CN114317618B - Lignocellulose raw material cascade utilization process based on alkali pretreatment - Google Patents
Lignocellulose raw material cascade utilization process based on alkali pretreatment Download PDFInfo
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- 239000002994 raw material Substances 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000003513 alkali Substances 0.000 title claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 55
- 229920005610 lignin Polymers 0.000 claims abstract description 45
- 238000000855 fermentation Methods 0.000 claims abstract description 41
- 239000002245 particle Substances 0.000 claims abstract description 33
- 239000007787 solid Substances 0.000 claims abstract description 23
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229920002488 Hemicellulose Polymers 0.000 claims abstract description 19
- 229910000403 monosodium phosphate Inorganic materials 0.000 claims abstract description 19
- 235000019799 monosodium phosphate Nutrition 0.000 claims abstract description 19
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 claims abstract description 19
- 239000000463 material Substances 0.000 claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 238000003756 stirring Methods 0.000 claims abstract description 10
- 238000001035 drying Methods 0.000 claims abstract description 8
- 150000007522 mineralic acids Chemical class 0.000 claims abstract description 8
- 230000001105 regulatory effect Effects 0.000 claims abstract description 7
- 239000000706 filtrate Substances 0.000 claims abstract description 6
- 238000004062 sedimentation Methods 0.000 claims abstract description 6
- 238000001914 filtration Methods 0.000 claims abstract description 5
- 238000007710 freezing Methods 0.000 claims abstract description 5
- 230000008014 freezing Effects 0.000 claims abstract description 5
- 238000005406 washing Methods 0.000 claims abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 40
- 241000209046 Pennisetum Species 0.000 claims description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 12
- 239000010902 straw Substances 0.000 claims description 7
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 6
- 230000004151 fermentation Effects 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 claims description 4
- 238000001291 vacuum drying Methods 0.000 claims description 4
- 238000000703 high-speed centrifugation Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 description 19
- 239000007789 gas Substances 0.000 description 13
- 238000004519 manufacturing process Methods 0.000 description 13
- 238000001514 detection method Methods 0.000 description 10
- 230000000052 comparative effect Effects 0.000 description 7
- 239000012798 spherical particle Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- 238000010979 pH adjustment Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 2
- 239000002551 biofuel Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002105 nanoparticle Substances 0.000 description 2
- 239000003895 organic fertilizer Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000009396 hybridization Methods 0.000 description 1
- 239000002029 lignocellulosic biomass Substances 0.000 description 1
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
- 235000019796 monopotassium phosphate Nutrition 0.000 description 1
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Abstract
The invention discloses a lignocellulose raw material cascade utilization process based on alkali pretreatment, which comprises the following steps: (1) Crushing lignocellulose raw materials, and adding alkali liquor for alkali pretreatment; (2) carrying out solid-liquid separation on the pretreated material; (3) Anaerobic fermentation treatment is carried out on the solid A to obtain biogas; (4) Stirring the liquid B, then rapidly pouring the stirred liquid B into an inorganic acid solution, regulating the pH value to be 4.1-4.5, and carrying out solid-liquid separation after fully stirring; (5) Washing, freezing and drying the solid C to obtain lignin particles; (6) Adding ethanol into the liquid D for sedimentation treatment, regulating the pH value to be 4.1-4.5, standing, vacuum filtering, obtaining filter residues which are hemicellulose, and drying filtrate to obtain sodium dihydrogen phosphate. According to the invention, the pretreatment liquid is treated to prepare lignin particles, hemicellulose and sodium dihydrogen phosphate, and finally, the high-efficiency conversion and utilization of the lignocellulose raw material are realized.
Description
Technical Field
The invention relates to the technical field of energy utilization of lignocellulose raw materials, in particular to a step utilization process of lignocellulose raw materials based on alkali pretreatment.
