, Volume 1, 2006) reports a type of waste treatment method that separated waste water from paper making into digested black liquid substance , medium-sized water and white water, all of which will be separately treated and used, in order to achieve comprehensive standards. However, during the evaporation of the black liquid substance of the method in question, the energy consumption is high, as well as the cost. In addition, ammonium sulfite decomposes during evaporation, so that there is a certain amount of ammonia in the condensate, which belongs to the ammoniacal nitrogen pollutant. Therefore, the condensate cannot be directly discharged. It is also necessary to treat the condensate, which further increases the cost. In addition, the pulp of non-wood fiber raw material prepared using the ammonium sulfite method is difficult to bleach. During bleaching, the bleach dosage is increased, which further increases the cost and increases the source of pollution.
[006] In addition to the disadvantages mentioned above, the manufacture of paper with non-wood fiber also has the following disadvantages: The paper pulp fiber is small, low in strength and weak in filtration performance, and the quality of the paper produced from paper pulp fiber has a relatively low quality; Water consumption is as high as 100 m3 to 150 m3 per ton of pulp; There are many small fibers in the black liquid substance, the polysaccharide content is high, the interference is taken by Silicon, and the lignin structure is complex, all of which result in the low concentration of black liquid substance and difficulties in the treatment of the black liquid substance ; The discharge of COD and BOD severely exceeds the standards. The discharge of COD wheat straw pulp in China accounts for more than 74% of the total discharge in the entire paper industry; In the residual chlorine bleaching liquid, there are not only common pollutant factors for the water environment such as COD and BOD, but also highly toxic products such as trichloromethane, dichlorophenol, trichlorophenol, and dioxin, chlorofuran, etc.
[007] In conclusion, during the manufacture of paper with straw raw material, the improvement of the individual stage alone will never achieve the comprehensive purpose of water conservation, energy conservation, reduction of consumption, increase of efficiency and high quality. Only advances in pulping, papermaking, energy conservation and consumption reduction technologies can achieve efficient and cyclical use of resources, and achieve the paper industry's sustainable development goal.
[008] Therefore, the present invention is deposited. Summary of the Invention
[009] The main objective of the present invention is to provide a method of cyclic use in pulping and papermaking processes with straw, which can, by controlling the processes, carry out the comprehensive and multiple cycle use of each raw material, intermediate product, waste material, residual liquid, energy, water and products.
[0010] In the present invention, straw refers to grass plant straw, comprising one, or a combination, of rice straw, wheat straw, cotton stalk, bagasse, corn stalk, reed and bamboo straw, in the However, rice straw, wheat straw and corn stalk are preferred.
[0011] In the present invention, the paper pulp prepared by the pulping processes mentioned in the present invention (i.e. digestion, pulp extrusion, pulp washing, and oxygen defibration and delignification) is called unbleached pulp, which can be used as the pulp for unbleached paper, wrinkled paper, snack box, gelatin printing paper, and food wrapper.
[0012] For the unbleached pulp mentioned in the present invention, during preparation, since no bleaching processing other than oxygen delignification in the prior art (there is a bleaching process called oxygen delignification in the prior art, so it is explained here for distinguish) is carried out, there is no contamination of bleaches in the pulp obtained, nor dioxin and adsorbable organic halides. Meanwhile, the pulp strength is protected, and the loss and degradation of cellulose in the pulp, due to the bleaching influence, is avoided.
[0013] The paper pulp mentioned in the present invention refers to the unbleached pulp, which has a fracture length of 5.0 to 7.5 km, a folding number of 40 to 90 times, a tear resistance of 230 to 280 mN, and a whiteness of 35 to 55% ISO; the low whiteness pulp has a whiteness of 43 to 65% ISO, a fracture length of 4.5 to 7.2 km, a tear strength of 200 to 300 mN, a fold number of 30 to 121 times, and a beat rate of 28 to 35 ° SR.
[0014] The unbleached pulp has a relatively high resistance. In particular, the fracture length and fold number of unbleached pulp has exceeded that of hardwood pulp. It can be used directly for the production of newspaper, book paper, and tissue paper, etc. Or, it can be more widely used for the production of other types of paper by adding only a small amount of wood pulp. Therefore, the cost for the product is significantly reduced, while the strength of the product is ensured. The low whitish pulp in the present invention can be used for the manufacture of newspaper, supercalendered paper, wrapping paper, paper diaper, toilet paper, tissue paper, facial tissues, napkins, paper towels, kitchen paper, paper writing paper, printing book paper, gelatin printing paper, single-sided writing paper, single-sided gelatin printing paper and wrinkled paper. It can also be used for the production of molded products with pulp, which include: bowl, bowl, glass, barrel, plate, tray and snack box; support, electric welding shield, interior decoration plate, molded vase, molded cup for the development of seedlings, molded slippers, absorbent pillow, and bathroom seat cushion; molded medical tray holder, molded medical protection product, and disposable medical container.
[0015] The purpose of the present invention can be achieved by the following methods:
[0016] The method of cyclical use in the pulping and papermaking processes mentioned in the present invention comprises the following steps: Among the raw materials for agricultural planting, greenhouse and garden F, selection of straw raw material G which is suitable for pulping, obtaining raw material for pulping A through preparation H, obtaining high-strength pulp B by digesting T, then obtaining pulp O by extrusion U and washing V, execution of post- treatment X for pulp O to obtain paper pulp Z, and manufacture of paper product W with pulp O; In step (1), obtaining residue I after preparation of the load, mixing residue I with contaminated condensate Q, obtaining substrate K by fermentation J, then returning the substrate formed K for agricultural planting, greenhouse planting and garden F for use, which may result in the cyclical availability of the raw material for straw G; Extraction of the black liquid substance C from the washed high-strength pulp B by extrusion U and washing V, and obtaining of the concentrated black liquid substance D by evaporation and concentration P, which can be used as fertilizer E to cyclically return to agricultural planting, greenhouse planting and garden F for use; With the help of flue gas desulfurization R, generation of ammonium sulphite S by the mixture of contaminated condensate Q obtained from the process P of evaporation and concentration of the black liquid substance C obtained after washing, and use of ammonium sulphite S in digestion T cyclically; Use of recycled water from medium phase water processing in the corresponding phases in the integral pulping process.
[0017] Based on the aforementioned circulation, M (crop by-product) from agricultural planting, greenhouse planting and garden F and / or organic residue L from other aspects are placed in step (2) of the circulation, the contaminated condensate Q is mixed, the substrate or fertilizer K is obtained by fermentation method J, and the substrate or fertilizer K is returned to agricultural planting, greenhouse planting and garden F to form the circulation.
[0018] The contaminated condensate or ammonium sulphite obtained by the absorption of flue gas is mixed with culture by-product or organic residue, the ratio of the mass percentage of carbon to the mass percentage of nitrogen in the mixture is adjusted to be 15 ~ 30: 1 to obtain the mixture before fermentation. The pH value of the mixture before fermentation is 9.5 ~ 10. Spontaneous fermentation for the mixture obtained before fermentation is carried out to obtain the fermented mixture. When the ratio of the mass percentage of carbon to the mass percentage of nitrogen in the fermented mixture obtained is within the range of 15 ~ 30: 1, and the pH is within the range of 6.5 ~ 8.5, the fermentation is completed and the substrate is obtained.
[0019] In fact, while the present invention makes full use of residues other than the pulp consumed by circulation technology, it is also required to add a large quantity of raw materials needed by the process, in order to prepare the lack of various raw materials during circulation. For example, most straw raw materials are raw materials out of circulation, and most of the ammonium sulphite comes from sources other than circulation.
[0020] During the processing of medium phase water, coagulation aids are added to the residual water after the UPCB adsorption filtration layer. The additive amount of coagulation aids is taken as 0.2 to 5 ppm of the total weight of the wastewater. Filtration is micro-filtration, with the number of meshes being 80 to 120.
[0021] Medium-stage water processing also includes the stages of filtration, sand circulation, flocculation sedimentation, separation and recycling. The flocculants are added to the recycling water to be processed before flocculation is established. Desalination is carried out for 70 to 90% of the total amount of flocculants (by weight). In the flocculation sedimentation step, firstly, 10 to 30% of the total amount of flocculants (by weight) are added to the recycling water to initiate the flocculation sedimentation in the water recycle. The GT dosing point is controlled in the range 106 to 108, and the time for the hybrid reaction is 2 to 8 minutes. Then the flake that is desalted and retextured is added to continue the flocculation sedimentation. The GT is controlled in the range of 105 to 106, and the time for the hybrid reaction is 5 to 15 minutes. After flocculation sedimentation, it is allowed to add coagulation aids to the recycling water, and the amount of the coagulation aids is 1 to 6 ppm of the weight of the recycling water to be processed.
[0022] To be more specific, the method of the present invention comprises the following steps: Raw material and residues obtained from cargo preparation
[0023] In the present invention, the raw material obtained by the method of preparation of dry cargo can be directly digested, or impregnated in the organ of Corti for impregnation after preparation of the cargo and before digestion.
[0024] During pre-impregnation, the liquid substance ratio is 1: 2 to 4, and the temperature of the liquid impregnation substance is 85 to 95 ° C. As a result, the liquid impregnating substance can entirely come into contact with the raw materials, which will result in the uniform impregnation of the raw materials.
[0025] The liquid impregnating substance can be an aqueous alkali with a certain concentration, such as an aqueous alkali with an amount of alkali being 2 to 4% of that of absolutely dry raw materials (in sodium hydroxide), or a mixed alkali liquid substance and black liquid substance, with the concentration of black liquid substance being 11 to 14 ° Be '(20 ° C).
[0026] The raw material is impregnated in the black liquid substance as the residual liquid substance, which performs the recycling of the black liquid substance, reduces the pressure of the environmental processing of the black liquid substance, and therefore provides the complete chemical reaction conditions for the raw material in digestion. Digestion of Raw Material
[0027] The batch type spherical digester, continuous digester, or vertical digester can be adopted for the digestion mentioned in the present invention. The details are as follows:
[0028] 1) When digestion is carried out by the ammonium sulphite method in a batch-type spherical digester or continuous digester:
[0029] 1 The liquid chemical for digestion is added to the straw raw material, with the amount of ammonium sulphite being 9 to 13% of that of absolutely dry raw materials, and the liquid substance ratio being 1 : 2 to 4;
[0030] 2 Steam is supplied for heating at a temperature of 165 to 172 ° C. The blocking time for temperature rise, relief and thermal insulation is 160 to 210 minutes for the spherical digester, and 30 to 40 minutes for the continuous digester.
[0031] 2) When digestion is carried out using the ammonium sulphite method in the vertical digester:
[0032] 1 The liquid chemical for digestion is added to the straw raw material for pulping that is obtained by preparing the filler, with the amount of ammonium sulfite being 9 to 15% of that of the absolutely dry raw materials , and the liquid substance ratio being 1: 6 to 10;
[0033] 2 The straw raw material for pulping is released into the digester through the black liquid substance. When the digester is fully supplied, the cover is closed. The chemical for digestion with a temperature of 130 to 145 ° C is added inside the digester. Meanwhile, the air in the digester is expelled and the pressure is increased to 0.6 to 0.75 MPa, and the temperature of the liquid chemical for digestion is increased to 156 to 173 ° C. The temperature rise, thermal insulation, and replacement are performed, and finally a pump is used to discharge the pulp into the expansion tank, with the blocking time being 220 to 360 minutes.
[0034] For the digestion process that adopts the ammonium sulfite method in the present invention, after digestion of grassy plants, a pulp of high solidity with a K value of 16 to 28 (equivalent to a cover number of 24 to 50) is obtained.
[0035] Compared to the prior art digestion method, the digestion method of the present invention, to a large extent, protects the constituents of the grassy plant raw material necessary for pulping, while significantly shortening the thermal insulation time , significantly reduces energy consumption, and improves pulping yield significantly, with 50 to 68% for primary pulp. As a result, production efficiency is significantly improved.
[0036] The digestion by the ammonium sulfite method of the present invention includes the alkaline ammonium sulfite method, the neutral ammonium sulfite method and the acid ammonium sulfite method.
[0037] The preferred digestion must be carried out using the alkaline ammonium sulphite method. Thus, the concentration can be directly carried out.
[0038] However, if digestion is performed by the neutral ammonium sulfite method and the acid ammonium sulfite method, an appropriate amount of alkali will be added to convert the ammonium sulfite to sulfite before the concentration is carried out on the substance. black liquid. Alkali refers to one, or a combination, of sodium hydroxide, calcium hydroxide, potassium hydroxide, or sodium bicarbonate, etc. Extrusion
[0039] The extrusion of the method in the present invention refers to the supply of the high solid pulp with a concentration of 8 to 15% at the entrance of the pulp extruder, then the extrusion of the black liquid substance by means of the extrusion force to obtain an extruded pulp with a concentration of 18 to 30%.
[0040] The extrusion can be performed by the pulp extruders that are used to extract the black liquid substance in the prior art. The preferred extruder is the single reduction pulp extruder, double screw pulp extruder, or double cylinder pulp extruder. During extrusion by the pulp extruder, since the very large extrusion force will be generated in order to facilitate defibration, fraying, brushing, and conquassation, the primary walls are damaged, the fibers absorb enough energy to generate very great tension within the fibers, and the reaction performance of the high-strength pulp will be significantly improved. Meanwhile, the fibers undergo fibrillation; the organic matter on the epidermis and the impurities between the fibers dissolve in the digested black liquid substance, and deposition discharged from the outlet chute. Therefore, the fiber concentration is significantly improved. Some ashes and impurities in the black liquid substance will also be discharged with the black liquid substance, which facilitate complete preparation for the next stage of the process. Furthermore, the change in the degree of beating of the high-strength pulp is very small before and after extrusion, that is, the damage to cellulose is small, which can keep the inherent lengths of grass fibers relatively well and minimize the fiber damage. Pulp Washing and Black Liquid Substance Recycling
[0041] The wash of the present invention refers to one or more washes of displacement of the extruded pulp by one of, or combination, black liquid substance with a temperature of 60 to 80 ° C, a concentration of 3 to 6.2 ° Be, and a pH value of 8 to 8.3, or fresh water with a temperature of 70 to 80 ° C.
[0042] The washing is performed in a vacuum pulp washing machine, pressure pulp washing machine or horizontal belt pulp washing machine.
[0043] The difference from the prior art is that the washing in the present invention is for a pulp of high solidity with a K value of 16 to 28 (equivalent to a layer number of 24 to 50). Since the solidity of this pulp species is very high, it is easier to wash away the ashes and impurities, in order to keep the pulp in a very high degree of purity.
[0044] The black liquid substance can be reused for digestion in Step 2. Oxygen delignification
[0045] The post-treatment mentioned in the present invention includes defibration, oxygen delignification, purification and screening. The obtained paper pulp, which is used for the production of paper products, is called unbleached pulp. The preferred bleaching does not include the traditional pulping of the non-wood fiber.
[0046] The defibration includes the treatment of the pulp washed by a desiccator, kneading machine, disc crusher, disc grinder in the tapping machine, or defibrator, in order to loosen the fiber structures.
[0047] Oxygen delignification refers to the removal of lignin in the pulp using sodium hydroxide and oxygen, which includes:
[0048] 1) Adjust the concentration of the pulp of high solidity, which is obtained after digestion, in 8 to 18%, that is, the delignification of oxygen is carried out under medium concentration conditions;
[0049] 2) Pump the pulp into the reaction tower for oxygen delignification, and add sodium hydroxide and oxygen; and
[0050] 3) Start the delignification reaction in the reaction tower for oxygen delignification, and then obtain a pulp with a K value of 10 to 14 (equivalent to a cover number of 13 to 19.8).
[0051] Preferably, the pulp strength obtained after oxygen delignification in Step 3) is the only one with a Kappa number from 14.5 to 17.7.
[0052] In the present invention, the control of the solidity of the pulp obtained after delignification with oxygen is to guarantee the removal of the maximum amount of lignin, on the one hand, and to guarantee the solidity of the pulp obtained on the other hand. Similarly, the method for oxygen delignification can be any method of the prior art, as long as the solidity of the pulp after controlled treatment is within the range specified in the present invention.
[0053] Oxygen delignification can be single tower / double tower oxygen delignification. For multi-stage oxygen delignification, the degradation influence of single tower / double tower oxygen delignification being used in the present invention is relatively small.
[0054] During oxygen delignification, the pulp has a temperature of 95 to 100 ° C and a pressure of 0.9 to 1.2 MPa at the entrance of the reaction tower, and a temperature of 100 to 105 ° C and a pressure of 0 , 2 to 0.6 MPa at the outlet. During oxygen delignification, the amount of alkali is 2 to 4% of the pulp absolutely dry (in sodium hydroxide), and the amount of oxygen is 20 to 40 kg per ton of pulp. The reaction time of the pulp inside the reaction tower is 60 to 150 minutes.
[0055] During oxygen delignification in the present invention, the delignification rate is 35 to 70%.
[0056] During the oxygen delignification mentioned in the present invention, the magnesium salt is used as a protective agent, the amount of which is 0.2 to 1.2% of the pulp absolutely dry. Meanwhile, H2O2 can be added as the reinforcer. Concentration of Black Liquid Substance
[0057] The contaminated condensate in the present invention includes the slightly contaminated condensate and / or the severely contaminated condensate.
