• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Ash-containing solids are separated from coal liquid by adding a blend comprising alcohol and a light oil fraction to said coal liquid, followed by a solids-liquid separation step.
    公开号:SU745369A3
    申请号:SU782592351
    申请日:1978-03-13
    公开日:1980-06-30
    发明作者:Л.Карр Норман；Л.Макджиннис Эдгар
    申请人:Галф Рисерч Энд Дивелопмент Компани (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to methods for purifying coal liquefaction products and can be used in coal chemical industry. Methods are known for purifying coal liquefaction products obtained as a result of contacting a mixture of coal and solvent containing hydroaromatic components with hydrogen from solid particles 1. The method for cleaning coal liquefaction products from solid particles is the closest to the invention by mechanically separating the latter from the raw material to obtain a concentrate of solid particles. 2. Solids TI1 # 1 are particles of ash or ash and undissolved hydrocarbons. Due to the small particle size (less than a micron), it is extremely difficult to separate them from the products of liquefaction coal, respectively, the cleaning speed of the products is low. The aim of the invention is to increase the cleaning rate due to the agglomeration of solid particles. This goal is achieved by the method of purifying coal liquefaction products from solid particles by mechanically separating the latter to obtain a concentrate of solid particles, in which 1-50% by weight of the aliphatic alcohol mixture of the liquid hydrocarbon fraction is added to the raw material before separating the solid particles. boiling at temperature above when the content of: alcohol in a mixture of 1-75%. Preferably, isopropyl alcohol, primary, secondary, tertiary butyl alcohol is used as aliphatic alcohol, kerosene, fractions, and coal purification products boiling at a temperature not higher are used as hydrocarbon fractions. Distinctive features of the method consist in adding a feedstock of 1-50% by weight of a mixture of aliphatic alcohol C2-C / 40 and a hydrocarbon fraction boiling not higher, as well as in preferred conditions of the process. Adding only alcohol to carbon liquefaction products leads to the agglomeration of solid particles. The temperature of the products to be purified should be in the range of 38371 ° C, i mainly 66-31b C, preferably 204-288 ° C. After making alcohol, the products must be intermixed to obtain a homogeneous composition: in the liquid phase. After the addition of alcohol and prior to the commencement of the stage, the products to be purified can remain at a mixing temperature of 30 seconds to. 3 hours, generally from 1 minute to 1 hour, preferably from 2-5 to 30 meters. However, the sintering process is more efficient when using a mixture of aliphatic alcohol and hydrocarbon fraction. Phenol, which has 6 hydrocarbon fractions (for example, coal liquids), has a detrimental effect on the process of separating solid particles, obviously, playing the role of a dispersion medium. In order to avoid the return of phenol, the carbon-hydrogen fraction should be heated to a temperature below the boiling point of the phenol, which equals. For example, the coal liquid fraction used as the lehydrogen fraction can be heated to a temperature not higher. The boiling range of the coal liquid fraction does not necessarily have to overlap the boiling range of the recycled solvent. The upper temperature limit is not reached if the hydrocarbon fraction used is not coal liquid and therefore does not contain phenols. For example, if the hydrocarbon fraction is a petroleum light, medium or heavy oil, then it can be heated no higher than before. The amount of alcohol mixed with the hydrocarbon fraction is 1-75% by weight, preferably 10-35% by weight. The amount of the added mixture is 1-50% by weight, most preferably 2-5% by weight. The process according to the invention may be carried out, for example, as follows. Alcohol is added to the heated, unfiltered suspension of the coal solution. The mixture is stirred and aged. Then it is passed through a filter on which a layer of filter material from diatomaceous earth was applied. After that, the alcohol-containing filtrate is fractionated to extract a low boiling fraction containing at least a portion of the alcohol. Then this fraction is reused in a mixture with the feedstock passing through the FIL1Tr. Some of the fresh alcohol may be added. To illustrate the invention, experiments were conducted on cleaning the sludge products of YasNYI coal; from solids by filtration. The data obtained are presented according to the mathematical model of the filter, walkie-talkie g W-KW-vC / where T is the filtration time, min; W is the weight of the filtrate collected during time T; K — parameter of filter sediment resistance, min / gram; С - resistance parameter of the filter material layer, min / gram, - filtration capacity or speed, g / min In the filtration experiments presented below, the amount of filtrate extracted W is automatically fixed as a function of time T. In filtration experiments in the following examples, A screen with an EO hole is used, which is located in the filter element and has a filter cover of 1.27 cm of diatomaceous earth. The filter element has openings with an inner diameter of 1.9 cm and a depth of 3.5 cm, the opening area is 2.84 cm. To prevent distortion, the screen rests on a solid grid. The filter coating is applied to the screen by packing a suspension consisting of 5% by weight of decalitic material of the filter coating and the hydrocarbon fraction used in the process with a nitrogen pressure of 2.8 kg / cm. The process of applying the filter coating is carried out at a temperature close to that of the subsequent filtration process. The resulting porous layer of filter material has a weight of about 1.2 g. After the deposition of the filter material, the sieve is blown with nitrogen at a pressure of 0.35 kg / cm for 1-2 seconds to remove traces of hydrocarbon fraction. 