Background
Because of shortage of fossil energy and environmental protection, there is an increasing demand for biofuels, and anaerobic fermentation is the most energy-efficient production process among all biofuel production technologies. Lignocellulosic biomass is widely used in anaerobic fermentation to produce methane, the methane yield of which is closely related to the biodegradability of the feedstock. Although lignocellulosic feedstock has good anaerobic fermentation potential, its recalcitrant structural properties result in its inability to be directly converted to high methane yields. Therefore, it is extremely important to improve anaerobic fermentation performance of the raw material by destroying lignocellulose structure through pretreatment.
Conventional pretreatment techniques can be categorized into physical, chemical, biological pretreatment. Among them, alkali pretreatment is one of the most commonly used pretreatment technologies with the best lignin removal effect, and compared with other chemical pretreatment, the alkali pretreatment has milder reaction conditions and does not need conditions such as high temperature, high pressure and the like. Compared with other alkali pretreatment, such as sodium carbonate delignification is lower, ammonium hydroxide needs to be subjected to high temperature and high pressure to achieve the sodium hydroxide pretreatment effect, the quicklime period is too long, and the like. Sodium hydroxide stands out as a commonly used alkaline reagent for the treatment of lignocellulose. However, sodium hydroxide pretreatment has some drawbacks, namely, a large amount of pretreatment liquid is generated, which causes harm to the environment. The pretreatment liquid is treated, and the product with additional value is produced, so that the anaerobic fermentation performance of the lignocellulose raw material is improved, and meanwhile, the economy is improved and the environmental protection is realized.
Typically, lignocellulosic feedstock is pretreated and anaerobic fermentation is carried out using only the solids fraction with disrupted internal structures, while the liquid fraction containing removed lignin and carbohydrates is often discarded. A large amount of lignin contained in the pretreatment liquid can be used to prepare lignin nanoparticles. The lignin nano particles have higher utilization value and can be used for preparing concrete, plastics and nano medicines. The hemicellulose in the pretreatment liquid can be separated and precipitated for industrial development and biotechnology. The current general acid precipitation black liquor lignin production can introduce salt which cannot be utilized to cause resource loss, so that the comprehensive alkali pretreatment and acid precipitation process needs to be provided to further improve the energy conversion efficiency and the economy of the whole process.
Disclosure of Invention
Aiming at the problem of the prior art and aiming at the characteristic of complex internal structure of the lignocellulose raw material, the invention provides a lignocellulose raw material cascade utilization process based on alkali pretreatment, which is used for treating pretreatment liquid to prepare lignin particles, hemicellulose and sodium dihydrogen phosphate while improving anaerobic fermentation performance of the lignocellulose raw material, so that the whole components of the lignocellulose raw material are comprehensively and efficiently utilized, the problems of high cost and ineffective utilization of the pretreatment liquid in the pretreatment process of the lignocellulose raw material are solved, and finally, the efficient conversion and utilization of the lignocellulose raw material are realized.
The invention aims to provide a lignocellulose raw material cascade utilization process based on alkali pretreatment, which comprises the following steps:
(1) Crushing lignocellulose raw materials, and adding alkali liquor for alkali pretreatment;
(2) Carrying out solid-liquid separation on the pretreated material in the step (1) to obtain a solid A and a liquid B;
(3) Performing anaerobic fermentation treatment on the solid A obtained in the step (2) to obtain biogas rich in methane; after the anaerobic fermentation treatment is finished, the anaerobic fermentation residues are refluxed to participate in the next anaerobic fermentation treatment;
(4) Fully stirring the liquid B obtained in the step (2), quickly transferring the liquid B into an inorganic acid solution, adjusting the pH value to be 4.1-4.5, and carrying out solid-liquid separation after fully stirring to obtain a solid C and a liquid D;
(5) Washing, freezing and drying the solid C obtained in the step (4) to obtain lignin particles;
(6) Adding ethanol into the liquid D obtained in the step (4) for sedimentation treatment, regulating the pH value to be 4.1-4.5, standing, and vacuum-filtering to obtain filter residues, namely hemicellulose, and vacuum-drying the obtained filtrate to obtain sodium dihydrogen phosphate.
