• 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:
    Summary The invention relates to a method of increasing the total yield of methane in the biological production of lignocellulosic material, wherein methane gas containing carbon dioxide is produced by a fermentation process. The process comprises separating the lignocellulosic material into a cellulose product having a lignin content of less than 10% by weight, which is then fermented, and a residual product containing lignin, that the fermentation process for methane production is supplemented by a thermochemical synthesis process in which the residue is used for preparation. methane gas, which contains carbon dioxide, that the methane gas from the fermentation process and the synthesis process are combined to separate carbon dioxide from methane, and that the energy needs of the fermentation process are met exclusively by energy from the synthesis process.
    公开号:SE1200203A1
    申请号:SE1200203
    申请日:2012-04-02
    公开日:2013-10-03
    发明作者:Anders Oestman；Nils Lindman
    申请人:Skandinavisk Kemiinformation Ab；
    IPC主号:
    专利说明:

    Set to htija total yield of methane from lignocellulosic material Technically omeade.
    The present invention relates to a method of increasing the total yield of methane in the biological production of lignocellulosic material, whereby methane gas containing carbon dioxide is produced by a fermentation process. Carbon dioxide-purified methane can be used to replace fossil natural gas, e.g. as an industry for internal combustion engines.
    The state of the art.
    Biogas, ie mainly methane, has attracted increasing attention as a fuel in vehicles during the 2000s. The gas is formed naturally during the decomposition of organic material. Since it is partly considered to have a climate impact in the unburned state, and partly can easily be used as fuel in (separate) engines, it has several advantages as a fuel. Politically, it has been strongly advocated as an alternative and renewable industry in the so-called second generation biofuels.
    Biogas has long been produced in various contexts; especially in connection with the treatment of wastewater. For several decades, the sludge from municipal wastewater treatment in Sweden has been rooted to reduce the waste problem. In special root chambers, a natural, anaerobic decomposition of the sludge has been carried out and the gas produced has been used on site for internal energy generation - or fuel without energy recovery. Today, the surplus of this gas constitutes a large part of the biogas sold as fuel.
    The technique of breaking down water-borne pollutants anaerobically has also been used for several decades in special water treatment; for example in the food industry's sewers. At high loads of organic material, anaerobic decomposition can sometimes be advantageous compared to aerobic decomposition, which leads to carbon dioxide and water in the stable for biogas.
    The experiences from these areas already in the 1980s led to the idea of a further production of biogas as a fuel and fuel. Extensive activities have been carried out to utilize also solid waste, for example stable goods, 16r biogas production with the underlying idea that a local production of a biofuel could 2 take place. In municipal waste dumps, technology was developed to collect the root gas that is spontaneously formed at the landfill.
    In all these cases, however, the raw material constitutes residual products from other production. Calculations of the total potential for biogas from these residual products end in a few or a few terawatt hours, compared with Swedish oil imports, which are in the order of 200 TWh.
    It has become natural to examine the preconditions for biogas production from commercially available raw materials. Above all, the eyes should be thrown on lignocellulose, ie plant material such as grass, straw, wood. In Swedish as well as international trade press there are a large number of research reports on biogas production from such On the other hand, one can hardly find any dedicated, commercial production of biogas from them.
    The reason for this should primarily be technical / financial. The energy efficiencies are relatively low because the rotatable components are only part of the raw material and the processes become expensive. The rooting of these natural plant materials simply requires a fairly extensive process. Not least, it can be stated that the rooting times for the materials are long and that diluted slurries must be used, which leads to very large root chambers. Something drastic and philosophical can be said, that these Rirhallands are fortunate for humanity. The natural resistance to degradation also allows us to use the materials for constructions and gives us the chance to store them.
    Object of the invention.
    An object of the present invention is to use lignocellulosic material for the production of methane and in particular to increase the yield of this gas during rooting. Another purpose is to use the miter rotatable material for methane production to replace fossil natural gas.