[0058] The NH4 + -N concentration of the slightly contaminated condensate is greater than 0 and less than 1000 mg / l.
[0059] The NH4 + -N concentration of the severely contaminated condensate is 4000 mg / l ~ 5000 mg / l, preferably 4000 mg / l ~ 4500 mg / l. Severely contaminated condensate is preferred. The temperature of the contaminated condensate is 25 ~ 70 ° C, preferably 50 ~ 70 ° C.
[0060] In the practical process of a specific industrial production, the concentration of NH4 + -N in the severely contaminated condensate varies widely. The purpose of the present invention is to comprehensively adjust the entire treatment process. How to perform the circulation on the basis of reaching the basic papermaking requirements is the aspect of the present invention. Therefore, even if the NH4 + -N concentration of the severely contaminated condensate is not within the scope disclosed in the present invention, as long as the technical scheme mentioned in the present invention is used, it will be considered within the scope of protection of the invention. Fertilizer Preparation
[0061] In the present invention, the concentrated black liquid substance, which is obtained by the evaporation and concentration of the pulping black liquid substance, can be directly used for the preparation of organic fertilizer. The researchers of the present invention have also observed that pulping by the method of the present invention can reduce the damage to cellulose, and the fulvic acid content in the residual liquid after digestion is relatively high. The fulvic acid content in the solid content of the black liquid substance is 10 to 20%.
[0062] Although the fulvic acid content in the solids content of the black liquid substance obtained by the ammonium sulfite method in the prior art is 6 to 12%, the fulvic acid content in the solids content of the black liquid substance obtained by pulping alkaline is 1 to 6%.
[0063] The fertilizer in the present invention includes solid fertilizer or liquid fertilizer that is formed by removing part of the water in the black liquid substance by evaporation and concentration, and adding some auxiliary materials in the obtained concentrated black liquid substance.
[0064] The solids content of the concentrated black liquid substance is 28 to 65%, and the baume grade is 9 to 40. The solids content 30 to 65% and the baume grade 18 to 40 are preferable , although more preferably, a solid content of 40 to 47% and a baume degree of 25 to 29. The pH of the concentrated black liquid substance is preferred to be 5 to 11, and a pH of 6 to 8 is most preferred.
[0065] The percentage by weight of each composition in the fertilizer in the present invention is as follows: from 30 to 80% for the concentrated black liquid substance (preferably from 50 to 60%) from 1 to 45% for lignin (from preferably 15 to 35%) from 1 to 25% for humic acid (preferably 10 to 15%)
[0066] Drying is spray drying or spray granulation of the pulp, preferably spray granulation of the pulp. During spray granulation of the pulp, the nose temperature is 550 - 600 ° C, the final temperature is 47 to 55 ° C, and a return charge rate> 50%.
[0067] The mud and / or ardealite can also be added in the concentrated black liquid substance. The weight percentage of the mud is 0 to 45%, and that of ardealite is 0 to 30%. Preferably, the weight percentage of the mud is 10 to 20%, and that of ardealite is 5 to 15%;
[0068] The sludge is the biochemical sludge obtained in the treatment of wastewater from papermaking, and its organic matter content is not less than 50%.
[0069] Inorganic auxiliary materials can also be added in the concentrated black liquid substance. Inorganic auxiliary materials refer to one, or a mixture of more than two types, of the inorganic salts containing N, P or K, preferably KC1. The addition of inorganic auxiliary materials causes the total content of N, P2O5 and K2O to become 4 to -30% of the dry weight percentage of the dry formula, preferably 5%.
[0070] In the present invention, auxiliary materials can also be soluble fertilizers of main elements. By adding soluble fertilizers of main elements in the diluted black liquid substance or in the concentrated black liquid substance, we can obtain the fertilizers from the discharge of water from fulvic acids. Main element soluble fertilizers can be one or more of soluble nitrogen fertilizer, soluble phosphate fertilizer, and soluble potassium fertilizer, among which soluble nitrogen fertilizer and soluble potassium fertilizer are preferred.
[0071] The percentage by weight of each composition is as follows: from 20 to 98% of the diluted black liquid substance or of the concentrated black liquid substance (50 to 90% preferable); from 2 to 80% of soluble fertilizers of main elements (10 to 50% preferable);
[0072] Soluble nitrogen fertilizer refers to a random or mixture of urea, ammonium bicarbonate, ammonium sulfate, ammonium chloride, ammonium dihydrogen phosphate, or diamonium hydrogen phosphate, among which urea is preferable . The percentage by weight of the nitrogen fertilizer soluble in the fertilizer of the discharge water of fulvic acids is from 2 to 60%, and preferably from 2 to 30%;
[0073] Soluble phosphate fertilizer refers to a random or mixture of ammonium dihydrogen phosphate, diamonium hydrogen phosphate, potassium dihydrogen phosphate, or di-potassium hydrogen phosphate, among which di- hydrogen ammonium phosphate is preferred. The weight percentage of the soluble phosphate fertilizer in the fulvic acid discharge water fertilizer is 2 to 60%, and preferably 2 to 30%;
[0074] Soluble potassium fertilizer refers to one or random mixture of potassium sulfate, potassium chloride, potassium dihydrogen phosphate, or potassium hydrogen phosphate, among which potassium chloride is preferred. The weight percentage of the potassium fertilizer soluble in the fulvic acid discharge water fertilizer is 2 to 50%, and preferably 2 to 30%.
[0075] Soluble fertilizers containing microelements (such as iron, copper, boron, zinc or magnesium, etc.) can also be added in the concentrated black liquid substance. Substrate Formation by Mixed Fermentation of Severely Contaminated Condensate and Residue
[0076] In the present invention, the contaminated condensate is mixed with one or more of the residues, by-product of the culture, or organic residues generated in the preparation of pulping load. The mixture is fermented by the nitrogen source in the contaminated condensate to obtain the substrate. Since there is a large amount of nutrition constituents in the residues, crop by-product, or organic residues, for example, there is a large amount of organic ingredients such as nitrogen, phosphorus, potassium in the stem, leaf, and straw root, the content of nitrogen in 100 kilograms of fresh straw is equivalent to 2.4 kilograms of nitrogen fertilizers, the phosphorus content is equivalent to 3.8 kilograms of phosphate fertilizer, and the potassium content is equivalent to 3.4 kilograms of fertilizer. potash. If 500 kg of straw is returned to the field, it is equivalent to using 50 kg of standard fertilizer in the field. It can also reduce the weight of the soil volume, make the soil more permeable to water and air, improve the water holding capacity and conserve soil moisture, as well as intensify granular structures.
[0077] During the aerobic fermentation of compost, the culture straws need a water content of more than 60%, and a temperature around 55 to 65 ° C. Meanwhile, C: N will be controlled within the range of 15 to 30: 1, in order to achieve the best fermentation conditions.
[0078] In the present invention, seriously contaminated condensate is preferable. The reason is that the NH4 + -N concentration of the severely contaminated condensate obtained by the method of the present invention is higher than 4000 mg / l, so that the severely contaminated condensate with a high nitrogen content can supplement the nitrogen required during fermentation of crop straws. Meanwhile, since the severely contaminated condensate contains nitrogen, it can increase the pH value in the initial fermentation stage, which can make strains more suitable for surviving in alkaline conditions. As a result, fermentation can be completed without adding lime. In addition, the temperature of the condensate contaminated in the present invention can be as high as 50 to 70 ° C. When it is mixed with the crops, it can quickly increase the fermentation temperature, speed up the reproduction of the strains, and significantly reduce the fermentation time.
[0079] When the temperature of the fermented mixture is between room temperature and 40 ° C, the mass ratio of carbon to nitrogen in the fermented mixture and the pH value are detected. If the ratio of the mass percentage of carbon to the mass percentage of nitrogen is within the range of 15 ~ 30: 1, and the pH value is within the range of 6.5 ~ 8.5, fermentation is completed. Otherwise, fermentation is not completed. In this case, a certain amount of water can be added to the fermentation mixture to promote fermentation, in order to avoid "wasting the seedlings".
[0080] The fermentation mentioned in the present invention includes the following steps: The contaminated condensate or ammonium sulphite obtained by the absorption of flue gas is mixed with culture by-product or organic residues, the ratio of the mass percentage of carbon to the percentage of nitrogen mass in the mixture is adjusted to 15 ~ 30: 1 to obtain the mixture before fermentation, the pH value of the mixture before fermentation is 9.5 ~ 10; Spontaneous fermentation is performed for the mixture before the fermentation obtained in Step 1) to obtain the fermented mixture; When the percentage mass ratio of carbon to the mass percentage of nitrogen in the fermented mixture obtained in Step 2) is within the range of 15 ~ 30: 1, and the pH is within the range of 6.5 ~ 8.5 , fermentation is completed and the substrate is obtained.
[0081] In the present invention, the bran can be added before fermentation, in order to increase the reproduction rate of the strains and to shorten the fermentation period.
[0082] In addition, in the present invention, prior to fermentation, one or more fermentation strains, nitrogen fertilizer, phosphate fertilizer, active biochemical sludge, plant nursery soil, lime, or farm animal excrement are added accordingly with the real conditions.
[0083] The substrate prepared in the present invention was detected by three authorized research institutions, namely, Land Resources and Fertilizer Institute under Beijing Forestry University, Shandong Institute of Plant Nutrition and Fertilizer under Shandong Agricultural University, and Tianjin Institute of Agricultural Resources and Environment Science. Various indicators, such as pH value, EC value, organic matter, humic acid, total nitrogen, total phosphorus, total potassium, available nitrogen, available phosphorus, available potassium, have adapted to the application range of organic substrate. Both the permeability and the nutrient content of the substrate are superior to that of peat and perlite. When the prepared substrate or fertilizer is used for the plant growth test, the various plant growth states are obvious, and no auxiliary material is needed to be added. Especially when the number of root systems in a plant increases by more than 30%, the thickness of the root also increases.
[0084] The substrates or fertilizers prepared in the present invention include (percentages are percentages by mass): Water Organic matter Humic acid Total nitrogen Total potassium Total phosphorus 0.1 to 0.5% (preferably 0.1 to 0, 3%)
[0085] The substrate or fertilizer of the present invention contains from 5% to 20% of humic acid, which can promote the absorption and utilization of nitrogen, phosphorus, potassium by crops, improve the physicochemical properties of the soil, stimulate growth and crop development, enhance crop resistance, and improve the quality of agricultural products, etc.
[0086] The contents of total nitrogen, total phosphorus and total potassium in the substrate or fertilizer of the present invention are, respectively, 2.3 times, 12 times and 57 times those of the peat substrate. Therefore, the nutrient contents of the main elements in the substrate or fertilizer of the present invention are, obviously, higher than those of the peat substrate.
[0087] For the substrate or fertilizer of the present invention, the total porosity is 40 ~ 60, preferably 45 ~ 55; aeration porosity is 30 ~ 50, preferably 35 ~ 40, and water containment porosity is 5 ~ 20, preferably 8 ~ 12. Preparation of Ammonium Sulphite
[0088] In the method of the present invention, the flue gas is stripped, and then released into the desulfurization tower. The contaminated condensate is introduced through the pipeline to absorb SO2 in the flue gas in order to obtain (NH4) 2SO3 for digestion in the ammonium sulfite method. The process includes the following steps: 1) Desulfurization is carried out by the flue gas through the contaminated condensate. The flue gas is the industrial coal flue gas, a Venturi tube is equipped in front of the desulfurization tower for desulfurization, and the Venturi tube is equipped with a sprinkler and connected to the bottom of the desulfurization tower. The stripped flue gas enters the Venturi tube, where it mixes with the mixed liquid substance of contaminated condensate and ammonia water through the sprinkler in the Venturi tube. Then the mixed liquid substance and the flue gas enter the desulfurization tower again for desulfurization; 2) The mixture of ammonium sulfite solution after desulfurization is used for pulping by the ammonium sulfite method in papermaking. The ammonium sulfite solution has a concentration of 10% to 35% and a purity of 80% to 99%.
[0089] The straw raw materials of the present invention can also come from raw materials out of circulation, and ammonium sulfite also comes from sources other than circulation.
[0090] The water treatment method mentioned in the present invention includes: Filtration, flocculation sedimentation, biochemical treatment, and advanced treatment.
[0091] Among them, flocculation sedimentation is performed through the UPCB treatment. The UPCB treatment includes the following steps: first, the discharge water completely mixed with flocculants is introduced into the hybrid reaction layer of the UPCB reactor, then optional, aerobic and cyclic sludge is added to the discharge water at the limit between the reaction layer hybrid and the swollen reaction layer; after the reaction in the swelled reaction layer, the flocculants are added or not added to the discharge water, and the discharge water is released into the filtration layer by adsorption in UPCB.
[0092] The method can also be one that includes the stages of filtration, sand circulation, flocculation sedimentation, separation and recycling. Before the flocculants are added to the recycling water to be processed for flocculation sedimentation, desalination is performed for 70 to 90% of the flocculants (by weight).
[0093] Desalination includes the following steps: promoting flocculation of flocculants in clean water, collecting the floc like flocculants in the flocculation sedimentation step, acidifying the floc, performing the anaerobic treatment to regenerate the floc, and collecting the floc again regenerated like flocculants in the flocculation sedimentation step.
[0094] There are the following advantages in the present invention:
[0095] (1) The present invention adopts grass straw and plant straw from the mallow family as the raw material. Digestion and pulping using the ammonium sulphite method is carried out after the preparation of the filler, so that the main prepared products can be used completely, and the waste and residual liquid generated in each section in the pulping can be reused. Therefore, the additional value of the by-products from each section of the pulping process is improved;
[0096] (2) The present invention uses the residues generated in the preparation of cargo and the contaminated condensate generated in the evaporation and concentration of the black liquid pulping substance to prepare the substrate, makes full use of the nitrogen element, temperature, necessary alkaline conditions for the fermentation of straw that can be supplied by the contaminated condensate, not only making full use of resources, but also reducing energy waste;
[0097] (3) After detecting the substrate prepared in the present invention, various indicators, such as pH value, EC value, organic matter, humic acid, total nitrogen, total phosphorus, total potassium, available nitrogen, phosphorus available, and available potassium, have adapted to the range of application of the organic substrate or fertilizer. Both the permeability and the nutrient content of the substrate are superior to those of peat and perlite. When the prepared substrate or fertilizer is used for the plant growth test, the various plant growth states are obvious, and no auxiliary material is needed to be added. Especially when the number of a plant's root systems increases by more than 30%, the root thickness also increases;
[0098] (4) The present invention improves the internal structure of the evaporator, which solves the difficulties in decolorizing the contaminated condensate in the biochemical treatment due to the high concentration of NH4 + -N. Meanwhile, the slightly contaminated condensate is directly used for washing, and the seriously contaminated condensate due to its high concentration of NH4 + -N, can be used to mix with the residue generated in the preparation of the pulping charge to produce the substrate or fertilizer, and can be used to pass flue gas desulfurization to produce digestion liquid for pulping using the ammonium sulfite method, that is, ammonium sulfite. This not only creates more economic benefits, but also reduces the operating cost of substrate or fertilizer fermentation, as well as the cost of pulping using the ammonium sulfite method;
[0099] (5) By adopting the method in the present invention, the water consumption per ton of pulp is 50 m3, which is much less than that of 80 to 150 m3 by the previous pulping technique;
[00100] (6) By the treatment method and device for water recycling adopted in the present invention, since the UPCB process is adopted, the reaction pattern is improved, the reaction time is increased, and the reaction is more adequate and effective. As a result, the consumption of chemicals is reduced, and the flow quality is improved. Meanwhile, the sludge in contact with the filtration mechanism is added, and the removal rate is increased. Only for applicants for the present invention, millions of RMB can be saved each year. Brief Description of Drawings
[00101] The following content is a brief description of the drawings. A very detailed description of the present invention can be made using the following drawings and in combination with the contents mentioned above.
[00102] Figure 1 illustrates the flow diagram of the process of cyclic use of grass straw mentioned in the present invention.
[00103] Figure 2 illustrates the schematic view of the air chamber structure of the evaporator mentioned in the present invention, where 1 refers to the upper dummy plate, and 2 refers to the lower dummy plate.
[00104] Figure 3 illustrates the schematic view of the UPCB treatment process in the method mentioned in embodiment 10 of the present invention.
[00105] Figure 4 illustrates the schematic view of the treatment of waste water from papermaking mentioned in embodiment 10 of the present invention.
[00106] Figure 5 illustrates the schematic view of Q2AO mentioned in embodiment 10 of the present invention.
[00107] Figure 6 and figure 7 illustrate the schematic structural views of UPCB reactors mentioned in embodiment 10 of the present invention.
[00108] Figure 8 illustrates the traditional A2O process.
[00109] Figure 9 illustrates the schematic view of the recycling water treatment method mentioned in embodiment 11 of the present invention. Detailed Description of the Preferred Embodiments
[00110] The following content is a detailed description of the preferred embodiments. A clearer understanding of the present invention can be obtained by the following embodiments and in combination with the specific descriptions mentioned above and the brief description of the drawings. Mode 1 Raw material and waste obtained from cargo preparation
[00111] Wheat straw raw materials for pulping and residues are obtained by preparing the conventional dry method load of wheat straw. Digestion of Raw Material
[00112] The pulping wheat straws obtained in the previous step are loaded into the rotary spherical digester, and the liquid chemical for digestion (ammonium sulfite) is added to the digester. The amount of ammonium sulfite is 15% of that of absolutely dry raw materials, with a liquid substance ratio of 1: 3.