Preferably, the lye in step (1) is sodium hydroxide solution.
Preferably, in step (1), the solid to liquid ratio of the lignocellulosic feedstock and lye is 1kg: (10-20) L.
Preferably, in the step (1), the mass concentration of the alkali liquor is 2.5% -5% (w/v).
Preferably, the alkaline pretreatment conditions in step (1) are: the pretreatment temperature is 30-37 ℃ and the pretreatment time is 12-24 h.
Preferably, anaerobic fermentation treatment conditions in the step (3) are as follows: the fermentation temperature is 30-37 ℃ or 50-55 ℃, the organic load of the feed is 1.0-4.0 kg VS/(m 3. Multidot. D), and the hydraulic retention time is 30-45 d.
Preferably, the inorganic acid solution in the step (4) is a phosphoric acid solution, and the mass concentration of the inorganic acid solution is 10% -15% (w/v).
Preferably, in the step (4), high-speed centrifugation is adopted to perform solid-liquid separation, and the centrifugation conditions are as follows: centrifugal speed is 8000-10000 rpm, and centrifugal time is 5-10 min.
Preferably, in the step (6), the volume ratio of the liquid D to ethanol is 1:2 to 3.
Compared with the prior art, the invention has the following advantages:
1. the invention has the advantages that the sodium hydroxide pretreatment is utilized, the lignin content in the raw materials is reduced, the internal structure of the lignocellulose raw materials is destroyed, and the anaerobic fermentation performance is improved;
2. the fermentation temperature of anaerobic fermentation treatment is medium temperature (30-37 ℃) or high temperature (50-55 ℃), because methanogens are in a relatively active state in the two temperature ranges, and the gas production rate of raw materials can be improved.
3. The anaerobic fermentation residues are subjected to reflux to participate in the next anaerobic fermentation treatment, so that the treatment problem of biogas residues and biogas slurry is avoided, and the stable operation of the anaerobic reactor is ensured.
4. The pretreatment solution obtained by pretreatment and separation of lignocellulose raw materials is poured into an inorganic acid solution, then solid-liquid separation is carried out, the obtained solid is washed, frozen and dried to obtain lignin particles, the obtained liquid is added with ethanol for sedimentation treatment and then is filtered, the obtained filter residues are hemicellulose, and the obtained filtrate is dried in vacuum to obtain sodium dihydrogen phosphate, so that the yield of each obtained substance is improved, and the energy conversion efficiency, the comprehensive utilization rate of the raw materials, the diversity of the process, the recovery rate of resources and the economic benefit are improved.
5. The morphology of the obtained lignin particles is that the spherical particle size is 60-360nm, the lignin particles are different from the traditional lignin particles used as fuel, and the lignin particles can be used for coating, glue and composite materials.
6. Controlling the pH value in the step (4) to be 4.1-4.5, wherein when the pH value is too high, the lignin particles with spherical morphology are difficult to obtain; in the step (6), the pH is controlled to be in the range of 4.1 to 4.5, because when the pH is too high or too low, another form of sodium salt is formed, and it is difficult to obtain potassium dihydrogen phosphate.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present invention.
Detailed Description
The technical solutions of the present invention will be clearly and completely described in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The equipment and reagents used in the present invention are conventional commercially available products in the art, unless specifically indicated.
Example 1
(1) The method comprises the steps of selecting the hybrid pennisetum as a lignocellulose raw material, crushing the hybrid pennisetum raw material, feeding the crushed hybrid pennisetum raw material into an alkali pretreatment device, and then adding sodium hydroxide solution with the mass concentration of 5% (w/v) for alkali pretreatment, wherein the solid-to-liquid ratio of the hybrid pennisetum raw material to the sodium hydroxide solution is 1:10, the pretreatment temperature is 37 ℃ and the pretreatment time is 24 hours.
(2) And (3) carrying out solid-liquid separation on the pretreated material in the step (1) through a high-speed centrifugal machine to obtain solid A and liquid B.