750 g of unfiltered oil (a liquefied carbon product) is introduced into the autoclave and maintained at 38-54 ° C with continuous stirring. The mixing was carried out with 1 bt using two five centimeter turbines. The number of revs is 2000 rpm. The filtration process begins after the supply of nitrogen to the autoclave under a pressure of 2.8-5.6 kg / cm. Non-filter oil is then withdrawn from the autoclave, passed through a heater, and passed to the filter. The effluent filtrate is weighed and the weight is automatically fixed at every 5s. To determine the effect of additives and the filtration process, comparative experiments are carried out in which the same filtered oil is used as a raw material. The latter has a declining characteristic; Specific gravity (15,) 1.15 Kinematic viscosity at 1 cSt Density at 15.6 ° С1.092 Ash content, wt.% 4.49 Insoluble pyridines, wt.% 6.34 Distillation data: Boiling point ,% at 1 atm, C Removed all. distillates at a power of 26 phi used. The hydrocarbon fraction used has the following characteristic. Specific gravity at 15, bos 0.880 Density at 15, 829 Kinematic viscosity at 37 ,, cSt0.8681 Distillation data; Boil-off,% Temperature, C 5 72. 95 End of boiling Example 1. To illustrate and not add various alcohols to the filtration process of the product being cleaned, a series of filter tests was carried out. The experiments were carried out at a temperature of 0 ° C and at a pressure drop of 2.8 kg / cm per liter. The results of these experiments are given in Table. 1. Table 1
    from consideration of the above results, it follows that the filter resistance parameter K is the best indicator of the effect of the additive on the filtering process, since this parameter contains all the effects in the filtering process related to the filter system and the filter coating. On the other hand, the value C characterizes filter system and filter coating, regardless of the effect of alcohol or phenol additives. The above results show that the filtration resistance parameter decreases with the use of alcohols by different values. Thus, with the use of secondary butyl alcohol, the greatest decrease in the resistance parameter is observed. In contrast, phenol increases the resistance parameter. This indicates that it is more a dispersion medium than an agglomerating one. Therefore, the presence of phenol has an adverse effect on the filtration process of coal liquefaction products. Example 2 To illustrate the use of methyl and ethyl alcohols as additives to the carbon liquefying products, the experiments were carried out at a filter pressure drop of 5.6 kg / cm. The results of the experiments are presented in table. 2
    The ID of these results follows. Example 3. It was tested that the use of methyl alcohol to determine the effect of organic and reduces the parameter of acid, aldehydes and ketones in filtration K, while the process of filtration of liquefied products using ethyl alcohol is more coal The results of these experiments are more efficiently set. 3
    Filtration at 210 ° C and pressure drop 5.6 kg / cm None0,02350,154,1
    Methyl ethyl ketone .0.02560,173.9
    From the above results, it follows that butyric aldehyde, methyl ethyl ketone and acetic acid have little effect on the resistance parameter K. Acetone has a somewhat unfavorable effect. The use of acids in industrial processes is undesirable because they are. Q is corrosive.
    TaejtHua 2
    Table 3
    Example 4 Experiments were carried out to determine the effect of the amount of isopropanol additive on the filtration process of coal liquefaction products. The experiments were carried out at a temperature of 260 ° C and at a pressure drop of 2.8 kg / cm. The results of these experiments are presented in Table. four.
    These results show a significant decrease in the resistance parameter K with a gradual increase in the amount of isopropanol from 0 to 2%. However, when using 2.7%, the effect is lower than when using 2%. This indicates that exceeding the critical alcohol content level reduces the resulting positive effect.
    These results show that the dwell time between the introduction of secondary butyl alcohol into the feedstock and the beginning of 1}) filtration has an effect on the filtration resistance parameter K. In an interval of 8 minutes with the addition of 2% secondary butyl alcohol, the effect of the additive reaches its maximum, then decreases. The effect of the additive is greater at 40 minutes of exposure than at 1 or 80 minutes.
    Table 4
    Example 5. Experiments in which butyl alcohol is used as an additive are expanded to illustrate the effect of the holding time of the raw material being filtered, in which the additive is contained, before filtering begins. Exposure is carried out at a temperature of 49 ° C. The results of these experiments are presented in Table. 5. Filtration was carried out at 260 ° C and at a pressure drop of 5.6 kg / cm for 2 minutes.