    Brief Description of the Drawing The only figure in the drawing shows a schematic composition of process steps according to the present invention. Brief Description of the Invention According to the invention, however, total yield of methane in biological production from lignocellulosic material, whereby methane gas containing carbon dioxide is produced by a fermentation process. The distinguishing feature of the method is that the lignocellulosic material is separated into a cellulose product with a lignin content of less than a percentage by weight, which is then fermented, and a residual product containing lignin, that the fermentation process for methane production is supplemented by a thermochemical synthesis process. for the production of methane gas, which contains carbon dioxide, that the methane gas from the fermentation process and the synthesis process is combined and undergoes separation of carbon dioxide from methane, and that the energy needs of the fermentation process are met by energy from the synthesis process. It is advantageous that the energy needs of the fermentation process are met exclusively by energy from the synthesis process.
    According to a preferred embodiment, the cellulose product is taken out in solid phase and washed.
    Then the washed cellulose is supplied with enzymes for at least partial hydrolysis of the cellulose. Furthermore, the at least partially hydrolyzed cellulose is fermented anaerobically to methane and carbon dioxide by microbial inoculation thereof.
    It is further advantageous that the residue from the anaerobic fermentation is wholly or partly fed to the thermochemical process for methane production. The hydrolysis and anaerobic fermentation are carried out at 40-70 ° C, preferably at 45-60 ° C. The residual product containing lignin in lost form with 50 to 70% by weight of dry matter content is fed to pressurized gasification with oxygen as oxidizing agent and the aqueous gas obtained from the gasification is used for the synthesis of methane. In addition, the residual product containing lignin is added separated extractive substances to the cellulose fermentation as promoting substances. In addition, some of the aqueous gas is transported to the anaerobic fermentation. This portion of the aqueous gas is at most 5% by volume of the total amount.
    It is already known that the constituents of the carbohydrates of lignocellulose are relatively easy to digest, i.e. to ferment anaerobically to methane and carbon dioxide. In the salvage sewage sludge from municipal water treatment as in the food industry's sewage, the original carbohydrates have been partially broken down into simple sugars and acids, etc., which can be converted relatively quickly.
    In the invention, in a first step, the lignocellulose is separated into its main constituents; cellulose, hemicellulose and lignin. The pulp industry has for a long time carried out such a separation in the pulp factories and this technology as modified such and alternative such has been demonstrated.
    The cellulose fraction then obtained still has long residence times to be converted to methane and carbon dioxide. However, by using an enzymatic hydrolysis step, the decomposition into simple sugars is started in a relatively (very) short time and the total rooting process is drastically shortened.
    Lignin cannot be fermented anaerobically to methane and carbon dioxide. On the other hand, lignin in the black liquor obtained in traditional pulp production constitutes an excellent gasification raw material. The black liquor gasification gives a rag gas which, with conventional technology, can be processed into synthetic gas for - likewise established - production of methane (and carbon dioxide).
    The hemicellulose follows to a small extent with the cellulose fraction as it is easily fermented to methane and carbon dioxide. The remaining stone, like the lignin, is gasified to - in the end - synthesis gas, for further conversion to methane.
    The residue from the decomposition to methane and carbon dioxide usually constitutes a waste problem. According to the invention, after a simple filtration, it can be transferred to, and combined with, the residual product containing lignin for further gasification and synthesis to methane.
    Through the separation and the separate treatments of the components of the lignocellulose, a substantially one hundred percent turnover of it is obtained. From all three main fractions, methane and carbon dioxide, ie biogas, are produced. The amount of by-products is small and the combination process results in a dedicated production of biogas from lignocellulose with a higher yield in a shorter time than what has been evaluated in other processes.
    The invention in relation to previously known processes and process combinations Savitt has been able to state that most of the described processes for biogas from lignocellulose contain a direct rooting of the entire lignocellulosic material. Numerous different microorganisms have been tested in the roots, but the total treatment times are mostly in the order of 100 days (and more). The methane yields are then about 300 liters per kg TS carbohydrate raw material and significantly lower per kg lignocellulose. Taken together, these processes are far from the combination process of the invention.
    The use of special cellulose hydrolyzing enzymes on lignocellulose is suggested. However, there is no precedent for any separation of the cellulose in the raw material, which is why these ideas are also far from the process combination of the invention.