[00113] The temperature is increased to 110 ° C during heating the first time, and this temperature is maintained for 40 minutes. Then the steam is released for 25 minutes. The temperature is raised within 40 minutes to 165 ° C, and is maintained for 75 minutes.
[00114] A highly solid pulp with a solidity of 21 (equivalent to a layer number of 34) is obtained. Extrusion
[00115] The highly solid pulp obtained in Step 2) is released into a double cylinder pulp extruder, which is used for the extraction of the black liquid substance in the prior art, for extrusion. After extrusion, a pulp of high solidity with a concentration of 25% and the concentrated black liquid substance are obtained. Pulp Washing and Black Liquid Substance Recycling
[00116] The highly solid pulp with a concentration of 25%, which is obtained in Step 3), is diluted to 2.5% using the black liquid substance at 70 ° C. Then the pulp is released into the washing machine with three-stage vacuum pulp for washing, then the washed pulp and the black liquid substance are obtained. The black liquid substance is recycled on digestion in Step 2). Oxygen delignification
[00117] The temperature of the washed pulp obtained in Step 4) is increased through the helical conveyor to 70 ° C. The pulp is then released into the medium concentration pulp tube. In the medium concentration pulp tube, the pulp is first fluidized by removing air in the pulp through thermal refining. It is then released into the reaction tower for oxygen delignification through the centrifugal medium concentration slurry pump. Before entering the reaction tower, the pulp in the tube is mixed with oxygen (with an addition amount of 30 kg per ton of pulp) and aqueous alkali (with an alkali amount of 3% of that of the pulp absolutely dried in sodium hydroxide), and heated by the steam that is released into the tube. Then, the pulp is intensely mixed, it is released in reaction tower No. 1 for delignification with oxygen. The protective agent is magnesium sulfate, the amount of which is 1.2% of the weight of the pulp absolutely dry. The inlet temperature is 98 ° C, and the pressure is 1.05 MPa. The pulp is kept in the tower for 85 minutes so that the complete delignification reaction is carried out. The temperature at the top of the tower is 102 ° C, and the pressure is maintained at 0.4 MPa. Then, the pulp, which is discharged by the trigger, is released in reaction tower No. 2 for delignification with oxygen through the medium concentration pump No. 2. 10 kg of oxygen and 10 kg of NaOH are added, and 20 kg of H2O2 are used as the reinforcer. The temperature and pressure are the same as those of reaction tower No. 1. The pulp is kept in it for 85 min. After treatment is complete, the pulp is blown out of the pulp chest for dilution.
[00118] An unbleached pulp with a fracture length of 5.3 km, a fold number of 80 times, a tear force of 220 mN, a whiteness of 45% ISO, and a degree of beat of 34 ° SR is obtained.
[00119] The unbleached pulp is first beaten in a cylindrical refiner, with a beat concentration of 3.8%, a beat pressure of 0.20 MPa, and a beat current of 65A. Then, the pulp is released in a double-disc refiner to beat, with a beat concentration of 3.3%, a beat pressure of 0.15 MPa, and a beat current of 50A. After the beat, a finished pulp with a beat degree of 48 ° SR and a wet beat weight of 2.9 g is obtained.
[00120] The beaten pulp is used to manufacture paper in a single-cylinder, one-way dryer toilet paper machine, with a base weight of (11.0 ± 2.0) g / m2, an untrimmed width of 2,900 mm and a speed of 260 m / min. Then unbleached paper with a base weight of 11.6 g / m2, a horizontal suction range of 50 mm / 100 s, a tensile index of> 8.3 Nm / g, a risk capacity of 176 mN and a brightness of 42% is obtained. Concentration of Black Liquid Substance
[00121] The black liquid substance obtained from Step 3) and Step 4) is evaporated and concentrated in a seven-part seven-part gas evaporator.
[00122] The temperatures for the six-fold effects are, respectively, as follows: from 110 to 100 ° C for Effect I, 90 to 100 ° C for Effect II, 80 to 90 ° C for Effect III, 70 to 80 ° C for Effect IV, 60 to 70 ° C for Effect V and 50 to 60 ° C for Effect VI. The concentration for various effects will be as follows (in Baumé grade): 5 to 8 for Effect VI, 7 to 10 for Effect V, 9 to 12 for Effect IV, 11 to 14 for Effect III; 14 to 17 for Effect II, and 18 to 21 for Effect I, for the first time passing from Effect II and Effect I, and 23 to 25 for Effect II, and 25 to 29 for Effect I for second pass of Effect II and Effect I. Then a concentrated black liquid substance (with a solids content of 60%, a Baumé grade 20, and a pH of 6), a severely contaminated condensate (with an NH4 + -N concentration 4000 mg / l, and a temperature of 70 ° C), and a slightly contaminated condensate (with an NH4 + -N concentration of 100 mg / l) are obtained. Fertilizer Preparation
[00123] The concentrated black liquid substance, lignin, humic acid, and mud are mixed in a slurry, with their mass percentage being 60%, 25%, 10% and 5% respectively. Then the spray granulation of the pulp is carried out, with a peak temperature of 600 ° C, and a final temperature of 55 ° C. Then, a solid state fulvic acid fertilizer is obtained, with grain sizes from 3 to 5 mm, a solidity of 23.4 N, an organic matter content of 60%, a total content of N + P2O5 + K2O 4%, and a fulvic acid content of 30%.
[00124] The condensate slightly contaminated with an NH4 + -N concentration of 100 mg / l is reused in the washing section in Step 4). Substrate Formation through Mixed Fermentation of Severely Contaminated Condensate and Residue
[00125] 1,000 kg of waste generated in Step 1) are collected, and 1) 000 kg of seriously contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 4,000 mg / l and a temperature of 70 ° C are added. The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.5. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When it becomes 35 ° C, fermentation is completed, with the pH being 6.5.
[00126] The organic substrate product obtained has 31.25% organic matter, 7.85% humic acid. Its total potassium content is 1.13%, the total phosphorus content is 0.12%, and the total nitrogen content is 1.13%. The aeration porosity is 38.8%, the total porosity is 49.64, and the porosity that holds water is 10.84%. In addition, there are some microelements: 22.53 mg / kg of copper, 62.70 mg / kg of zinc, 2.38 g / kg of iron, and 281.03 mg / kg of manganese.
[00127] The substrate obtained can be used for agricultural planting of wheat, but it is not limited to wheat only. Mode 2 1) Raw material and residues obtained from cargo preparation
[00128] The rice straw for pulping and the residue are obtained by preparing the load by the dry rice straw method through the hammer crusher. Then the rice straw for pulping is dipped in the organ of Corti for impregnation. The liquid impregnating substance is an aqueous alkali with an amount of alkali of 4% of that of the raw materials absolutely dried with sodium hydroxide, with a liquid substance ratio of 1: 4. After the straws are impregnated and mixed for 40 minutes in the liquid substance at a normal pressure and a temperature of 85 ° C, the impregnated raw materials are obtained. 2) Digestion of Raw Material
[00129] The impregnated raw materials obtained in Step 1) are sent to the rotary spherical digester, and the liquid chemical for digestion (ammonium sulfite) is added inside the digester. The amount of ammonium sulfite is 11% of that of the absolutely dry raw materials, with a liquid substance ratio of 1: 3.
[00130] Steam is supplied in the rotary spherical digester for heating at a temperature of 125 ° C, and the temperature is maintained for 40 minutes. The vapor is relieved on a small scale. The temperature is raised to 170 ° C, and the temperature is maintained for 75 minutes.
[00131] A highly solid pulp with a K value of 18 (equivalent to a layer number of 27) is obtained. 3) Extrusion
[00132] The highly solid pulp with a concentration of 15% obtained in Step 2) is released into a single cylinder pulp extruder from the entrance to the extrusion. After the black liquid substance is extruded, the pulp with a concentration of 30% is discharged from the outlet. The pulp of high solidity has a beat rate of 28 ° SR before extrusion, which becomes 29 ° SR after extrusion. The Baumé degree of the extruded black liquid substance is 11 ° B 'at 20 ° C. The concentration of residual ammonium sulphite in the black liquid substance is 8 g / l. 4) Pulp Washing and Black Liquid Substance Recycling
[00133] The pulp from the pulp extruder outlet in Step 3) is diluted by the diluted black liquid substance at a temperature of 60 ° C, so that the pulp concentration becomes 2.5%. Then, the pulp is released to a template screen for screening. Then the pulp is washed by the conventional method. After washing the pulp, the concentration of the pulp is adjusted to 10%. The black liquid substance obtained after washing the pulp is recycled for digestion in Step 2). 5) Oxygen delignification
[00134] The washed pulp obtained in Step 4) is defibrated by the demiller, and then released into the pulp tube of medium concentration. In the medium concentration pulp tube, the pulp is first fluidized by removing air in the pulp through thermal refining. Then, it is released in the reaction tower for oxygen delignification by the centrifugal medium concentration pulp pump. Before entering the reaction tower, the pulp in the tube is mixed with oxygen (with an addition amount of 20 kg per ton of pulp) and aqueous alkali (with an alkali amount of 4% of that of the pulp absolutely dried in sodium hydroxide), and heated by the steam that is released into the tube. Then, the pulp is intensely mixed, it is released in a reaction tower for oxygen delignification. The protective agent is magnesium sulfate, the amount of which is 1% of the weight of the pulp absolutely dry. The inlet temperature is 95 ° C, and the pressure is 0.9 MPa. The pulp is kept in the tower for 75 minutes so that the complete delignification reaction is carried out. The temperature at the top of the tower is 100 ° C, and the pressure is maintained at 0.5 MPa. After the treatment is complete, the pulp is blown out into the pulp tank for dilution. At this exact moment, the pulp strength is reduced to a K value of 10 (equivalent to a layer number of 13). Then with a pump, the diluted pulp is pumped into the vacuum pulp washer for washing, sorting and purification.
[00135] An unbleached pulp with a whiteness of 41% ISO, a fracture length of 5.2 km, a tear force of 240 mN, a folding number of 45 times, and a beat rate of 32 ° SR is obtained. 6) Concentration of Black Liquid Substance
[00136] The black liquid substance obtained from Step 3) and Step 4) is evaporated and concentrated in a seven-part seven-part gas evaporator.
[00137] The temperatures for the six-fold effects are respectively as follows: from 110 to 100 ° C for Effect I, 90 to 100 ° C for Effect II, 80 to 90 ° C for Effect III, 70 to 80 ° C for Effect IV, 60 to 70 ° C for Effect V and 50 to 60 ° C for Effect VI. The concentration for various effects will be as follows (in Baumé degree): 5 to 8 for Effect VI, 7 to 10 for Effect V, 9 to 12 for Effect IV, 11 to 14 for Effect III; 14 to 17 for Effect II, and 18 to 21 for Effect I, for the first time passing from Effect II and Effect I, and 23 to 25 for Effect II, and 25 to 29 for Effect I for second pass of Effect II and Effect I. Then a concentrated black liquid substance (with a solids content of 60%, a Baumé grade 20, and a pH of 6), a severely contaminated condensate (with an NH4 + -N concentration 5000 mg / l, and a temperature of 50 ° C), and a slightly contaminated condensate (with an NH4 + -N concentration of 90 mg / l) are obtained. 7) Preparation of Fertilizer
[00138] Mix the concentrated black liquid substance, lignin, humic acid, and sludge in the slurry, with their mass percentage being 50%, 35%, 10% and 5% respectively. KCI is added. Then the spray granulation of the pulp is carried out, with a peak temperature of 560 ° C, and a final temperature of 52 ° C. Then, a fulvic acid fertilizer in solid state is obtained, with grain sizes from 3 to 5 mm, a solidity of 19.4 N, an organic matter content of 65%, a total content of N + P2O5 + K2O 5%, and a fulvic acid content of 24%.
[00139] The condensate slightly contaminated with an NH4 + -N concentration of 90 mg / l is reused in the washing section in Step 4). 8) Substrate Formation through Mixed Fermentation of Severely Contaminated Condensate and Residue
[00140] 1,000 kg of waste generated in Step 1) are collected, and 3,000 kg of seriously contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 5,000 mg / l and a temperature of 50 ° C are added. The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.5. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When it becomes 35 ° C, fermentation is completed, with the pH being 6.5.
[00141] The organic substrate product obtained has 31.25% organic matter, 7.85% humic acid. Its total potassium content is 1.13%, the total phosphorus content is 0.12%, and the total nitrogen content is 1.13%. The aeration porosity is 38.8%, the total porosity is 49.64, and the porosity that holds water is 10.84%. In addition, there are some microelements: 22.53 mg / kg of copper, 62.70 mg / kg of zinc, 2.38 g / kg of iron, and 281.03 mg / kg of manganese.
[00142] The substrate obtained can be used for agricultural rice planting, but it is not limited to rice only. Mode 3
[00143] 1) Reed raw materials for pulping and residues are obtained through the preparation of load by the dry reed method by hammer crusher.
[00144] 2) Digestion of Raw Material
[00145] The chemical for digestion (ammonium sulfite) is added to the reed raw materials for the pulping obtained in Step 1). Then digestion is performed with continuous digestion in a horizontal tube. The amount of ammonium sulfite is 10% of that of absolutely dry raw materials, with a liquid substance ratio of 1: 3.5.
[00146] Steam is supplied for heating at a temperature of 172 ° C, which totally takes 35 to 40 minutes.
[00147] A highly solid pulp with a K value of 27 is obtained.
[00148] 3) Extrusion
[00149] The pulp obtained in Step 2) is extruded by the conventional method to obtain the extruded pulp and the concentrated black liquid substance.
[00150] 4) Washing of Pulp and Recycling of Black Liquid Substance
[00151] The extruded pulp obtained in Step 3) is washed by the conventional method to obtain the washed pulp and the diluted black liquid substance.
[00152] 5) Oxygen delignification
[00153] Defibration and oxygen delignification are performed for the washed pulp obtained in Step 4) by the conventional method. An unbleached pulp with a whiteness of 45% ISO, a fracture length of 5.0 km, a fold number of 90 times, and a tear force of 230 mN is obtained.
[00154] Then the beating and papermaking are carried out on the pulp by the conventional method to obtain the unbleached paper.
[00155] 6) Concentration of Black Liquid Substance
[00156] The diluted black liquid substance obtained in Step 3) and the black liquid substance obtained in Step 4) are mixed to obtain a new black liquid substance with a solids content of 15% and a Baumé grade of 9. Then the black liquid substance is evaporated and concentrated in a conventional five-fold evaporator. The concentrated black liquid substance with a solids content of 30%, a Baumé degree of 18, and a pH value of 11 is obtained, so it is a contaminated condensate with an NH4 + -N concentration of 1,800 mg / L and a temperature 60 ° C.
[00157] 7) Preparation of Fertilizer
[00158] The concentrated black liquid substance, lignin and humic acid are mixed in the slurry, with their percentage of mass respectively being 30%, 45% and 25%. Then a fulvic acid fertilizer is obtained through direct drying, with an organic matter content of 70%, a total N + P2O5 + K2O content of 4%, and a fulvic acid content of 5%.
[00159] 8) Substrate Formation through Mixed Fermentation of Severely Contaminated Condensate and Residue
[00160] 1,000 kg of waste generated in Step 1) are collected, and 3,000 kg of contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 1,800 mg / l and a temperature of 60 ° C are added. The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.6. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When it becomes 35 ° C, fermentation is completed, with the pH being 6.5. The obtained organic substrate product has 20% organic matter, 10% humic acid. Its total potassium content is 1.5%, the total phosphorus content is 0.3%, and the total nitrogen content is 1%. Aeration porosity is 35%, total porosity is 45, and the porosity that holds water is 8%. In addition, there are some microelements: 22.56 mg / kg of copper, 62.56 mg / kg of zinc, 2.42 g / kg of iron, and 281.10 mg / kg of manganese.
[00161] The obtained substrate can be used for the reed agricultural plantation. Mode 4
[00162] 1) The raw materials of cotton stalks for pulping and waste are obtained by preparing the filler using the conventional dry method of cotton stalks.
[00163] 2) Digestion of Raw Material
[00164] The raw materials of cotton stalk for pulping obtained in Step 1) are loaded into the continuous digester. Then the chemical for digestion (ammonium sulfite) is added inside the continuous digester. The amount of ammonium sulphite is 15% of that of the absolutely dry raw materials, with a liquid substance ratio of 1: 3.5.
[00165] Steam is supplied for heating at a temperature of 172 ° C, which totally takes 40 minutes.
[00166] A highly solid pulp with a K value of 20 is obtained.
[00167] 3) Extrusion
[00168] The pulp obtained in Step 2) is extruded by the conventional method to obtain the extruded pulp and the concentrated black liquid substance.
[00169] 4) Washing the Pulp and Recycling the Black Liquid Substance
[00170] The extruded pulp obtained in Step 3) is washed by the conventional method to obtain the washed pulp and the diluted black liquid substance. The diluted black liquid substance can be partially reused for digestion in Step 2).
[00171] 5) Oxygen delignification
[00172] Defibration and oxygen delignification are performed for the washed pulp obtained in Step 4) by the conventional method. An unbleached pulp with a whiteness of 23% ISO, a tear strength of 280 mN, a fracture length of 6.0 km, and a fold number of 40 times is obtained.
[00173] Then the beating and papermaking are carried out on the pulp by the conventional method to obtain the unbleached paper.
[00174] 6) Concentration of the Black Liquid Substance
[00175] The diluted black liquid substance obtained from Step 3) is evaporated and concentrated in a seven-part seven-part gas evaporator. The temperatures for the six-fold effects are respectively as follows: from 110 to 100 ° C for Effect I, 90 to 100 ° C for Effect II, 80 to 90 ° C for Effect III, 70 to 80 ° C for Effect IV, 60 to 70 ° C for Effect V and 50 to 60 ° C for Effect VI. The concentration for various effects will be as follows (in Baumé degree): 5 to 8 for Effect VI, 7 to 10 for Effect V, 9 to 12 for Effect IV, 11 to 14 for Effect III; 14 to 17 for Effect II, and 18 to 21 for Effect I, for the first time passing from Effect II and Effect I, and 23 to 25 for Effect II, and 25 to 29 for Effect I for second pass of Effect II and Effect I. Then a concentrated black liquid substance (with a solids content of 63%, a Baumé degree 39, and a pH of 5), a severely contaminated condensate (with a concentration of NH4 + - N of 4300 mg / l, and a temperature of 65 ° C), and a slightly contaminated condensate (with an NH4 + -N concentration of 85 mg / l) are obtained.
[00176] 7) Preparation of Fertilizer
[00177] The concentrated black liquid substance, lignin, and humic acid are mixed in the slurry, with their mass percentage being 80%, 5% and 15% respectively. KCI is added. Then a solid-state fulvic acid fertilizer is obtained, with an organic matter content of 67%, a total N + P2O5 + K2O content of 4%, and a fulvic acid content of 40%. The slightly contaminated condensate with an NH4 + -N concentration of 85 mg / l is reused in the washing section in Step 4).
[00178] 8) Substrate Formation through Mixed Fermentation of Severely Contaminated Condensate and Residue