(3) And (3) feeding the solid A obtained in the step (2) into an anaerobic fermentation system for anaerobic fermentation treatment, wherein the anaerobic fermentation treatment conditions are as follows: the fermentation temperature is 37 ℃, the organic load of the feed is 2.0kg VS/(m 3. D), the hydraulic retention time is 40d, and the biogas rich in methane is obtained. The biological fuel gas is sent into a gas storage device, and can be used for cogeneration, purification, upgrading and reutilization; and (3) refluxing 85% of anaerobic fermentation residues to an anaerobic reactor to participate in the next anaerobic fermentation treatment, and preparing 15% of anaerobic fermentation residues into a solid or liquid organic fertilizer by adopting the existing process.
(4) Pouring the liquid B obtained in the step (2) into a phosphoric acid solution with the mass concentration of 10% rapidly after fully stirring at room temperature, adjusting the pH value to 4.3, and carrying out solid-liquid separation by a high-speed centrifuge after fully stirring for 20min, wherein the centrifugal speed is 8000rpm and the centrifugal time is 8min; solid C and liquid D were obtained.
(5) And (3) cleaning, freezing and drying the solid C obtained in the step (4) to obtain lignin particles.
(6) Adding ethanol into the liquid D obtained in the step (4) for sedimentation treatment, wherein the volume ratio of the liquid D to the ethanol is 1:2, regulating the pH value to 4.3, standing for 5min, vacuum filtering, drying the obtained filter residue to obtain hemicellulose, and vacuum drying the obtained filtrate to obtain sodium dihydrogen phosphate.
Through detection, the process of the embodiment 1 is adopted to treat the hybrid pennisetum, and the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, which proves that the anaerobic fermentation system operates more stably; the lignin removal rate of the hybrid pennisetum reaches 75%, and the gas production rate of the raw material is more than 280mL/gVS; the lignin particles with spherical morphology can be obtained, the morphology of the lignin particles is spherical, the particle size is 60-360nm, the lignin particles are different from the traditional lignin particles used as fuel, and the lignin particles can be used for coating, glue and composite materials; hemicellulose recovery rate is 82%, and sodium dihydrogen phosphate recovery rate is 27%.
Example 2
(1) Selecting straw as lignocellulose raw material, crushing the straw raw material, feeding the crushed straw raw material into an alkali pretreatment device, and then adding sodium hydroxide solution with the mass concentration of 2.5% (w/v) for alkali pretreatment, wherein the solid-liquid ratio of the straw raw material to the sodium hydroxide solution is 1:10, the pretreatment temperature is 30 ℃ and the pretreatment time is 12h.
(2) And (3) carrying out solid-liquid separation on the pretreated material in the step (1) through a high-speed centrifugal machine to obtain solid A and liquid B.
(3) And (3) feeding the solid A obtained in the step (2) into an anaerobic fermentation system for anaerobic fermentation treatment, wherein the anaerobic fermentation treatment conditions are as follows: the fermentation temperature is 37 ℃, the organic load of the feed is 2.0kg VS/(m 3. D), the hydraulic retention time is 40d, and the biogas rich in methane is obtained. The biological fuel gas is sent into a gas storage device, and can be used for cogeneration, purification, upgrading and reutilization; and (3) refluxing 85% of anaerobic fermentation residues to an anaerobic reactor to participate in the next anaerobic fermentation treatment, and preparing 15% of anaerobic fermentation residues into a solid or liquid organic fertilizer by adopting the existing process.
(4) Pouring the liquid B obtained in the step (2) into a phosphoric acid solution with the mass concentration of 10% rapidly after fully stirring at room temperature, adjusting the pH value to 4.1, and carrying out solid-liquid separation by a high-speed centrifuge after fully stirring for 30min, wherein the centrifugation speed is 10000rpm and the centrifugation time is 10min; solid C and liquid D were obtained.
(5) And (3) cleaning, freezing and drying the solid C obtained in the step (4) to obtain lignin particles.