    As a side process in ethanol production, the beverage is sometimes led to a biogas production where the remaining pentoses (as well as any hexoses) are anaerobically fermented to methane and carbon dioxide. The lignin can be processed into industry in various ways. Although ethanol production can in some way be said to be a separation process, it has nothing to do with the invention's combination of processes.
    The process combination of the invention with an initial separation of the lignocellulose is indicated in some proposed processes: A Swedish patent, SE 527 646 C2, states a process combination with an initial "pulp boiling" and an ethanol production from the cellulose fraction and a gasification of the black liquor (for further synthesis to methanol, DME, FT products, etc.). The process combination has similarities with the present invention and the patent states without further specification that material and energy exchanges must take place between the process parts.
    In North America, a company, Lignol, is developing processes that include an initial separation of lignin and cellulose based on solvent technology. Thus, the established pulp cooking technology does not increase and savitt has been seen, no dedicated biogas production from the lignocellulose is stated. According to what could be deduced from these processes, the solvent technology and the possibilities for a "purer" lignin are the main step awn if in one case ethanol production from the cellulose is also suggested.
    Some patents, such as US 6,172,272 B1, disclose a fuel production from the lignin fraction from pulp production (black liquor). However, they mostly refer to a form of by-product reprocessing in connection with conventional pulp production where only a part of the lignin is taken out for fuel production. The rest goes as usual to the recovery boiler. Black liquor gasification is, according to what could have been patrdffas, not included in the context.
    All in all, it can be said that the process described in the stated Swedish patent specification has the greatest resemblance to the present invention. One difference, of course, is that the method described in this male reference relates to a fermentation to ethanol while the present invention contains a rooting to biogas. In practice, however, the fundamental and procedural differences are significant, mainly due to the fact that anaerobic methane fermentation places completely different demands on what ethanol production does. The present invention is based on how the production of methane can be made more efficient in a combination of processes. 6 Alkaline separation of lignocellulose In the Swedish pulp industry, wood raw material is the established raw material for the production of cellulose. Internationally, dven straw is used as a raw material (eg in India). In Sweden, the technology with grass as ravara was demonstrated a few decades ago. It is thus verified that alkaline separation of the type used in pulp production also works on other lignocellulosic materials.
    There is also no reason to assume that the other separation techniques for cellulose and lignin from lignocellulose would not work. In the further description of the invention, however, the first alternative is a sulfur-free pulp boiling - "sulfur-free" to avoid later problems with sulfur in the final products. Such boiling is commercially available in some plants abroad and has been verified on a large scale in a project carried out with support from the Swedish Energy Agency (Norrtorp 2009).
    The raw material - of the type indicated above - is boiled in substantially conventional salt with alkali, the lignin and most of the hemicellulose being dissolved. The solution, ie the black liquor, is taken to a separation of tall oil and evaporated.
    The solid cellulose fraction is filtered and rinsed and dewatered and led to biogas production. The rinsing water is mixed with the previous black liquor and evaporated.
    With cooking times of about 4 hours and an alkalinity in the cooking sink of about 22% NaOH per 20 kg of TS ravara, a cellulose fraction with about 5% lignin is obtained, which seems to be an upper limit for an efficient methane solution. Higher levels of lignin have been shown to have inhibitory effects in rooting.
    The Saval cooking step, such as the evaporation of black liquor and rinsing water, has great steam requirements which are satisfied from the gasification and synthesis in the process combination of the invention.
    In pulp processes, the cooking liquor, ie alkali (NaOH), is produced by recycling sodium from the recovery boiler and burning lime in a lime kiln. Fire lime frail mesaugnen reacted with aterfort sodium flan black liquor to fly NaOH. In the process combination, the corresponding salt from the carburettor takes place on the corresponding salt. The lime kiln requires an industry which in the process combination of the invention can be caused by the gasification process.
    As stated, alternative separation processes for the division of cellulose, hemicellulose and lignin into the lignocellulose are not excluded in the process combination. The above-mentioned technique with solvent (Lignol) is, like for example, the release of cellulose with supercritical water fully conceivable. In the combination of processes of the invention, however, these separation methods meant a departure from the goal of "existing" and commercially available technology.