[00179] 1,000 kg of residual cotton stalks generated in Step 1) are collected, and 3,500 kg of seriously contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 4,300 mg / l and a temperature of 65 ° C are added . The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.6. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When it becomes 26 ° C, fermentation is completed, with the pH being 7.2. The obtained organic substrate product has 30% organic matter, 15% humic acid. Its total potassium content is 1.8%, the total phosphorus content is 0.4%, and the total nitrogen content is 1.5%. Aeration porosity is 40%, total porosity is 55, and the porosity that holds water is 12%. In addition, there are some microelements: 22.63 mg / kg of copper, 62.62 mg / kg of zinc, 2.51 g / kg of iron, and 281.12 mg / kg of manganese.
[00180] The obtained substrate can be used for agricultural cotton plantation. Mode 5 1) Raw material and residues obtained from cargo preparation
[00181] The raw materials for pulping and the residues are obtained through the preparation of load by the dry method by hammer crusher using the rice straw and wheat straw with a mass ratio of 1: 3. 2) Digestion of Raw Material
[00182] The raw materials for pulping obtained in Step 1) are loaded into a spherical batch digester. Then, the chemical for digestion (ammonium sulphite) is added to the continuous digester. The amount of ammonium sulphite is 13% of that of the absolutely dry raw materials, with a liquid substance ratio of 1: 3.5. The steam is supplied for heating at a temperature of 115 ° C, and the temperature is maintained for 35 minutes. The vapor is relieved on a small scale. The temperature is raised to 172 ° C, and the temperature is maintained for 70 minutes. A pulp of high solidity with a concentration of 14% and a K value of 19 is obtained. 3) Extrusion
[00183] The pulp obtained in Step 2) is extruded by the conventional method to obtain the extruded pulp and the concentrated black liquid substance. 4) Pulp Washing and Black Liquid Substance Recycling
[00184] The extruded pulp obtained in Step 3) is washed by the conventional method to obtain the washed pulp and the diluted black liquid substance. 5) Oxygen delignification
[00185] Defibration and delignification with double-stage oxygen are performed for the washed pulp obtained in Step 4) by the conventional method. An unbleached pulp with a whiteness of 50% ISO, a fracture length of 5.0 km, a tear force of 200 mN, a fold number of 45 times, and a beat rate of 42oSR is obtained. Then pulping and papermaking are carried out using the conventional method to obtain the paper with lower whiteness. 6) Concentration of the Black Liquid
[00186] The concentrated black liquid substance obtained in Step 3) and the diluted black liquid substance obtained in Step 4) are mixed to obtain a new black liquid substance with a solids content of 15% and a Baumé grade of 9. Then the black liquid substance is evaporated and concentrated. The concentrated black liquid substance with a solids content of 30%, a Baumé grade of 18 is obtained, thus it is a condensate contaminated with an NH4 + -N concentration of 1,600 mg / L and a temperature of 55 ° C. 7) Preparation of Fertilizer
[00187] The concentrated black liquid substance, lignin and humic acid are mixed in the slurry, with their percentage of mass respectively being 30%, 45% and 25%. Then a fulvic acid fertilizer is obtained through direct drying, with an organic matter content of 70%, a total N + P2O5 + K2O content of 4%, and a fulvic acid content of 5%. 8) Substrate Formation through Mixed Fermentation of Contaminated Condensate and Residue
[00188] 1,000 kg of waste generated in Step 1) are collected, and 4,500 kg of contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 1,600 mg / l and a temperature of 55 ° C are added. The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.6. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When at 32 ° C, fermentation is completed, with the pH being 8.2. The obtained substrate has 30% organic matter, 15% humic acid. In addition, there are some microelements: 22.63 mg / kg of copper, 62.62 mg / kg of zinc, 2.51 g / kg of iron, and 281.12 mg / kg of manganese.
[00189] 9) The fertilizer obtained in Step 7) can be used for the agricultural planting of rice and wheat, but it is not limited to rice and wheat. After harvesting, rice straws and wheat straws can be reused in Step 1) for cargo preparation, in order to enter the circulation mentioned above. Mode 6 1) Raw material and residue obtained from cargo preparation
[00190] The raw materials of bamboo cane for pulping with a length of 30 mm and the residue are obtained through the preparation of cargo by the conventional dry method of bamboo canes. 2) Digestion of Raw Material
[00191] The raw materials of bamboo cane for pulping obtained in Step 1) are loaded into the digester by the packer through the hot black liquid substance with a temperature of 140 ° C. When the digester is completely filled, the cover is closed. The chemical for digestion with a temperature of 160 ° C is added to the digester. In said chemical for digestion, the amount of ammonium sulfite is 15% that of the absolutely dry raw materials, and the liquid substance ratio is 1:10. Meanwhile, the air in the digester is discharged, and the pressure is increased to 0.75 MPa. The circulation pump for heating the digestion liquid in the system and the still heated tube are used to heat the digestion liquid to 173 ° C. The period of temperature rise, thermal insulation, and displacement, lasts 220 minutes. The final pH value is adjusted to 8.5. Finally, the slurry is released into the expansion tank via the pumps. After digestion, a bamboo cane pulp with a K value of 16 (equivalent to a cover number of 24) and a beat rate of 10 ° SR is obtained. 3) Extrusion
[00192] The concentration of the bamboo cane pulp obtained in Step 2) is adjusted to 10% using the black liquid substance. The pulp is then released into the single screw pulp extruder for the treatment of the concentrated black liquid discharge. The concentrated black liquid substance obtained can be used as the water reducer for subsequent evaporation. The pulp concentration is increased from 10% before extrusion to 30% after extrusion.The concentration of the black extruded liquid substance is 9Be '(20 ° C), and that of residual ammonium is 14 g / L. Bamboo cane pulp is diluted to 3.0% using the black liquid substance diluted with a temperature of 60 ° C and a concentration of 6.1 ° Be '. The pulp is released in the template screen for the screening of the thick pulp, with the loss in 0.3% feedback screen, impurities are removed by the treatment of high concentration slag removal, with a loss of 0.2%. 4) Pulp Washing and Black Liquid Substance Recycling
[00193] The bamboo cane pulp is washed by the vacuum pulp washer type drum for washing. The washing temperature is 65 ° C. The degree of beating of the thick pulp that enters the pulp washer is 31 ° SR. 5) Oxygen delignification
[00194] The heated pulp is released in the slurry of medium concentration pulp for thermal refining, and then released in the reaction tower for oxygen delignification for the treatment of delignification through the medium concentration pump. After that, the pulp is washed again by the black liquid substance for oxygen delignification. The wet weight of the washed pulp is 1.8 g, and the residual fluid after washing the pulp is 440 ppm.
[00195] The concentration of the washed pulp is 9%. An unbleached pulp with a 40% ISO whiteness, a fracture length of 7,200 m, a tear strength of 250 mN, a fold number of 45 times, and a beat rate of 32 ° SR is obtained. The blending is performed, respectively, for 70% (by weight) of the unbleached pulp mentioned above and 30% of the bleached wood pulp. The pulp concentration of unbleached pulp is 3.0%, while that of wood pulp is 4.5%. The mixing is performed in a double disc refiner. The quality standards for the finished pulp after the beat are as follows: the beat rate of the unbleached pulp is 35 ° SR, and the wet weight for the beat is 1.6 g; the beat rate of the wood pulp is 46 ° SR, and the wet weight for the beat is 2.0 g. The bleached wood pulp is the only one treated by the prior art, including NBKP, needle bleached sulphite wood pulp, etc. The beaten pulp is used for making paper in paper machines commonly used in the prior art. Unbleached scholastic paper with a basis weight of 70 g / m2 is obtained. 6) Concentration of Black Liquid Substance
[00196] The black extruded liquid substance obtained from Step 3), with a concentration of 9Be '(20 oC) and a concentration of residue of 14 g / L, is evaporated and concentrated in a gas evaporator of sixfold effect and seven parts. The temperatures for the six-fold effects are respectively as follows: from 110 to 100 ° C for Effect I, 90 to 100 ° C for Effect II, 80 to 90 ° C for Effect III, 70 to 80 ° C for Effect IV, 60 to 70 ° C for Effect V and 50 to 60 ° C for Effect VI. The concentration for various effects will be as follows (in Baumé degree): 5 to 8 for Effect VI, 7 to 10 for Effect V, 9 to 12 for Effect IV, 11 to 14 for Effect III; 14 to 17 for Effect II, and 18 to 21 for Effect I, for the first time passing from Effect II and Effect I, and 23 to 25 for Effect II, and 25 to 29 for Effect I for second pass of Effect II and Effect I. Then a concentrated black liquid substance (with a solids content of 65%, a Baumé degree 40, and a pH of 5), a severely contaminated condensate (with a concentration of NH4 + - N of 4500 mg / l, and a temperature of 25 ° C), and a slightly contaminated condensate (with an NH4 + -N concentration of 80 mg / l) are obtained. 7) Preparation of Fertilizer
[00197] The concentrated black liquid substance, lignin, and humic acid are mixed in the slurry, with its mass percentage being 80%, 5% and 15% respectively. KCI is added. Then a solid-state fulvic acid fertilizer is obtained, with an organic matter content of 67%, a total N + P2O5 + K2O content of 4%, and a fulvic acid content of 40%. The slightly contaminated condensate with an NH4 + -N concentration of 80 mg / l is reused in the washing section in Step 3). 8) Substrate Formation through Mixed Fermentation of Contaminated Condensate and Waste
[00198] 1,000 kg of waste generated in Step 1) are collected, and 4,000 kg of seriously contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 4,500 mg / l and a temperature of 25 ° C are added. The mixture before fermentation is obtained by mixing and stirring it evenly. In the mixture, the water content is 60%, the ratio of the mass percentage of carbon to the mass percentage of nitrogen is 25: 1, and the pH value is 9.8. After mixing, the mixture undergoes spontaneous aerobic fermentation. The temperature during fermentation is monitored. The temperature keeps rising during fermentation. After it reaches 55 to 60 ° C, it will remain for 25 days. Then it falls. When it comes to 40 ° C, the fermentation is completed, with the pH being 6.5. The obtained organic substrate product has 50% organic matter, 20% humic acid. Its total potassium content is 2.0%, the total phosphorus content is 0.5%, and the total nitrogen content is 2%. The aeration porosity is 50%, the total porosity is 60, and the porosity that holds the water is 20%. In addition, there are some microelements: 22.48 mg / kg of copper, 62.65 mg / kg of zinc, 2.38 g / kg of iron, and 281.03 mg / kg of manganese.
[00199] The obtained substrate can be used for the agricultural planting of bamboo canes, but it is not limited only to bamboo canes. Mode 7
[00200] The substrate preparation is done according to the method in mode 1. The difference is that the raw materials for fermentation are respectively the culture by-product such as rice straw, or organic waste in household waste, and the mixture of the culture by-product such as rice straw, organic waste in household waste and the by-product of the preparation of pulping load, with a mixing weight ratio of 1: 1. The fertilizer obtained has basically the same effect as that in modality 1. Comparison Example 1 (Comparison Table of Physical and Chemical Indicators for Substrate and Peat)
Resultados de testeQuando o valor EC do substrato for 1,93 Ms/cm, e a condutividade de substrato (valor EC) for < 2,6 Ms/cm, não há nenhum dano para as várias culturas; O valor de pH do substrato é 7,95, enquanto que a do substrato de turfa é de 4,5 a 7,5, sem diferença óbvia; Os teores médios de N, P e K no substrato de turfa são como se segue: 0,49 % a 3,27 % para o nitrogênio total, 0,01 % a 0,34 % para o fósforo total e 0,01 % a 0,59 % para o potássio total. Os teores do nitrogênio total, fósforo total e potássio total no substrato na presente invenção são respectivamente 2,3 vezes, 12 vezes e 57 vezes daqueles do substrato de turfa;[00201] The following table is the comparison table of the physical and chemical indicators for the substrate and peat for the present invention. Test results When the EC value of the substrate is 1.93 Ms / cm, and the substrate conductivity (EC value) is <2.6 Ms / cm, there is no damage to the various cultures; The pH value of the substrate is 7.95, while that of the peat substrate is 4.5 to 7.5, with no obvious difference; The average levels of N, P and K in the peat substrate are as follows: 0.49% to 3.27% for total nitrogen, 0.01% to 0.34% for total phosphorus and 0.01% 0.59% for total potassium. The contents of total nitrogen, total phosphorus and total potassium in the substrate in the present invention are 2.3 times, 12 times and 57 times respectively of those of the peat substrate;
[00202] From the test results above, we can see that the levels of total nitrogen, total phosphorus and total potassium in the substrate are higher than those of peat, so is the aeration porosity. Therefore, the effect of the substrate is better than that of the peat substrate. Mode 8 1) Raw material and residues obtained from cargo preparation
[00203] Bagasse raw materials for pulping are obtained through the preparation of cargo by the conventional dry bagasse method. 2) Digestion of Raw Material
[00204] The pulp bagasse raw materials obtained in the previous step are loaded into a rotary spherical digester. Then the chemical for digestion (ammonium sulfite) is added inside the rotary spherical digester. The amount of ammonium sulphite is 10% of those absolutely dry raw materials, with a liquid substance ratio of 1: 3.5. The steam is supplied for heating at a temperature of 115 ° C, and the temperature is maintained for 35 minutes. The vapor is relieved on a small scale. The temperature is raised to 172 ° C, and the temperature is maintained for 70 minutes. A pulp of high strength with a concentration of 14% of a K value of 18 is obtained. 3) Extrusion
[00205] The pulp obtained in Step 2) is extruded by conventional method to obtain the extruded pulp and the concentrated black liquid substance. 4) Pulp Washing and Black Liquid Substance Recycling
[00206] The extruded pulp obtained in Step 3) is washed by the conventional method to obtain the washed pulp and the diluted black liquid substance. 5) Oxygen delignification
[00207] Defibration and delignification with single stage oxygen are performed for the washed pulp obtained in Step 4) by the conventional method. An unbleached pulp with a whiteness of 40% ISO, a fracture length of 4.5 km, a tear strength of 300 mN, a folding number of 30 times, and a beat rate of 32oSR is obtained. Then pulping and papermaking are carried out using the conventional method to obtain unbleached paper. 6) Concentration of Black Liquid Substance
[00208] The black liquid substance obtained in Step 3) and the black liquid substance obtained in Step 4) are mixed to obtain a new diluted black liquid substance with a solids content of 15% and a Baumé grade of 9. Then the black liquid substance is evaporated and concentrated. The concentrated black liquid substance with a solids content of 30%, a Baumé grade of 18 is obtained, so it is a contaminated condensate with an NH4 + -N concentration of 1,700 mg / L and a temperature of 48 ° C. 7) Preparation of Fertilizer
[00209] The concentrated black liquid substance, lignin and humic acid are mixed in the slurry, with their mass percentage being 30%, 45% and 25% respectively. Then a fulvic acid fertilizer is obtained through direct drying, with an organic matter content of 70%, a total N + P2O5 + K2O content of 4%, and a fulvic acid content of 5%. 8) Generation of Ammonium Sulphite and Substrate Formation through Mixed Fermentation
[00210] The contaminated condensate obtained in Step 6) with an NH4 + -N concentration of 1,700 mg / l and a temperature of 48 ° C is used for the desulfurization of residual flue gases to obtain the ammonium sulphite, which is used as the digestion liquid in the ammonium sulfite method in Step 2) for digestion. The method for desulphurising waste flue gases is a method that uses the prior art.
[00211] Or the addition is done during substrate fermentation in Mode 1 - Mode 3, which provides the additional nitrogen source to enter the circulation. Mode 9
[00212] It is the same as the other embodiments, with the following differences: 8) Generation of Ammonium Sulphite and Substrate Formation through Mixed Fermentation
[00213] The severely contaminated condensate obtained with an NH4 + -N concentration of 4,000 mg / l and a temperature of 70 ° C is used for flue gas desulphurisation to obtain ammonium sulphite, which is used as the liquid of digestion in the ammonium sulfite method in Step 2) for digestion.
[00214] The method for flue gas desulfurization is the method in the present invention, the steps of which are as follows: first, the flue gas is subjected to dust removal treatment in the electrostatic cleaning device and, then pressurized on the draft fan; the flue gas is released into the Venturi tube, which is connected to the water tank with residual ammonia; the mixture of the severely contaminated condensate obtained and water with ammonia is injected into the venturi tube to absorb the sulfur dioxide, obtaining the mixed liquid substance of ammonium bisulfite.
[00215] The liquid substance mixed with flue gases that flows out of the Venturi tube is released in the leaching assembly at the bottom of the desulfurization tower. The excessive amount of mixed liquid substance of severely contaminated condensate and water with ammonia is injected to react with ammonium bisulfite to produce ammonium sulfite.
[00216] In the leaching set, a mixture of water with ammonia of ammonium bisulfite and ammonium sulfite is obtained. The mixed liquid substance is pumped to the highest position in the tower, and then ejected downward through the three-layer sprinkler in the middle of the tower. Then the liquid substance and the flue gas flowing above are uniformly mixed. As a result, the residual sulfur dioxide in the flue gas is absorbed. The ammonium bisulfite in the mixed liquid substance reacts with sulfur dioxide to produce ammonium sulfite, and then the liquid substance is released into the leaching set. The steps are repeated until the sulfur dioxide in the flue gas is completely absorbed.
[00217] In addition, there is a sprinkler for fresh water at the top of the tower, which is used to absorb the ammonia that escapes the desulfurization process. The absorbed ammonia is returned to the leaching set, and then added to the circulation to absorb sulfur dioxide by spraying.
[00218] There is a pH detector in the desulfurization tower. When the pH in the desulfurization tower reaches 7.5, that is, the equilibrium state is reached between ammonium sulphite and ammonium bisulfite, the liquid substance is discharged into the ammonium sulphite tank. After sedimentation, filtration and purification, the liquid substance is released into the ammonium sulphite storage tank, which will be used for pulping by the ammonium sulphite method.
[00219] The exhaust gas, after absorbing fresh water at the top of the desulfurization tower, is vented from the top of the tower, and then released into an ammonia absorption tower through the draft fan. In the ammonia absorption tower, the residual ammonia in the exhaust gas is absorbed by fresh water to produce diluted ammonia water, which will be released into the ammonia water tank. The concentration of water with ammonia is adjusted to 1% ~ 2%. Then the ammonia water is released into the water tank with residual ammonia. The sulfur dioxide in the flue gas is absorbed and reused. In addition, water with residual ammonia generated in other industries can be used in the water tank with residual ammonia. After the concentration is adjusted to an acceptable level, water with residual ammonia will be used for the absorption of exhaust gas. The exhaust gas, after absorption, is vented, with the absorption rate of sulfur dioxide up to 99.5%.
[00220] The liquid substance mixed with ammonium sulfite produced in the previous steps is used as the chemical for digestion in the method of ammonium sulfite in Step 2) of modality 1, which will be added in the digester for digestion and subsequent processes, forming the circulation. Mode 10