(6) Adding ethanol into the liquid D obtained in the step (4) for sedimentation treatment, wherein the volume ratio of the liquid D to the ethanol is 1:2, regulating the pH value to 4.1, standing for 10min, vacuum filtering, drying the obtained filter residue to obtain hemicellulose, and vacuum drying the obtained filtrate to obtain sodium dihydrogen phosphate.
According to detection, the process of the embodiment 2 is adopted to treat the straws, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the straws reaches 70%, the gas yield of raw materials is greater than 300mL/gVS, the spherical lignin particles with the particle size of 90-480nm are obtained, the hemicellulose recovery rate is 75%, and the sodium dihydrogen phosphate recovery rate is 23%.
Example 3
This embodiment 3 differs from embodiment 1 only in that: the pH value is adjusted to 4.5 in the step (4), and the pH value is adjusted to 4.5 in the step (6).
Through detection, the process of the embodiment 3 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 280mL/gVS, and the spherical lignin particles with the particle size of 60-240nm are obtained; hemicellulose recovery rate is 85%, and sodium dihydrogen phosphate recovery rate is 21%.
Example 4
This embodiment 4 differs from embodiment 1 only in that: the mass concentration of the sodium hydroxide solution in the step (1) is 3.75% (w/v), and the solid-to-liquid ratio of the hybridization pennisetum raw material to the sodium hydroxide solution is 1:20.
Through detection, the process of the embodiment 4 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 64%, the raw material gas production rate is greater than 265mL/gVS, the spherical lignin particles with the particle size of 120-240nm are obtained, the hemicellulose recovery rate is 76%, and the sodium dihydrogen phosphate recovery rate is 32%.
Example 5
This embodiment 5 differs from embodiment 1 only in that: the mass concentration of the phosphoric acid solution in the step (4) is 15% (w/v).
By detection, the process of the embodiment 5 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 280mL/gVS, the lignin particles with spherical particle size of 210-420nm are obtained, the hemicellulose recovery rate is 73%, and the sodium dihydrogen phosphate recovery rate is 36%.
Example 6
This embodiment 6 differs from embodiment 1 only in that: the mass concentration of the phosphoric acid solution in the step (4) was 12.5% (w/v).
By detection, the process of the embodiment 6 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 280mL/gVS, the lignin particles with spherical particle size of 190-390nm are obtained, the hemicellulose recovery rate is 76%, and the sodium dihydrogen phosphate recovery rate is 30%.
Example 7
This example 7 differs from example 1 only in that: in the step (6), the volume ratio of the liquid D to the ethanol is 1:3.
Through detection, the process of the embodiment 7 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 280mL/gVS, the lignin particles with spherical particle size of 60-360nm are obtained, the hemicellulose recovery rate is 86%, and the sodium dihydrogen phosphate recovery rate is 27%.
Example 8
This embodiment 8 differs from embodiment 1 only in that: the fermentation temperature in the step (3) is 53 ℃.
Through detection, the process of the embodiment 8 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 320mL/gVS, the lignin particles with spherical particle size of 60-360nm are obtained, the hemicellulose recovery rate is 82%, and the sodium dihydrogen phosphate recovery rate is 27%.
Comparative example 1
This comparative example 1 differs from example 1 only in that: the pH value is adjusted to 2.0 in the step (4) and 2.0 in the step (6).
Through detection, the process of comparative example 1 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 320mL/gVS, the spherical lignin particles with the particle size of 120-240nm are obtained, the hemicellulose recovery rate is 89%, and sodium dihydrogen phosphate is not recovered.
Comparative example 2
This comparative example 2 differs from example 1 only in that: the pH value is adjusted to 7.0 in the step (4), and the pH value is adjusted to 7.0 in the step (6).
Through detection, the process of comparative example 2 is adopted to treat the hybrid pennisetum, the pH of the discharged material in the step (3) can be maintained at 7.2-7.5, the lignin removal rate of the hybrid pennisetum reaches 75%, the gas production rate of the raw material is more than 320mL/gVS, spherical lignin particles are not obtained, the hemicellulose recovery rate is 76%, and sodium dihydrogen phosphate is not recovered.