    As shown below, all products from the separation have been converted to methane and carbon dioxide. Saval rooting process as the thermochemical can be reacted even by any solvents used in the separation, arc & such can be easily monitored. No reprocessing and recycling of the solvents will be relevant, which is why the use of solvents will be a matter of economy. This comment is partly due to the fact that there is now access to relatively cheap glycerol from the production of rapeseed methyl ester (RME). Experiments have shown that glycerol has the ability to release lignin and that mixing glycerol in a "normal" pulp cooker can have positive effects.
    Biogas production from the cellulose fraction A separated cellulose fraction has generally been found to be much easier to ferment anaerobically than the original lignocellulose. Although the latter has been pretreated in various ways (eg by so-called "steam explosion"), residence times between 50 and 100 days are indicated for "complete" rooting (see, for example, Willian E. Eleazer, et al .; Biodegradability of Municipal Spolid Waste Components in Laboratory-Scale Landfills, 1997) while more or less pure cellulose can be rooted in 10-20 days (e.g. Laube and Martin; Conversion of Cellulose to Methane and Carbon Dioxide ... 1981).
    For simple sugars, the corresponding rooting time is shaved for hours or a few days.
    Indications of this kind are only indicative because the rooting rates are affected by the microflora inoculated, the TS levels, etc. However, the relative retention times - or vice versa the reaction rates - should be relevant. Regarding the reaction temperatures, it usually applies that 10 degrees C higher temperature in the range 30-70 degrees C doubles the reaction rate.
    The content of lignin and hemicellulose and the structural effects of them probably have the greatest effect on the rooting rate and the total resuhat. At the same time, however, a number of studies have been done on other substances in the materials and their inhibitory effect on rooting. An effect of such "contaminants" cannot be ruled out and in the invention the cellulose fraction from the alkaline separation is carefully rinsed and washed before being taken to the anaerobic fermentation. In order to exploit the potential of the invention, the cellulose fraction is further hydrolyzed enzymatically with a commercial enzyme mix (used in eg ethanol production). The temperature of the hydrolysis is maintained at 55 degrees C and with a residence time of a few hours, about 30% (of the theoretical yield) of hydrolysis of the cellulose to glucose is obtained.
    After the primary hydrolysis, an anaerobic fermentation to methane and carbon dioxide is carried out in two steps at about 55 degrees C, i.e. a thermophilic fermentation. The amount of sugar that is initially released stimulates the later rooting. In addition, a further hydrolysis with the help of the enzyme mix will continue to form simple sugars in the rooting chambers.
    After a total residence time of about 10 days, the cellulose is largely expelled and has then produced almost 300 liters of methane gas per kg COD.
    The product gas, which is a 50/50 mixture of methane and carbon dioxide, is taken to a gas water where the carbon dioxide is separated. The residue after rooting is a diluted slurry where a small amount of solid can be filtered. The water, which contains <1 g COD per liter, goes to conventional water purification.
    The cellulose fraction is relatively poor in nutrients and a supply of nitrogen and potassium, etc. must take place. The yield of methane is less than for many wastes from, for example, the food industry where fatty acids, etc. contribute to methane formation. In the combination process there is a certain amount of such available from the separation of tall oil after the alkaline separation and these are also added to the digestion.
    The anaerobic fermentation of cellulose / glucose to methane takes place in several steps and is somewhat complex. The first step is a breakdown of glucose into acetic acid, propanoic acid and butanoic acid during the simultaneous production of vale and carbon dioxide; according to the example attic acid: C6111206 -> 2 CH3COOH +4 H2 +2 CO2 (1) In a second step, propanoic acid and butanoic acid are also converted to attic acid with simultaneous production of cotton and carbon dioxide. This does not appear hdr. Methane is finally formed according to two scales: CH3COOH -> CH4 + CO2 (2) 4H2 + CO2 -> CH4 + 2 H (3) All reaction steps take place biochemically, ie under microbial influence. Under different conditions, the ratio between reactions (2) and (3) may vary. (Through some control, the total reaction can even be controlled towards hydrogen gas production) However, it is obvious that the water concentration in the solution plays a certain role in the yield. In the process combination of the invention with a gasification line, there is a possibility of controlling it by transferring hydrogen gas from the synthesis gas to the rooting of the cellulose fraction. Tests of the effect of choice on the anaerobic fermentation to methane have been reported in the literature, but they have not yet been evaluated in relation to the invention.