    Table 5
    Example 6 i Experiments were performed to illustrate the use of a mixture consisting of a hydrocarbon fraction, which uses a light fraction of process oil with a boiling point below and isopropanol for a filtration resistance parameter K. Experiments are carried out at a temperature of 260 ° C and a pressure differential 2 , 8 kg / cm2. The results of these experiments are presented in table. 6
    A comparison of these results with the results of experiment 4 shows that the effective effect on the resistance during filtration is observed when using a mixture of light oil and isopropane. From example 4 it follows that the positive effect is reduced if the amount of isopropanol is increased from 2 to 2.7%. However, the data from the last example shows that when using isopropanol in the amount of 5.6%, the resistance to filtration decreases compared to using 2% isopropanol if isopropanol is combined with light process oil. In addition, the positive effect of the use of 2% isopropanol increases, eu and
    to grease him. with a light oil. PreimK, min / g
    Additive (concentration 2 wt.%)
    Isopropanol Isopropanol Isopropanol Is missing Isopropanol
    Table 6
    The substance of using a mixture of light oil and isopropanol, presented in this example, can be accomplished by applying a recirculation filter & that light oil obtained from distillation, the boiling range of which covers the boiling point of the alcohol additive. This avoids the cost of separating all or part of the isopropanol from the oil filtrate, which contains iso-propanol.
    Example 7: Experiments illustrate the effect of a holding time between the supply of isopropanol to the product to be purified and the start of filtration. The experiments were carried out at 260 ° C and at a pressure drop of 5.6 kg / cm. The results of these experiments are presented in Table. 7. Table 7
    The exposure time at 260C between the flow of the additive and the start of filtration, min
    3 6 9
    35
    The above results show that there is an improvement in the resistance parameter when filtering K, resulting from an increase in the dwell time between the feed of isopropanol and the start of filtration.
    Example 8. To further determine the effect of time between the supply of isopropanol in the 4th product and the start of the filtration process, four experiments were carried out. The results of the experiments are shown in the graph. In one of the experiments no isopropanol was added (curve 1). In three experiments, the purified product contains isopropanol in the amount of 2.% by weight. The exposure time is, respectively, two, four and six minutes. In all experiments, the temperature was 260 ° C. The pressure drop was 5.6 kg / cm (curves 2, 3, 4, respectively),
    The dependence of w on T will be obtained according to the given mathematical model.
    In the drawing, W values are plotted on the horizontal axis, T / W values are plotted on the vertical axis. The coefficient K characterizes the slope of each curve, and each curve with a vertical axis gives a coefficient C (Cyi-C).
    From the analysis of each curve, it follows that parameter C depends on the characteristics of the layer of filter material, and how it is related to the filtration rate at the beginning of the experiment, before a significant amount of the filtered sediment is deposited on the layer of filter material. On the other hand, the angle of inclination K is a parameter characterizing the filter cake, which is deposited on the layer of filter material during the filtration process, and therefore it characterizes the filtration process itself, excluding the material covered by the filter material. A relatively small angle of inclination (a low value of K) indicates a substantially low resistance of the precipitate during filtration. A decrease in the K coefficient leads to an increase in the filtration rate. From the analysis of the figure, it follows that the upper curve has the largest angle of inclination (the largest value of the coefficient K). The bottom curve has the smallest angle (the lowest K value).
    As can be seen from the figure, the use of isopropanol t. In all cases leads to a decrease in resistance. However, a gradual increase in the exposure time between the supply of isopropanol and the start of the filtration process leads to a gradual decrease in resistance.
    The points on the curves denote the time since the beginning of the Filtration process (0.25; 0.5; 0.75; 1.0; 1.5; 2, O min).
    From the graph it follows that after 1 min from the start of filtration, during the first experiment (upper curve), a smaller amount is obtained.
    filtrate, than when carrying out the fourth experiment (lower curve). Although it is clear from each curve that the filtration rate at the end of the experiment is lower compared to the beginning of the experiment, the angle of inclination of the lower curve indicates that the filtration rate in this case decreases slightly in the course of the experiment.
    Each filtration experiment is carried out.
    without washing the dilution of the filter cake.
    Since prolavka solvent causes changes in the composition of the filter sludge, it also affects
    The value of k. Many industrial filters are of a continuous rotating type, in which filtration cycles last no more than 1 minute, they alternate continuously with washing cycles, in which the washing solvent is sprayed through the filter cake to flush the absorbed coal liquid. Therefore, all the filtration rates obtained in the experiments relate to the operation of the filter during the first minute of the filtering process.
