CN103509827B - A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating - Google Patents
A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating Download PDFInfo
- Publication number
- CN103509827B CN103509827B CN201210211831.4A CN201210211831A CN103509827B CN 103509827 B CN103509827 B CN 103509827B CN 201210211831 A CN201210211831 A CN 201210211831A CN 103509827 B CN103509827 B CN 103509827B
- Authority
- CN
- China
- Prior art keywords
- fermentation
- solid
- steam explosion
- stalk
- simultaneous saccharification
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 185
- 240000008042 Zea mays Species 0.000 title claims abstract description 129
- 235000002017 Zea mays subsp mays Nutrition 0.000 title claims abstract description 129
- 238000000034 method Methods 0.000 title claims abstract description 104
- 239000010902 straw Substances 0.000 title claims abstract description 93
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 title claims abstract description 70
- 235000009973 maize Nutrition 0.000 title claims abstract description 70
- 238000000855 fermentation Methods 0.000 claims abstract description 154
- 230000004151 fermentation Effects 0.000 claims abstract description 153
- 238000004880 explosion Methods 0.000 claims abstract description 96
- 239000007787 solid Substances 0.000 claims abstract description 92
- 238000004821 distillation Methods 0.000 claims abstract description 35
- 238000004519 manufacturing process Methods 0.000 claims abstract description 33
- 238000010248 power generation Methods 0.000 claims abstract description 31
- 238000002485 combustion reaction Methods 0.000 claims abstract description 30
- 230000008569 process Effects 0.000 claims abstract description 30
- 238000005265 energy consumption Methods 0.000 claims abstract description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 87
- 239000007788 liquid Substances 0.000 claims description 72
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims description 59
- 235000005822 corn Nutrition 0.000 claims description 59
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 36
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 31
- 239000000126 substance Substances 0.000 claims description 23
- 108010059892 Cellulase Proteins 0.000 claims description 21
- 229940106157 cellulase Drugs 0.000 claims description 21
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 18
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 18
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 18
- 241000894006 Bacteria Species 0.000 claims description 16
- 108090000790 Enzymes Proteins 0.000 claims description 16
- 102000004190 Enzymes Human genes 0.000 claims description 16
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 claims description 16
- 229940088598 enzyme Drugs 0.000 claims description 16
- 239000002028 Biomass Substances 0.000 claims description 14
- 230000005611 electricity Effects 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 238000010353 genetic engineering Methods 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000007598 dipping method Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 6
- 230000007062 hydrolysis Effects 0.000 claims description 6
- 238000006460 hydrolysis reaction Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000002054 inoculum Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000010802 sludge Substances 0.000 claims description 5
- 235000011194 food seasoning agent Nutrition 0.000 claims description 4
- 238000000227 grinding Methods 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 239000000843 powder Substances 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 238000002791 soaking Methods 0.000 claims description 2
- 229920002488 Hemicellulose Polymers 0.000 abstract description 11
- 229920002678 cellulose Polymers 0.000 abstract description 7
- 239000001913 cellulose Substances 0.000 abstract description 7
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 62
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 40
- NOEGNKMFWQHSLB-UHFFFAOYSA-N 5-hydroxymethylfurfural Chemical compound OCC1=CC=C(C=O)O1 NOEGNKMFWQHSLB-UHFFFAOYSA-N 0.000 description 31
- RJGBSYZFOCAGQY-UHFFFAOYSA-N hydroxymethylfurfural Natural products COC1=CC=C(C=O)O1 RJGBSYZFOCAGQY-UHFFFAOYSA-N 0.000 description 31
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 30
- 239000008103 glucose Substances 0.000 description 30
- 229960003487 xylose Drugs 0.000 description 30
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 description 28
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 23
- SRBFZHDQGSBBOR-LECHCGJUSA-N alpha-D-xylose Chemical compound O[C@@H]1CO[C@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-LECHCGJUSA-N 0.000 description 16
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 description 14
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 description 14
- 238000011084 recovery Methods 0.000 description 14
- 239000000446 fuel Substances 0.000 description 8
- 239000000835 fiber Substances 0.000 description 7
- 239000000758 substrate Substances 0.000 description 7
- 239000001117 sulphuric acid Substances 0.000 description 7
- 235000011149 sulphuric acid Nutrition 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- 239000003112 inhibitor Substances 0.000 description 4
- 108090000623 proteins and genes Proteins 0.000 description 4
- 230000009466 transformation Effects 0.000 description 4
- LPQOADBMXVRBNX-UHFFFAOYSA-N ac1ldcw0 Chemical compound Cl.C1CN(C)CCN1C1=C(F)C=C2C(=O)C(C(O)=O)=CN3CCSC1=C32 LPQOADBMXVRBNX-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000004817 gas chromatography Methods 0.000 description 3
- 150000002402 hexoses Chemical class 0.000 description 3
- 150000002972 pentoses Chemical class 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229920002307 Dextran Polymers 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 229920001131 Pulp (paper) Polymers 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- HEBKCHPVOIAQTA-NGQZWQHPSA-N d-xylitol Chemical compound OC[C@H](O)C(O)[C@H](O)CO HEBKCHPVOIAQTA-NGQZWQHPSA-N 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000004537 pulping Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 238000010563 solid-state fermentation Methods 0.000 description 2
- 229920001221 xylan Polymers 0.000 description 2
- 150000004823 xylans Chemical class 0.000 description 2
- 241000209128 Bambusa Species 0.000 description 1
- 244000025254 Cannabis sativa Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- 238000005844 autocatalytic reaction Methods 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- -1 biogas Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010812 external standard method Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 239000002198 insoluble material Substances 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 238000004811 liquid chromatography Methods 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 230000004580 weight loss Effects 0.000 description 1
- 235000015099 wheat brans Nutrition 0.000 description 1
Classifications
-
- 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
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- 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
Abstract
The invention provides a kind of method utilizing maize straw power generating simultaneously ethanol and biogas, the method comprises the following steps: 1. preimpregnation; 2. Steam explosion treatment; 3. simultaneous saccharification and fermentation and distillation; 4. solid residue combustion power generation; 5. anaerobically fermenting.Mierocrystalline cellulose in stalk, hemicellulose and xylogen are separately converted to ethanol, biogas and electric energy by the method, utilize remaining steam in electric energy and power generation process to solve the energy consumption in a part of ethanol production process, thus improve the utilization ratio of stalk, reduce the production cost of cellulosic ethanol.