    Although the rooting rate through the above measures is drastically shortened, it is fundamentally the case that the reaction rate decreases with increasing degree of smoothing. The combination with a thermochemical production of methane provides an optimization possibility in that unreacted material in the rooting can be transferred to the thermochemical production of methane. Simply put, a shorter residence time in the rooting, i.e. a lower conversion of the carbohydrates in it, means that the remaining material is used in the gasification / synthesis to methane. However, this does not happen easily without complications and in addition the energy efficiency of the rooting is higher than it is in the thermochemical sub-process, so the question of how far the rooting time can be shortened becomes an optimization question.
    Theoretically, the fermentation is slightly exothermic, but in practice the thermophilic rooting requires energy supply to maintain the temperature. The biogas line thus has a heat demand which is satisfied by the process combination of the invention.
    Black liquor gasification and production of synthetic natural gas Substitute natural gas Gasification of black liquor is described in detail in another hall. It has been extensively tested and reported by, among others, Chemrec in Sweden. In short, the black liquor is gasified at high temperature with oxygen to a rag gas containing mainly hydrogen gas, carbon monoxide. carbon dioxide and methane.
    Some of the cooled and dust-cleaned ragas are extracted as fuel for the above-mentioned lime kiln. The residue is taken via a "sulfur monitor" (to protect the catalyst against sulfur poisoning) for the synthesis of methane according to the reactions: CO + 3 H2 -> CH4 + H (4) CO2 + 4 H2 -> CH4 + 2 H () After the synthesis carbon dioxide formed is separated in the same gas water as used in the biogas process.
    In the process combination of the invention, even unreacted material from the rooting can be fed to the gasification as a raw material. The gasification then not only serves as a means of increasing the methane production from the lignocellulose. From an environmental point of view, it is also a means of avoiding other environmental protection measures. One of the limitations of the transfer is that the specific energy content of the gasification raw material is lowered. Furthermore, the energy efficiency in gasification / synthesis is lagger than what it is for rooting to methane. Thus, the degree of extinction in the anaerobic fermentation to methane becomes an optimization issue for the overall process.
    In an alternative design of the process combination of the invention, the fuel demand in the lime kiln can be supplied with ravara (lignocellulose), which results in a higher yield of methane in the gasification line and somewhat improves the overall efficiency. However, this depends on how the lime kiln is designed and what kind of industry it is designed for.
    Process combination As indicated above, the process combination of the invention intends to maximize the yield of biogas / methane from lignocellulose. The example below also shows that the cellulose-based rooting is the process part that has the highest energy efficiency and produces the most methane from rava15 ran.
    This meant that the central process in the combination takes the rooting of carbohydrate term and that that sub-process is controlling for the other units. Based on this, the principle is: that the separation of the components in lignocellulose should, as far as possible, provide the rooting with the carbohydrates that are available in the raw material. that optimal conditions for rooting are met in the form of temperatures, stirring and any additive chemicals. that the required process energy for the hydrolysis and digestion steps is charged to the product from these steps to the least possible extent. • that the residual products from the rooting are handled with the least cost for environmental protection, etc.
    In short, it can be said that it is the responsibilities with these factors that prevented individual corrosion processes for lignocellulose from being established. The process combination, which naturally becomes relatively complex, thus aims in principle to solve the process technical problems that an individual rooting is burdened ay.
    In the combination, however, there are also a number of possibilities for synergy effects where the efficiency of the individual rooting process can be increased: It has been found that when rooting lignocellulose, all carbohydrates can be fermented to methane and carbon dioxide. By separating lignin from (polymeric) carbohydrates as above, the cellulose fraction can be utilized almost fully. In the alkaline separation no more than 5% of the cellulose which accompanies the black liquor is lost and the separation also gives the possibility to wash out the cellulose from other possible rooting inhibitors (an lignin).