[00221] Water treatment methods in this modality include filtration, flocculation sedimentation, biochemical treatment, and advanced treatment.
[00222] Flocculation sedimentation is the UPCB treatment.
[00223] The biochemical treatment is the QA2O treatment.
[00224] Advanced treatment includes regular precipitation separation steps.
[00225] Filtration is microfiltration, with the number of meshes being 80 to 120.
[00226] In addition, the steps for the treatment of dehydration of the mud obtained in UPCB and QA2O are included.
[00227] For the issues mentioned above, the researchers of the present invention invented a process that integrates the advantages of vortex reactor, cyclone reactor and porous plate reactor, as well as integrating sludge circulation technology, contact filtration technology mud, and optional and anaerobic decomposition of microorganisms. The detailed process flow is as follows.
[00228] Reference to figure 3. The discharge water in the papermaking is first released in the retention basin, in which the flocculants are added. The discharge water and flocculants are intensively mixed by the pump and the lift pipe. Then the mixture is released in the hybrid reaction layer of the UPCB reactor.
[00229] Preferably, the dissipating water is filtered before entering the collection basin, and sand formed in rapids in the granulation basin, in order to remove the sand, the fiber, part of the lignin, pigment, etc. The common treatment methods in the prior art are adopted for the filtration and treatment of rapids forming sand in the granulation basin, which can be properly selected by the common technical team in the field according to the requirements. In addition, all selections are included in the scope of the routine design, so that no creative work is required to be performed.
[00230] After that, the optional, aerobic and cyclic sludge is added at the limit between the hybrid reaction layer and the increased reaction layer, so that the flocculation sedimentation can be completely completed.
[00231] Then, the flocculants are added or not added to it. Coagulation aids are added to the water in the sedimentation basin after the UPCB adsorption filtration layer, so that the flocculation sedimentation can be completed more effectively, and the liquid supernatant is easier to separate.
[00232] As for the dosage point, the commonly used flocculants can be added. The flocculants can be properly selected by the common technical team in the field according to the requirements. The selection is obvious to the team, so that no creative work is needed to be done. Flocculants include liquid flocculants (PAC, PAFC, PSAC, PSFAC, etc.).
[00233] The dosing point "a" is before the lift pump. The dosage concentration is 1 to 10%, with 3 to 6 preferable. There is no special limitation for the dosage method. Flocculants can be added via a fluoroplastic pump or inhaled by negative pressure before the pump.
[00234] After intensive mixing, the discharge water is released in the hybrid reaction layer of the UPCB reactor.
[00235] The discharge water, with the mixed chemical, enters the lower part of the round UPCB reactor along the tangent, with an upward declination angle of 15 to 45 °. Water in this region or within the entire reactor is maintained in a state of rotational flow. According to the need, such devices as the cyclone reactor, a mixed flow reactor, pore plate reactor, etc., can be equipped in this region, so that the state of rotational flow can be maintained.
[00236] Dosing point b is located at the limit between the hybrid reaction layer and the increased reaction layer. This point is on the central axis of the reactor, where anaerobic, facultative, aerobic and physicochemical flocculent sludge is added. There is no special limitation on the added sludge, as long as it can work according to the description above. According to the needs, the common technical team in the field can select the appropriate sludge using conventional technologies. The selection is obvious to the team, so that no creative work is needed to be done.
[00237] The UPCB adsorption filtration layer is located on the upper part of the reactor, which consists mainly of flow pipe, guide plate, doser, filter screen agitator, etc. During operation, a mud filtration layer with a certain thickness is formed in the upper median part of this layer, which is in a semi-fluid state. It can capture large amounts of small, non-flake SS in the increased reaction area. Taking the filter screen as the dividing line, the part above the screen is the flow reaction area for the slurry and water mixture, and the part below the screen is the filtration area of the suspended mud with high concentration . The filter screen can be nylon, polyester or stainless steel, etc., with the number of meshes ranging from 20 to 40. The thickness of the mud layer varies according to the reactor sizes. However, in the industrial process, considering the size of the general equipment, the thickness of the mud layer is generally 1 to 2 m in general.
[00238] Preferably, a dosage point d is added, in which more coagulant auxiliaries can be added, so that the flake is denser and larger, and the water is clearer. Coagulant aids are those most commonly used in the field. The common technical team in the field can determine coagulant auxiliaries through simple tests. The dosage at this point is preferable to be 0.2 to 5 ppm.
[00239] In order to remove the sludge in the circulation more effectively, the hydraulic retention time is preferably controlled within 4 to 10 hours. When the retention time is very short, the biological effect is not clear; when it is too long, the mud tends to float upwards.
[00240] During the removal of SS and coloform in the reactor, pollutants of large particulate matter in the water are removed, and the optional anaerobic acidification reactions by hydrolysis occur to some extent. So it is necessary that subsequent anaerobic, aerobic and other treatments are much easier to perform. The effects of UPCB technology are shown in the following table:
[00241] By the discharge water treatment method in the present invention, the recycling rate of the discharge water is above 60%.
[00242] QA2O consists mainly of three stages, that is, A1, A2 and O, but varies widely from the conventional A2O process. A1, A2 and S are separately configured, and the stages are respectively A1 (complex reaction aeration basin), A2 (pulsed water distribution upstream anaerobic reactor), and O (multistage delayed AO aeration basin ). The process has a strong ability to remove pollutants such as SS, COD, BOD, etc. The conventional A2O mud circulation extends throughout the process. The massive circulation of liquid substance mixed in the aerobic tank occurs in Stage A2 and Stage O, in order to remove nitrogen and phosphorus.
[00243] From the two flowcharts, it can be seen that there are relatively large differences between the QA2O process and the conventional A2O process. In the conventional A2O process, the sludge is circulated in the three stages, that is, A1, A2 and S, there is no intermediate sedimentation basin in the center, there is a circulation of mixed liquid substance between Stage A2 and Stage O; in the three stages, A1 is anaerobic, A2 is optional, and O is aerobic. In the QA2O process, Stage A1 mainly adopts facultative bacteria, however, it conforms to physicochemical reactions. The sedimentation basin is built separately for this stage, so is the mud circulation system; Stage A2 mainly adopts facultative bacteria, mandatory anaerobic bacteria, so it is a completely anaerobic process; Stage A2 has its independent mixed liquid substance circulation system, so it does not depend on the recycling of mud from Stage A1 and Stage O; o Stage The main mind adopts aerobic bacteria; in Stage O, the multi-stage cascade of oxygen enrichment and oxygen deficit stages (ie, multi-stage AO) is performed by supplying alternative oxygen from the aeration equipment; in addition, a biological selection basin is built before Stage O, in order to optimize the strains.
[00244] The process mainly has five functions: SS removal, nitrogen removal, phosphorus removal, increased biodegradable capacity and degradation of COD and BOD.
[00245] (1) Stage A1 takes SS removal as the main task, meanwhile it triggers the denitrification of the nitrifying acid combination reaction, and performs the removal of nitrogen and phosphorus (refers to the aeration basin part of the complex reaction for more information).
[00246] (2) Stage A2 takes anaerobic digestion as the main task, meanwhile it breaks down some organic macromolecule materials into organic micromolecule materials, intensifies the removal rate of the subsequent Stage O, and performs the release of phosphorus (refer to apart from the pulsating upstream anaerobic water distribution reactor for more information).
[00247] (3) Stage O provides full activity for aerobic bacteria, in the meantime it performs multi-stage AO alternation, and makes microorganisms more active in order to achieve a relatively high removal rate. In addition, long-term operation under low delayed loads produces large amounts of aerobic granular mud.
[00248] The reactor in question has the following aspects:
[00249] 1 - It is not a three-phase separator. This is one of the biggest differences between this anaerobic reactor and the conventional reactor. Due to the relatively large diameter / height ratio (5: 1), the flow rate of the discharge water is reduced, thus the purpose of solid-liquid separation is realized.
[00250] 2-0 pulsed water distribution system is adopted. With the help of siphon extraction, the A1 flow stored in the water dispenser for 3 ~ 5 minutes is discharged to the bottom of the basin with the flow rate returned in a short period of time (within twenty seconds). Then, the mud at the bottom of the basin is stirred upwards to produce the state of suspension. Therefore, the mud and the water are intensely mixed, so that the efficiency of the anaerobic reaction is guaranteed.
[00251] 3 - It is especially suitable for (but not limited to) the medium phase discharge water in the chemical pulp of wheat straw. It has a good relevance to cellulose, hemicellulose, polysaccharide, reducing sugar, modified starch from the overflow water in the overflow water, part of the lignin, and its derivatives in the overflow water, etc. It provides full activity to hydrolytic acidification in the decomposition of this macromolecule into a micromolecule, creating a good environment for aerobic treatment.
[00252] 4 - Anaerobic bacteria are granular mud and flaky mud. Conventional anaerobic bacteria, due to undersized diameters and high flow rate, cause severe loss of flaky mud, and consider the cultivation of granular anaerobic mud as the main purpose. However, this reactor allows the coexistence of granular sludge and flaky sludge, and allows it to work simultaneously, in order to achieve the highest removal effect, while increasing the removal capacity.
[00253] 5 - The treatment capacity of a single basin is high. The large diameter-length ratio significantly increases the treatment capacity of a single basin.
[00254] In the process of this modality: the average COD in water in the natural state of medium phase is 3800 mg / L, and after treatment by the system, the average COD in the UPCB flow is 1900 mg / L, the average COD in A1 is 1,280 mg / L, the average COD in the A2 stream is 730 mg / L, the average COD in the secondary sedimentation stream is 85 mg / L, and the SS is less than 50 mg / L.
[00255] Through the use of aerobic physicochemical and biochemical treatment methods in the prior art, the COD in water in its natural state is about 2500 mg / L. For physical-chemical treatment, the quantity of PAC flocculants is 800 ppm, and that of PAM is 5 ppm, and the COD in the flow is about 1850 mg / L. For aerobic biochemical treatment, when the hydraulic retention time is 96 hours, the COD in the flow is about 350 mg / L.
[00256] From the above descriptions, it can be concluded that the treatment cost of the prior art is higher than that of the process mentioned in this modality, and the flow is not stable and cannot reach the standards. Mode 11
[00257] The water treatment methods in this modality include filtration, sand circulation, flocculation sedimentation, separation and recycling.
[00258] In the filtration step in the present invention, conventional filtration technologies in the prior art can be used to remove sand, fiber, a part of the lignin, pigment, etc., remove large amounts of suspended solids (SS) and while this pulp recycling.
[00259] Preferably, the rotary microcoater is used for filtration. Steel mesh or nylon mesh with a mesh number of 80 to 120 is adopted. Preferably, the recycled pulp is concentrated in 2% (by weight) and then returned to the pulping system. The SS in the filtered discharge water is controlled within 800 mg / L.
[00260] There are sands in the filtered discharge water. In order to reduce the cost of recycling, improve the quality of the recycling water, and ensure the normal operation of the subsequent equipment, preferably the sand removal is performed by the discharge water. The sand removal methods commonly used in the prior art can be used.
[00261] Generally, the granulation basin is selected for the circulation of sand. The intermittent sand discharge is carried out at the bottom, and flocculation sedimentation is carried out by the liquid supernatant.
[00262] For the different recycling waters, that is, medium stages with different concentrations and levels of impurities, the total amount of flocculants is that with which the impurities can be sedimented. The common technical team in the field can determine the amount of flocculants by simple tests.
[00263] However, in this embodiment, preferably, the total amount of flocculent is 300 to 800 ppm of the weight of the recycled water to be treated.
[00264] Since the salt contents of the discharge water produced at different pulping stages are different, in the present invention, preferably, the discharge water is separated into discharge water with high salt content and discharge water with low salt content, and only low-salt discharge water is collected. Conventional filtration, sand circulation and flocculation sedimentation steps are used to remove sand, fiber, part of the lignin, pigment, etc., so that the discharge water can reach the discharge or recycling standards.
[00265] In the present invention, flocculation sedimentation consists of two stages: first, 10 to 30% (by weight) of the flocculants are added to the recycling water; from 70 to 90% of the flocculants are subjected to the salt removal treatment, then the flake subjected to the salt removal treatment is added to the recycle water to be treated in order to complete the flocculation sedimentation.
[00266] The salt removal treatment includes: making the flocculants flocculate in fresh water, and collecting the floc like flocculants in the flocculation sedimentation step.
[00267] The other salt removal treatment includes: making the flocculants flocculate in the recycling water to be treated, collecting the flake; perform acidification and anaerobic treatment of the flake. Acidification and anaerobic treatment can be performed by conventional technologies in the prior art, which is obvious to the common technical team in the field. To be more specific, it includes releasing the flake within the acidification set, controlling the temperature within 25 to 45 ° C, controlling the retention time within 8 to 12 hours, and cultivating the acid-producing bacteria, in the meantime controlling the solid-liquid separation, that is, to separate a sedimentation basin or concentration basin. After acidification, the flake is released into the anaerobic system to perform acidification, in order to guarantee the best performance of acid-producing bacteria; meanwhile, ensure the counter-flow agitation resistance, ensure the intensive mixing and flow of the strains, avoid the generation of granular mud, and control the hydraulic retention time within 20 to 36 hours, in order to facilitate the regeneration of the flake; then the regenerated flake is collected to be used as the flocculants in flocculation sedimentation.
[00268] Preferably, in the present invention, regeneration is carried out in the concentration of flakes of 3 to 5% (by weight). After the regeneration is completed, the pH is within 6 to 6.5.
[00269] In the present invention, there are no special limitations on the flocculants to be used. For example, prior art ferro-aluminum compound salt flocculants can be used.
[00270] In order to achieve better flocculation sedimentation effect, coagulation aids can be added. Similarly, there are no special limitations on the use of clotting aids. For example, the commonly used polyacrylamide coagulation aids can be selected. There is no special limitation on dosage, which can be properly selected by the common technical team in the field according to the requirements.
[00271] However, preferably, the dosage of the coagulation aids is 1 to 6 ppm of the weight of the discharge water to be treated. The runtime of the coagulation aids is preferably 1 to 3 minutes, with 2 minutes being the most preferable.
[00272] In flocculation sedimentation, preferably, first of all 10 to 30% of flocculants (by weight) are added in the recycle water to initiate the flocculation sedimentation in the recycle water. The dosing point GT is controlled in the range 106 to 108, where G is the speed gradient, while T is the stirring time. The time for the hybrid reaction is 2 to 8 minutes, with 4 to 6 minutes preferable, and 5 minutes the most preferable. Then, the flake that is subjected to the salt removal treatment and textured again is added to continue the flocculation sedimentation. The GT is controlled in the range of 105 to 106, and the time for the hybrid reaction is 5 to 15 minutes, with 6 to 10 minutes preferable, and 8 minutes the most preferable.
[00273] In this modality, preferably, sedimentation lasts from 2 to 12 hours in the sedimentation basin, with 4 to 8 hours preferable. Supernatant water is either directly discharged or recycled. From 30 to 50% of the precipitate is regenerated, that is, hydrolytic acidification and anaerobic treatment are performed, in order to obtain the flake for the treatment of recycled water, which will be used as the flocculants in the sedimentation. By the recycle water treatment method in the present invention, the average phase recycling rate reaches 70 to 80%.
[00274] In figure 9, the recycled water W is filtered in the filtration section, and the sand circulated in the granulation basin, in order to remove the sand, the fiber, part of the lignin, pigment, etc. The common treatment methods in the prior art are adopted for the filtration and treatment of sand circulation in the granulation basin, which can be properly selected by the common technical team in the field according to the requirements. In addition, all selections are included in the scope of routine design, so that no creative work is required to be performed.
[00275] Then the treated recycle water is released into the reaction tank, where the product is first subjected to flocculation sedimentation with part of the flocculants (say 10 to 30% by weight). Then, the flake submitted to the remaining salt removal treatment is added to perform the flocculation sedimentation, in order to guarantee complete flocculation sedimentation.
[00276] In this modality, 100% of the flake submitted to the salt removal treatment can be selected as the flocculants to perform the flocculation sedimentation. The dosage of the flocculants and the flocculation sedimentation process are the same or similar to those in the salt removal treatment for a part of the flocculants mentioned above. The common technical team in the field can do this through simple tests.
[00277] Preferably, coagulation aids are added to the recycle water, so that flocculation sedimentation can be completed more effectively, and the liquid supernatant is easier to separate.
[00278] After complete flocculation sedimentation, the treated recycle water is released into the sedimentation basin to separate the sludge. The liquid supernatant is collected in the collection basin and recycled in the papermaking section. The changes in the aspects of the discharge water before and after the recycling water recycling system are shown in the following table:
[00279] From the table, it can be seen that the system can effectively remove COD and SS in the discharge water, with the COD removal rate above 58%, and the SS removal rate above 85%. In addition, the operation of the system is stable, and there is almost no fluctuation in flow quality, which guarantees the quality of the recycled water.