    权利要求:
    Claims (3)
    [1]
    1. The method of purification of coal liquefaction products from solid particles by mechanically separating the latter
    from the raw material to obtain a concentrate of solid particles, about tl and the fact that, in order to increase the purification rate, 1-50 wt.% of the mixture of aliphatic alcohol of the liquid hydrocarbon fraction boiling is added to the raw material before separating the solid particles. at a temperature not higher than 260s, when the alcohol content in the mixture is 1-75 wt.%.
    [2]
    2. Method POP.1, characterized in that isopropyl alcohol, primary, secondary, tertiary butyl alcohol is used as aliphatic alcohol,
    [3]
    3. The method according to claim 1, characterized in that kerosene fractions, coal purification products boiling at a temperature not higher than 170 ° C are used as the hydrocarbon fraction.
    Information sources,
    taken into account in the examination
    1. US patent 3849287, class, 208-8, published. 1974.
    2. US patent number 3892654,
    cl. 208-8, published. 1975 (prototype).
    类似技术:
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    同族专利:
    公开号 | 公开日
    US4124485A|1978-11-07|
    NL7802382A|1978-10-06|
    PL111205B1|1980-08-30|
    AU3333678A|1979-08-23|
    JPS53125401A|1978-11-01|
    DE2812865A1|1978-10-05|
    IN147502B|1980-03-22|
    GB1595033A|1981-08-05|
    FR2386598A1|1978-11-03|
    CA1098851A|1981-04-07|
    AU510346B2|1980-06-19|
    BR7801988A|1978-12-19|
    PL205784A1|1979-03-12|
    DD136395A5|1979-07-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1573307A|1921-11-16|1926-02-16|Frank L Dietz|Fuel oil|
    US1573308A|1922-02-02|1926-02-16|Frank L Dietz|Motor fuel oil|
    US1811552A|1929-07-09|1931-06-23|Standard Oil Dev Co|Stable mixture of petroleum hydrocarbons and secondary alcohols|
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    US2087582A|1933-08-22|1937-07-20|Standard Oil Dev Co|Motor fuel|
    US4029567A|1976-04-20|1977-06-14|Canadian Patents And Development Limited|Solids recovery from coal liquefaction slurry|US4298450A|1977-12-05|1981-11-03|The United States Of America As Represented By The United States Department Of Energy|Alcohols as hydrogen-donor solvents for treatment of coal|
    US4252648A|1979-05-07|1981-02-24|Gulf Research & Development Company|Filtration of a coal liquid slurry using an alkylmethacrylate copolymer|
    US4255258A|1979-05-07|1981-03-10|Gulf Research & Development Company|Filtration of a coal liquid slurry using an alkylmethacrylate copolymer and an alcohol|
    US4260485A|1979-05-07|1981-04-07|Gulf Research & Development Company|Filtration of a coal liquid slurry using polyisobutylene and an alcohol|
    US4252647A|1979-05-07|1981-02-24|Gulf Research & Development Company|Filtration of a coal liquid slurry using an ethylene vinyl acetate copolymer|
    US4251364A|1979-05-07|1981-02-17|Gulf Research & Development Company|Filtration of a coal liquid slurry using polyisobutylene|
    US4252646A|1979-05-07|1981-02-24|Gulf Research & Development Company|Filtration of a coal liquid slurry using an ethylene vinyl acetate copolymer and an alcohol|
    US4420930A|1979-06-07|1983-12-20|Gulf Research & Development Company|Process for operating a furnace or a combustion engine|
    US4278443A|1979-06-07|1981-07-14|Gulf Research & Development Company|Energy generating process and novel fuel therefor|
    US4264453A|1980-01-10|1981-04-28|Pori International, Inc.|Reclamation of coking wastes|
    US4298452A|1980-03-28|1981-11-03|Texaco Inc.|Coal liquefaction|
    US4544477A|1983-10-12|1985-10-01|Standard Oil Company|Polar solvent extraction and dedusting process|
    US4627913A|1985-01-09|1986-12-09|Air Products And Chemicals, Inc.|Catalytic coal liquefaction with treated solvent and SRC recycle|
    US4617105A|1985-09-26|1986-10-14|Air Products And Chemicals, Inc.|Coal liquefaction process using pretreatment with a binary solvent mixture|
    US4770766A|1986-03-12|1988-09-13|Otisca Industries, Ltd.|Time-controlled processes for agglomerating coal|
    JP5426832B2|2008-03-19|2014-02-26|株式会社神戸製鋼所|Production method of ashless coal|
    US9834730B2|2014-01-23|2017-12-05|Ecolab Usa Inc.|Use of emulsion polymers to flocculate solids in organic liquids|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/784,049|US4124485A|1977-04-04|1977-04-04|Separation of solids from coal liquids with an additive blend|
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