    In the "normal" cooking process, the stone part of the hemicellulose, which is also lost in black form, is "lost". ("lost", salts in citations because it in the gasification line is also converted to methane) With a minor modification of the cooking process, however, the hemicellulose can also be "erased" to the root line. It has been clarified that in (acidic) pre-boiling of the lignocellulose large parts of the hemicellulose are hydrolysed and with a deduction of this hydrolyzate it can be fed to the root line. The technology is partly established in certain cooking processes where the purpose is primarily a leaching of certain metals from the wood raw material before it is boiled alkaline.
    As previously mentioned, there is some supply of fatty acids in the black liquor which can have a stimulating effect on the microbial rooting.
    • In terms of energy, the digestion (as well as the alkaline separation) consumes steam while the gasification line produces a lot of energy.
    The gasification line also means, of course, that the residual product (lignin, and other substances) which occur in other cases is not only treated but also used for methane production.
    Taken together, the gasification line provides the material and energy conditions for the alkaline separation which, in turn, allows considerable benefits for the decomposition to biogas; higher total sales in shorter treatment times.
    Furthermore, the rooting line and the thermochemical line provide opportunities for alternative separation processes. As long as any process chemicals in these are biodegradable or thermochemically treatable, they can be used as a methane product in the previous lines.
    Example Alkaline separation (without sulfur) has been tested with lignocellulosic frail different plant materials. At temperatures between 160 and 180 degrees C and alkali contents between 20 and weight percent NaOH (per kg TS ravara), cellulose fractions with <5% lignin have been prepared. The cellulose loss has been about 5% while the greater part of the hemicellulose has gone into solution. With an average wooden raw material that has the composition 45% cellulose, 25% hemicellulose, 26% lignin and 4% other (including extractives and inorganic material) and fed with 70% TS, a cellulose fraction of approx. 360 kg is obtained from 1 ton of raw material. TS of which 300 kg is cellulose.
    The cellulose fraction is dewatered and pH-adjusted and mixed with an enzyme mix at 50-55 degrees C for an initial hydrolysis of the cellulose in particular. After a few hours of residence time, the order of 30% of the cellulose has been hydrolyzed to glucose and the slurry is taken further to series-connected rooting reactors.
    In these, grafting material produced from the current raw material with the aid of, for example, sludge from municipal water treatment is supplied (and confirmed at stations in operation). The anaerobic fermentation starts momentarily on the basis of the previously formed glucose. As was the case with the fermentation, fatty acids from the separation of tall oil from the released lignin drum can be used, but this is not taken into account in this case.
    In the first rooting reactor, e.g. a. primary acids from the breakdown of glucose, etc. If the rate of formation of these is too great, the pH will drop and & much which is compensated with a little amount of cooking liquor from the alkaline separation. Methane and carbon dioxide production already starts in this reactor and a gas separation takes place.
    Based on general data for methane formation from glucose, a methane production of approximately 120 liters per kg COD is estimated with a 24-hour residence time, which corresponds to approximately 5 m3 in the current case. This volume also includes the continued hydrolysis of cellulose, which continues to take place with the aid of the previous enzyme mix. The temperature in the rooting reactor is 55 degrees C.
    The hydrolysis of the cellulose determines the rate of decomposition to methane and carbon dioxide. The activity of the originally added enzymes gradually decreases but is partially compensated by the microbial activity from the inoculation. In total, however, the reaction rate decreases and in a second rooting reactor residence times of about 10 days (at 55 degrees C) are required. After this time, the cellulose is almost exhausted (to the COW by the continued hydrolysis and the favored rooting of glucose).
    A total of about 130 m3 of methane is obtained from the two digestion reactors, corresponding to approximately 290 liters of methane per kg of COD in the cellulose fraction. The residual product from the roots consists of solid material in strongly diluted form and it is filtered ay. In this case, the amount of unreacted material is so small that the transfer of residue to the gasification has only.