权利要求:
Claims (10)
[0001]
1. Cyclic use method in the pulping and papermaking processes with straw, the method being characterized by the fact that it comprises the following steps: among the raw materials for agricultural planting, greenhouse and garden planting, selection of raw material straw raw material that is suitable for pulping, obtaining straw raw material for pulping by preparing the filler, obtaining a pulp with a Kappa number strength of 24 to 50 per digestion, then obtaining pulp by extrusion and washing, performing post-treatment for the pulp to obtain the paper pulp, and making a paper product; extract a black liquid substance during the extrusion and washing of the pulp with a Kappa number solidity of 24 to 50, obtaining a black liquid concentrated by evaporation and concentration, in which it is used as a first fertilizer to cyclically return to agricultural planting, greenhouse and garden planting for use; generate ammonium sulfite by mixing a contaminated condensate obtained from the evaporation process and concentration of the black liquid substance with gas desulfurization, and cyclically use ammonium sulfite in the digestion in step (1), obtaining a residue after the preparation of the load , mixes the residue with the contaminated condensate, obtaining a second fertilizer by fermentation, return of the second fertilizer for agricultural planting, greenhouse and garden planting for use, which can result in the cyclical availability of the straw raw material; use of recycled water from intermediate phase water processing in the corresponding phases in an integral pulping process, intermediate phase water processing which includes filtration, flocculation sedimentation, biochemical treatment, and advanced treatment; the advanced treatment including a precipitation separation step and flocculation sedimentation being performed by the upstream flow physical and chemical bed treatment (UPCB); the UPCB treatment, which includes: first, a discharge water totally mixed with flocculants being introduced into a hybrid reaction layer of a UPCB reactor; then the optional, aerobic and cyclic sludge being added to the discharge water at the limit between a hybrid reaction layer and an increased reaction layer; after the reaction in the increased reaction layer, the flocculants being added or not added to the discharge water, and the discharge water being released in an adsorption filtration layer in UPCB; post-treatment includes defibration and oxygen delignification; where the waste water mixed with flocculants enters the bottom of the UPCB reactor along the tangent, with an upward declination angle of 15 to 45 °; the hydraulic retention time is controlled within 4 to 10 hours.
[0002]
2. Method according to claim 1, characterized by the fact that the by-product of the agricultural planting, greenhouse and garden planting and / or organic waste is placed in the circulation of step (4), and mixed with the contaminated condensate ( Q), and the second fertilizer is obtained by the fermentation method, and is returned to agricultural planting, greenhouse planting and garden to form the circulation.
[0003]
Method according to claim 1, characterized in that the paper pulp for making paper products is an unbleached pulp.
[0004]
Method according to claim 1, characterized in that the contaminated condensate includes a first contaminated condensate with a concentration of NH4 + -N being greater than 0 and less than 1,000 mg / L and / or the second contaminated condensate with a concentration of NH4 + -N being from 4,000 mg / L to 5,000 mg / L; and the temperature of the contaminated condensate is 25 to 70 ° C.
[0005]
5. Method according to claim 1, characterized by the fact that the fermentation for the production of the first fertilizer includes the following steps: the contaminated condensate or ammonium sulphite obtained by the absorption of flue gas being mixed with the culture by-product or organic residue, the ratio of the percentage of mass of carbon to the percentage of mass of nitrogen in the mixture being adjusted to 15 to 30: 1 to obtain a mixture before fermentation; the pH value of the mixture before fermentation is 9.5 to 10; the mixture before fermentation in Step 1) spontaneously fermenting to obtain a fermented mixture; the fermentation being completed and the second fertilizer being obtained, when the percentage mass percentage of carbon to the mass percentage of nitrogen in the fermented mixture in Step 2) is within the range of 15 ~ 30: 1, and the pH is within the range of 6.5 to 8.5 ,.
[0006]
6. Method according to claim 1, characterized by the fact that the gas desulfurization means that the flue gas is subjected to the dust removal treatment, and then released in a desulfurization tower, and the contaminated condensate is introduced through of the pipeline to absorb SO2 in the flue gas in order to obtain (NH ^ SOa for digestion in the ammonium sulfite method; the process includes the following steps: desulfurization being carried out for the flue gas through the contaminated condensate, the gas of combustion being from industrial coal, a Venturi pipe being equipped in front of the desulfurization tower for desulfurization, and the Venturi pipe being equipped with a sprinkler and connected to the bottom of the desulfurization tower; the flue gas subjected to the dust removal treatment that enters the Venturi tube, where it is mixed with a mixed liquid substance of contaminated condensate and water with ammonia through the sprinkler in the Venturi tube, then the mixed liquid substance and the flue gas that enter the desulfurization tower once again for desulfurization; the mixture of ammonium sulphite solution after desulphurization being used in pulping by the ammonium sulphite method in papermaking, and the ammonium sulphite solution having a concentration of 10% to 35% and a purity of 80% to 99 %.
[0007]
7. Method according to claim 1, characterized by the fact that the paper pulp is an unbleached pulp that has a fracture length of 4.0 to 7.5 km, a folding number of 30 to 120 times, a tear resistance of 230 to 280 mN, and a whiteness of 35 to 65% ISO.
[0008]
8. Method according to claim 1, characterized by the fact that the discharge water and the flocculants are mixed by the pump and the lifting tube before the discharge water enters the UPCB hybrid reaction layer; a coagulation aid is added to the discharge water and the amount of coagulation aid is 0.2 to 5 ppm of the total weight of the discharge water, filtration is micro-filtration, with the number of meshes being 80 to 120.
[0009]
9. Method according to claim 1, characterized by the fact that in flocculation sedimentation, in the first place 10 to 30% of the flocculants by weight are added to the recycled water to initiate the flocculation sedimentation in the recycled water; the dosing point GT is controlled in the range of 106 to 10a, and the time for the hybrid reaction is 2 to 8 minutes; then a flake that is subjected to the salt removal treatment and again textured is added to continue the flocculation sedimentation; the GT is controlled in the range of 105 to 106, and the time for the hybrid reaction is 5 to 15 minutes.
[0010]
10. Method according to claim 9, characterized by the fact that clotting aids are added to the water after flocculation sedimentation, and the amount of the clotting aids is 1 to 6 ppm of the weight of the recycled water to be processed .