Comparative examples 1 and 2 differ from example 1 only in the PH adjustment in step (4) and in step (6), and the test data shows that when the PH adjustment in step (4) is too high, no lignin particles having a spherical morphology are obtained, and when the PH adjustment in step (6) is too high or too low, sodium dihydrogen phosphate is not recovered.
The above embodiments are only described to assist in understanding the technical solution of the present invention and its core idea, and it should be noted that it will be obvious to those skilled in the art that several improvements and modifications can be made to the present invention without departing from the principle of the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.
Claims (3)
1. The lignocellulose raw material cascade utilization process based on alkali pretreatment is characterized by comprising the following steps of: the process comprises the following steps:
Crushing lignocellulose raw materials, adding alkali liquor into the crushed lignocellulose raw materials for alkali pretreatment, wherein the solid-to-liquid ratio of the lignocellulose raw materials to the alkali liquor is 1kg: (10-20) L, wherein the mass concentration of alkali liquor is 2.5-5% (w/v), and the alkali pretreatment conditions are as follows: the pretreatment temperature is 30-37 ℃, the pretreatment time is 12-24 hours, and the lignocellulose raw material is straw or pennisetum;
Carrying out solid-liquid separation on the pretreated material in the step (1) to obtain a solid A and a liquid B;
Performing anaerobic fermentation treatment on the solid A obtained in the step (2) to obtain biogas rich in methane; after the anaerobic fermentation treatment is finished, the anaerobic fermentation residues are refluxed to participate in the next anaerobic fermentation treatment, and the anaerobic fermentation treatment conditions are as follows: the fermentation temperature is 30-37 ℃ or 50-55 ℃, the feeding organic load is 1.0-4.0 kg VS/(m 3 x d), and the hydraulic retention time is 30-45 d;
Fully stirring the liquid B obtained in the step (2), quickly transferring the liquid B into an inorganic acid solution, regulating the pH value to be 4.1-4.5, and carrying out solid-liquid separation after fully stirring to obtain solid C and liquid D, wherein the inorganic acid solution is a phosphoric acid solution, and the mass concentration of the inorganic acid solution is 10% -15% (w/v);
washing, freezing and drying the solid C obtained in the step (4) to obtain lignin particles;
Adding ethanol into the liquid D obtained in the step (4) for sedimentation treatment, wherein the volume ratio of the liquid D to the ethanol is 1: 2-3, regulating the pH value to be 4.1-4.5, standing, and vacuum-filtering to obtain filter residues, namely hemicellulose, and vacuum-drying the obtained filtrate to obtain sodium dihydrogen phosphate.
2. The alkali pretreatment-based lignocellulose raw material cascade utilization process according to claim 1, wherein the alkali liquor in the step (1) is sodium hydroxide solution.
3. The step utilization process of lignocellulose raw material based on alkali pretreatment according to claim 1, wherein in the step (4), solid-liquid separation is performed by high-speed centrifugation under the following conditions: the centrifugal speed is 8000-10000 rpm, and the centrifugal time is 5-10 min.
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| CN115433742B (en) * | 2022-08-12 | 2024-03-19 | 中国林业科学研究院林产化学工业研究所 | Method for co-producing biogas and organic fertilizer from agricultural and forestry residues through solid anaerobic fermentation |
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| CN111172201A (en) * | 2020-01-16 | 2020-05-19 | 吉林大学 | A kind of method for preparing cellulosic ethanol by alkali pretreatment |
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| CN111172201A (en) * | 2020-01-16 | 2020-05-19 | 吉林大学 | A kind of method for preparing cellulosic ethanol by alkali pretreatment |
| CN111394402A (en) * | 2020-03-09 | 2020-07-10 | 中国科学院广州能源研究所 | Method for co-producing medium-chain fatty acid and biogas by using wood fiber raw material |
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