    The lignin stream released from the alkaline separation - which is not retrievable - is evaporated to 60-70% TS and gasified with oxygen to a ragas which after condensation of water vapor mainly contains carbon monoxide, carbon dioxide and hydrogen gas and a small amount of methane. Since carbon dioxide is a potential reactant in methane synthesis, a shift of the gas does not seem necessary but is led more or less directly to the methane reactors. In these, methane according to formulas (4) and (5) above is formed and after carbon dioxide separation, 100 m3 of methane are obtained as 94% in the product gas. The other components are nitrogen gas, water vapor and carbon monoxide.
    In the lower part of the carburettor is the main part of the sodium contained in the cooking liquor for the alkaline separation. With conventional technology in the pulp industry, lime has been converted to escape boiling liquor. Lime burning requires fuel and tentatively thanks to about 75% of the filter cake from the separation of solid material in the residues' root product. The remaining fuel demand is taken from the ragas after the carburettor, or supplied as solid ravara (lignocellulose).
    In both cases, the industry's need for lime burning will lower the energy recovery rate for the total process from just over 70% to just under 70% (calculated as energy in the methane divided by energy in the raw material - without regard to electricity consumption). The internal steam needs, etc. are then met and in addition to the methane, carbon dioxide and a wastewater for water purification are obtained.
    The above examples are based for the separation process, the first hydrolysis step and the gasification on laboratory-scale test results as well as results from large-scale experiments. For the rooting, data has been extracted from reports that are available online and in the archives of granting authorities. With regard to varying data, a certain average calculation has an Tants.
    Using another separation technique for the components of the lignocellulose does not provide an example of the solvent release option to release the lignin. This technique, as described, for example, by Lignol / Repap / alcell, is carried out in the same way as "ordinary" cooking processes at 150-180 degrees C and will in these respects have similarities to the example above - to which is added a solvent handling of scope.
    With the "supercritical water" option, the process design is partly different because this technique releases the cellulose and leaves the lignin in solid form. This complicates the gasification of the indestructible lignin fraction.
    In both cases, the stated benefits are obtained by digesting a more or less pure cellulose fraction. There may be some synergy effects of the combinations of processes, but in total the complexity of the overall process seems to increase. 14
    权利要求:
    Claims (12)
    [1]
    Sail to increase the total yield of methane in biological production from lignocellulosic material, wherein methane in gas phase is produced by a fermentation process, which gas phase also contains carbon dioxide, characterized in that the lignocellulosic material is separated in a cellulose product with a weight content of less than 10%. , which then undergoes fermentation, and a residual product containing lignin, the fermentation process for producing methane is supplemented by a thermochemical synthesis process, in which the residual product is used for producing methane in gas phase, which gas phase comprises carbon dioxide as a component, the gas phases containing methane from the fermentation process and during & separation of carbon dioxide from methane, and the energy needs of the fermentation process are met by energy from the synthesis process.
    [2]
    2. A kit according to claim 1, characterized in that the energy requirements of the fermentation process are met exclusively by energy from the synthesis process.
    [3]
    Set according to claim 1 or 2, characterized in that the cellulose of the cellulose product is taken out in solid form, which is washed.
    [4]
    A kit according to claim 3, characterized in that the washed cellulose is provided with enzymes for at least partial hydrolysis of the cellulose.
    [5]
    A set according to claim 4, characterized in that the at least partially hydrolysed cellulose is fermented anaerobically to methane and carbon dioxide by microbial inoculation thereof.
    [6]
    A set according to claim 5, characterized in that the residue from the anaerobic fermentation is wholly or partly fed to the thermochemical process for methane production.
    [7]
    Set according to claim 5, characterized in that the hydrolysis and the anaerobic fermentation are carried out at 40-70 ° C, preferably at 45-60 ° C.
    [8]
    8. Set according to one or more of the oceans 1 - 7, characterized in that the residual product containing lignin in lost form with 50 - 70% by weight of dry matter content is forced to pressurized gasification with oxygen as oxidizing agent.
    [9]
    9. A kit according to claim 8, characterized in that the aqueous gas obtained from the gasification is used for the synthesis of methane.