类似技术:

---

公开号 | 公开日 | 专利标题

---

BR112012023453B1|2020-07-14|METHOD OF CYCLIC USE OF STRAW IN THE PULPATION AND PAPER MANUFACTURING PROCESS

---

CN107473549A|2017-12-15|A kind of agricultural wastes cyclic utilization system

---

WO2015004146A1|2015-01-15|Method and plant for treatment of organic waste

---

KR101626752B1|2016-06-02|Recycling System for anaerobic digestive fluid

---

CN102249498B|2012-09-05|Biochemical treatment method for waste water from small and medium-sized starch factories

---

CN101450955B|2013-04-24|Method for producing yellow humic acid from grass type stalk

---

CN101659572B|2012-02-29|Method for producing fertilizer by utilizing mud and plant straws

---

Hien et al.1999|Closed wastewater system in the tapioca industry in Vietnam

---

CN104594090B|2018-10-12|Anhydrous puffing pulping process

---

BRPI0915815B1|2020-09-08|PROCESS FOR THE PRODUCTION OF METHANE FROM PROCESS WATERS AND BIOGENIC MATERIAL

---

CN102230285A|2011-11-02|Pulping system and pulping method for environment-friendly mechanical pulp and chemical mechanical pulp of non-woody crops

---

AU607028B2|1991-02-21|A method for purifying resin-containing waste liquor in the manufacture of cellulose pulps

---

CN101451324B|2013-03-27|Pulp and black liquor prepared by grass type raw material, preparation method and use thereof

---

CN103523945A|2014-01-22|Clean production method of plant fiber product

---

CN106631564A|2017-05-10|Method for producing potassium fulvate organic fertilizer by biological enzyme pretreatment and potassium hydroxide alkaline process wheat straw pulping black liquid extraction

---

CN110670396B|2021-02-02|Production process for preparing fulvic acid and biological fiber from straw raw material

---

JP6363596B2|2018-07-25|Chemical pulp manufacturing method

---

CN107119479B|2020-07-10|Low-salt-dissolving clean paper pulp and preparation method thereof

---

CN105502794B|2018-06-26|A kind of pH adjusting methods of anaerobic fermented liquid

---

CN109423902A|2019-03-05|A kind of organic fertilizer and preparation method thereof that the black liquid generated using soda pulping process technique is prepared

---

CN1408942A|2003-04-09|Pulping technology for paper-making by biological dry steaming without black liquor and pollution

---

CN106495835A|2017-03-15|A kind of preparation method of Organic sludge manure

---

CN104230127B|2016-03-23|The technique of biogas is prepared in reforged tobacco wastewater process

---

CN102817264B|2015-05-13|Method for manufacturing paper pulp by using fresh cow dung

---

CN106631392A|2017-05-10|Method of using black liquid extracted during pulping of corn straw through bioenzyme pretreatment and potassium hydroxide alkaline process to produce potassium fulvate organic fertilizer

同族专利:

---

公开号 | 公开日

---

CA2792315A1|2011-09-22|

---

CN101768887A|2010-07-07|

---

US8778135B2|2014-07-15|

---

CN101768887B|2012-12-26|

---

CA2792315C|2015-04-21|

---

US20120325421A1|2012-12-27|

---

BR112012023453A2|2016-05-24|

---

WO2011113329A1|2011-09-22|

引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

US3984225A|1974-08-19|1976-10-05|International Telephone And Telegraph Corporation|Soil conditioners and fertilizers from spent sulfite liquor|

---

CA1095663A|1975-02-12|1981-02-17|John Gordy|Pulping process|

---

US5059406A|1990-04-17|1991-10-22|University Of Tennessee Research Corporation|Desulfurization process|

---

CA2238292A1|1997-05-21|1998-11-21|S & S Lime, Inc.|Method of obtaining and using particulate calcium carbonate|

---

CN1231275A|1998-04-05|1999-10-13|朱大恒|Method for producing biological organic fertilizer by utilizing tobacco stalk|

---

CN1104379C|1998-04-17|2003-04-02|赵德志|Complex treatment process for waste water of paper making ammonium salt process|

---

SE9802442D0|1998-07-07|1998-07-07|Papsea Ab|purification device|

---

SE514742C2|1998-11-26|2001-04-09|Excelentec Holding Ab|Ways to purify sulphide-containing condensates|

---

US6454944B1|2000-11-08|2002-09-24|Larry J. Raven|Process and apparatus for conversion of biodegradable organic materials into product gas|

---

CN1248771C|2001-06-22|2006-04-05|国家电站燃烧工程技术研究中心|Reaction process for desulfurizing fume with integrated dual-circulation fluidized bed|

---

CN100500991C|2001-11-13|2009-06-17|徐守才|Process for reclaiming and comprehensively utilizing waste digestion liquid of alkaline straw pulp generated by sodium sulfite method|

---

WO2003043939A2|2001-11-16|2003-05-30|Ch2M Hill, Inc.|Method and apparatus for the treatment of particulate biodegradable organic waste|

---

CN1374424A|2002-04-19|2002-10-16|朱树文|Comprehensive papermaking effluent treating process|

---

CN1616759A|2004-09-07|2005-05-18|武绍亮|Ecological balance pulping method without pollution|

---

CN1915912A|2005-08-19|2007-02-21|北京中航宏源环境工程技术有限公司|Method for producing marketable products of organic fertilizer from pulping waste liquid in paper making through imine process|

---

CN100418932C|2006-06-07|2008-09-17|张朋端|Technology of making organic fertilizer using papermaking waste liquid and agricultural straw|

---

US7635404B1|2006-12-05|2009-12-22|Kadant Grantek Inc.|Fertilizer combination products including fertilizer granules and cellulosic granules carrying pesticides and other active ingredients|

---

WO2009015556A1|2007-07-27|2009-02-05|Shandong Tralin Paper Co., Ltd|Process for producing paper-making pulps from grasses and pulps obtained by the process|

---

WO2009015555A1|2007-07-27|2009-02-05|Shandong Tralin Paper Co., Ltd|Grass paper pulp used by papermaking and preparation method thereof|

---

WO2009056017A1|2007-10-29|2009-05-07|Shandong Tralin Paper Co., Ltd|A process for comprehensive utilization of stalks of grass-type plants|

---

KR101410110B1|2007-12-05|2014-06-25|산동 후인 페이퍼 앤드 인바이런멘탈 프로텍션 테크놀로지 컴패니, 리미티드|Grass type unbleached paper products and production method thereof|

---

CN101451315B|2007-12-05|2011-12-28|山东福荫造纸环保科技有限公司|Method for comprehensive utilization of grass type stalk|

---

US8414808B2|2008-10-03|2013-04-09|DVO. Inc.|Composite components from anaerobic digested fibrous materials|

---

CN101759451B|2008-10-17|2013-10-23|山东泉林纸业有限责任公司|Organic fertilizer and preparation method thereof|

---

CN101759450B|2008-10-17|2013-12-04|山东福荫造纸环保科技有限公司|Circle application of waste condensate water during pulping with ammonium sulfite method|

---

CN101759449B|2008-10-17|2013-10-23|山东泉林纸业有限责任公司|Seedling medium and preparation method thereof|

---

CN101760975B|2008-10-17|2012-08-08|山东福荫造纸环保科技有限公司|Circulation process for performing ammonium sulfite pulping by using sulfur-containing flue gas absorber|

---

CA2749168C|2008-12-09|2017-09-12|Shandong Fuyin Paper & Environmental Protection Technology Co., Ltd|A base paper, the preparation method and use thereof|

---

CN101781057B|2009-01-16|2012-01-04|山东福荫造纸环保科技有限公司|Treatment method of waste papermaking water|

---

CN101781031B|2009-01-16|2012-02-08|山东福荫造纸环保科技有限公司|Purification treatment method of reclaimed papermaking water|

---

US20110042307A1|2009-04-23|2011-02-24|Ghd, Inc.|Methods and apparatuses to reduce hydrogen sulfide in a biogas|

---

US8449773B2|2009-07-06|2013-05-28|Brigham Young University|Method for pretreatment of cellulosic and lignocellulosic materials for conversion into bioenergy|

---

CN101768887B|2010-03-17|2012-12-26|山东和润浆纸有限公司|Circular utilization method of straw in pulping and papermaking processes|

---

US20130157334A1|2011-12-19|2013-06-20|Shell Oil Company|Process for converting a lignocellulosic biomass|CA2749168C|2008-12-09|2017-09-12|Shandong Fuyin Paper & Environmental Protection Technology Co., Ltd|A base paper, the preparation method and use thereof|

---

CN101768887B|2010-03-17|2012-12-26|山东和润浆纸有限公司|Circular utilization method of straw in pulping and papermaking processes|

---

CN102174763B|2010-12-30|2013-01-02|维达纸业有限公司|Treatment method for paper making waste water|

---

CN102677530B|2012-05-13|2015-02-25|王性仁|Low-carbon papermaking method|

---

US9133068B2|2012-11-26|2015-09-15|Neo Energy, Llc|System and method for producing fertilizer from organic waste|

---

GB201304872D0|2013-03-15|2013-05-01|Imp Innovations Ltd|Treatment|

---

US11118308B2|2013-03-15|2021-09-14|Ip2Ipo Innovations Limited|Treatment of lignocellulosic biomass with ionic liquid|

---

CN103641278A|2013-12-19|2014-03-19|北京北方节能环保有限公司|System and method for treating purified cotton production wastewater by adopting anoxic processes|

---

CN104012387A|2014-01-21|2014-09-03|无锡思清源生物科技有限公司|Organic composite substrate for oilseed rape tray-soilless seedling and preparation method thereof|

---

CN104805724B|2014-01-29|2017-02-01|山东贝特尔环保科技有限公司|Pulping black liquor treatment method|

---

CN103966879A|2014-05-20|2014-08-06|袁志平|Biomass power generating, pulping and foliage fertilizer preparing combined production method|

---

GB2530987B|2014-10-03|2017-06-21|Nafici Env ResLtd|A method for processing straw|

---

EP3029010B1|2014-12-01|2017-03-08|S2P AG Straw - Pulp & Paper|Method for producing a fertilizer from black liquours|

---

US10351481B2|2015-03-10|2019-07-16|Compass Minerals Manitoba Inc.|Potassium-based starter fertilizer|

---

CN104928962A|2015-04-27|2015-09-23|宁夏紫荆花纸业有限公司|Method for pulping corn stalk as a raw material and making natural-color household paper|

---

US20160346788A1|2015-05-29|2016-12-01|Anaergia Inc.|Organics recovery from dry fraction|

---

GB201520453D0|2015-11-20|2016-01-06|Imp Innovations Ltd|Process|

---

CN105367264A|2015-12-02|2016-03-02|宁夏紫荆花纸业有限公司|Method for producing organic fertilizer by using waste straw crumbs left after preparation and screening of crop straws for pulping|

---

CN105801210B|2016-03-09|2016-12-28|南京农业大学|A kind of method utilizing the direct composting of straw and the Straw manures of preparation|

---

CN105625076A|2016-03-25|2016-06-01|安徽格义循环经济产业园有限公司|Environment-friendly unbleached paper|

---

CN105780583B|2016-03-25|2018-04-06|安徽格义循环经济产业园有限公司|Non-timber class paper pulp|

---

CN105803848A|2016-03-25|2016-07-27|安徽格义循环经济产业园有限公司|Pulping method|

---

CN105780566A|2016-03-25|2016-07-20|安徽格义循环经济产业园有限公司|Method for manufacturing unbleached paper|

---

CN106186294B|2016-08-25|2019-09-03|江南大学|A kind of processing recovery method of cop tube paper production waste pulp|

---

CN106221849A|2016-10-14|2016-12-14|安徽格义循环经济产业园有限公司|Stalk fuel containing biomass sludge and preparation method thereof|

---

CN106702798A|2017-03-23|2017-05-24|东北林业大学|Method of utilizing waste liquid and waste residue of corn pulping to prepare fertilizer|

---

CN107089746B|2017-05-17|2020-07-28|四川凤生纸业科技股份有限公司|Recycling method of natural color bamboo pulp pulping washing wastewater|

---

CN109423909A|2017-08-30|2019-03-05|黑龙江如柏科技有限公司|It is a kind of using grass class plant as the process integration of raw material|

---

CN109423915A|2017-08-30|2019-03-05|黑龙江如柏科技有限公司|It is a kind of using grass class plant as the process integration of raw material|

---

CN107938417A|2017-11-29|2018-04-20|何永庆|The method that organic fertilizer is prepared using pulping waste liquor|

---

CN108316029A|2018-02-27|2018-07-24|徐州工程学院|A kind of High-efficiency straw utilizes method and system|

---

CN108409435B|2018-04-27|2021-11-12|福建龙马环卫装备股份有限公司|Sludge aerobic composting method|

---

CN108611912B|2018-05-03|2020-10-27|大禾环保科技有限公司|Process for producing fulvic acid fertilizer and high-strength corrugated paper by using all-cotton straws as raw materials|

---

CN109024033B|2018-08-02|2020-11-24|青岛科技大学|Pulping method using high-concentration brine as cooking medium|

---

CN109487612B|2018-12-18|2021-06-22|王海申|Treatment system and method for cleaning pulping pollutants|

---

CN110244028A|2019-05-23|2019-09-17|岳阳林纸股份有限公司|A kind of method of quick detection beating degree|

---

SE543640C2|2019-09-04|2021-05-11|Stora Enso Oyj|Fluff pulp from oxygen delignified pulp|

---

CN110670396B|2019-10-15|2021-02-02|史晓菲|Production process for preparing fulvic acid and biological fiber from straw raw material|

---

CN111472185A|2020-04-08|2020-07-31|石河子市国力源环保制浆有限公司|Recycling method in straw pulping and papermaking process|

---

CN111470693A|2020-04-08|2020-07-31|石河子市国力源环保制浆有限公司|Process and equipment for producing organic compound fertilizer by using straw papermaking chain|

---

CN111549077A|2020-05-09|2020-08-18|山东省科学院能源研究所|Method for producing organic acid and converting methane by regulating and controlling degradation of silage straws by using black liquor|

---

CN112169540A|2020-09-21|2021-01-05|张家港市杨舍丝印工艺厂|Comprehensive treatment system for waste|

---

CN112726266A|2020-12-24|2021-04-30|东北农业大学|Method for treating straw and paper pulp obtained by method|

法律状态:
2018-04-10| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

---

2019-10-08| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|

---

2020-03-10| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

---

2020-03-17| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

---

2020-03-24| B09Y| Publication of grant cancelled [chapter 9.1.2 patent gazette]|Free format text: ANULADA A PUBLICACAO CODIGO 9.1 NA RPI NO 2567 DE 17/03/2020 POR TER SIDO INDEVIDA. |

---

2020-07-14| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 11/03/2011, OBSERVADAS AS CONDICOES LEGAIS. |

优先权:

---

申请号 | 申请日 | 专利标题

---

CN2010101261890A|CN101768887B|2010-03-17|2010-03-17|Circular utilization method of straw in pulping and papermaking processes|

---

CN201010126189.0|2010-03-17|

---

PCT/CN2011/071724|WO2011113329A1|2010-03-17|2011-03-11|Circular utilization method of straw in pulping and papermaking process|

---