    [10]
    A set according to claim 8 or 9, characterized in that the extractive substances separated from the residual product containing lignin are fed to the cellulose fermentation as promoting substances.
    [11]
    11. Sat according to 9, characterized in that some of the aqueous gas is forced to the anaerobic fermentation.
    [12]
    A set according to claim 11, characterized in that at most 5% by volume of the aqueous gas is fed to the anaerobic fermentation. Lignocellulose Carbon dioxide separation methane (biogas) residual filter cake for gasification Enzymatic hydrolysis of the carbohydrates filter cake Filtration Irot gas contaminated water Separation of iLignici, exicactive substances, fatty acids, ryi in and possible residues of carbohydrates 1Carbohydrates with 10% extra vitamins ) Dust training (gas water) Gasification of filter cake, lignin, etc in slurry form or as a solution lignin and the least substances fatty acids, extractives, etc. filter cake to m nin ev. water gas Possible Transfer of hydrogen content gas • Thermophilic digestion (fermentation) of the carbohydrates remained Methane synthesis Dewatering and washing of solid carbohydrate fraction FIGURE
    类似技术:
    公开号 | 公开日 | 专利标题
    Sindhu et al.2017|Water hyacinth a potential source for value addition: an overview
    Bharathiraja et al.2016|Biohydrogen and Biogas–An overview on feedstocks and enhancement process
    Ahmad et al.2016|Renewable and sustainable bioenergy production from microalgal co-cultivation with palm oil mill effluent |: A review
    Budzianowski2016|A review of potential innovations for production, conditioning and utilization of biogas with multiple-criteria assessment
    Tabatabaei et al.2020|A comprehensive review on recent biological innovations to improve biogas production, part 2: mainstream and downstream strategies
    Kumar et al.2015|Lignocellulose biohydrogen: practical challenges and recent progress
    Pham et al.2015|Food waste-to-energy conversion technologies: Current status and future directions
    ES2315272T3|2009-04-01|A PROCEDURE TO PROCESS LIGNOCELLULOSIC MATERIAL.
    Khanal et al.2008|Bioenergy and biofuel production from wastes/residues of emerging biofuel industries
    EP3374511A1|2018-09-19|Method for poultry litter fermentation and biogas production
    Chia et al.2020|Outlook on biorefinery potential of palm oil mill effluent for resource recovery
    Formann et al.2020|Beyond sugar and ethanol production: value generation opportunities through sugarcane residues
    Liao et al.2014|Integrated farm-based biorefinery
    Stamatelatou et al.2014|Biomethane and biohydrogen production via anaerobic digestion/fermentation
    US10513715B2|2019-12-24|Wet oxidation of biomass
    Trzcinski et al.2017|Microbial biomethane from solid wastes: Principles and biotechnogical processes
    Costa et al.2013|Biomethanation potential of biological and other wastes
    Seebaluck et al.2008|Bioenergy for sustainable development and global competitiveness: the case of sugar cane in Southern Africa
    SE1200203A1|2013-10-03|Ways to increase total yield of methane from lignocellulosic containing material
    Bhange et al.2012|Green waste as a resource for value added product generation: a review
    Ahmad et al.2019|Source-sink relationship of sugarcane energy production at the sugar mills
    van Haandel et al.2015|Role of anaerobic digestion in increasing the energy efficiency and energy output of sugar cane distilleries
    Chakraborty et al.2018|Thermophilic Biomethanation of Food Waste for the Production of Biogas and Concomitant Use of Biogas as a Fuel Supplement for Cooking
    Raizada et al.2002|Waste management and production of future fuels
    CN101768620A|2010-07-07|Method for producing biogas by micro-reaction thermal-explosion straw fermentation
    同族专利:
    公开号 | 公开日
    SE537504C2|2015-05-26|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE1200203A|SE537504C2|2012-04-02|2012-04-02|Ways to increase total yield of methane from lignocellulosic material|SE1200203A| SE537504C2|2012-04-02|2012-04-02|Ways to increase total yield of methane from lignocellulosic material|
    [返回顶部]