Description
Technical field
The invention belongs to biomass energy field, relate to maize straw alcohol electricity co-production technology particularly, particularly a kind of method utilizing maize straw to produce ethanol, biogas coproduction generating.
Background technology
Along with the development of economic society, the whole world constantly increases the demand of the energy, and traditional fossil energy consumes caused energy shortage, environmental pollution and weather variation issue in a large number and is becoming increasingly acute.And biomass energy is more and more subject to the attention of national governments and scientist as a kind of renewable energy source.Stalk is a kind of well clean reproducible energy, is one of new forms of energy of most developing and utilizingpotentiality, has good economy, ecology and social benefit.Stalk has multiple development and utilization measure, straw-returning, gasifying stalk, straw power generation, alcohol production by stalk etc.China is the output big country of stalk, and annual stalk output has 700,000,000 tons, but the energy can be utilized now to only have 50%, and major part is the modes of urban residents by inefficient combustion.By improving the comprehensive utilization ratio of stalk, the high quality conversion accelerating stalk is imperative.
Chinese patent CN101519671B discloses the processing method of a kind of hybrid giant napier transforming fuel alcohol coproduction generating, paper pulp, and its technical process as shown in Figure 1.The method mainly comprises the following steps:
(1) tieed up under 1.5MPa pressure to hybrid giant napier raw material pressure one short period of time and carry out steam explosion pre-treatment;
(2) xylo-oligosaccharide preparation: carry out washing process to the quick-fried rear hybrid giant napier of vapour, water lotion is the hemicellulose after degraded, for the preparation of xylo-oligosaccharide;
(3) long and short fiber classification: the hybrid giant napier after the quick-fried process of vapour by obtain after classification combing staple length be greater than 3cm macrofiber element and staple length be less than 3cm staple fibre;
(4) macrofiber element slurrying: after combing, macrofiber is used for ethanol autocatalysis slurrying then bleaching;
(5) staple fibre solid state fermentation cellulase: get the staple cellulose 4g after combing, wheat bran 1g, contain (NH with every 100ml
4)
2sO
41.5g, MgSO
40.6g, KH
2pO
4mix after the inorganic salt solution 12ml of 0.3g is moistening, 121 DEG C, after sterilizing in 30 minutes, access 3ml viride seed liquor, 30 DEG C of cultivations; Cultivate working sample after 4 days all the time and filter paper enzyme activity.
(6) staple fibre simultaneous saccharification and fermentation: solid-to-liquid ratio 1: 20, every gram of substrate adds 20IUFPU cellulase and 0.01g yeast, obtains ethanol in 37 DEG C of fermentation 72h distillation;
(7) after simultaneous saccharification and fermentation slag drying treatment for biomass power generation fuel, simultaneously reclaim fermentation produce CO
2.
The index of correlation of this technical scheme:
(1) long and short proportion of fibers: 1:0.4
(2) macrofiber slurrying slightly starch, screened yield and delignification rate: 52.6%, 34.5%, 83.2%
(3) solid state fermentation cellulase sample weight loss and filter paper enzyme activity (FPU): 24.6%, 39.8(IU/g dry medium)
(4) simultaneous saccharification and fermentation alcohol getting rate: 0.129g ethanol/g substrate
(5) hybrid giant napier fermentation residue calorific value: 19.03MJ/kg
Technique scheme also has the following disadvantages:
(1) pretreatment process that this technical scheme uses is conventional vapor explosion preconditioning technique, a large amount of monose in hydrolyzed solution after vapour can be caused quick-fried are degraded further, degraded product is mainly the fermentation inhibitors such as furfural, hydroxymethylfurfural and acetic acid, both decrease the productive rate of monose, have impact on again the productive rate of ethanol in fermenting process.
(2) this technology does not make raw material be fully exploited, from its 52.6% slightly slurry and 34.5% screened yield, raw material has larger loss in pulping process.In addition, owing to adopting hydrogen peroxide and sodium hydroxide to carry out boiling to macrofiber in long stapled bleaching process, and the xylogen in macrofiber and hemicellulose are removed, but the hemicellulose that this partial loss do not fallen of this technical scheme and xylogen use.In addition, can produce a large amount of black liquor in employing sodium hydroxide pulping by cooking process, the words of directly discharge can cause larger pollution to environment.
(3) this technical scheme does not adopt and the bacterial classification of pentose and hexose can be utilized simultaneously to ferment in simultaneous saccharification and fermentation process, and in staple fibre, remaining hemicellulose effectively can not be converted into ethanol.The alcohol getting rate of this technology is not high, is only 12.9g/100g substrate.In addition, the large usage quantity of enzyme used in fermentation, up to 20FPU/g substrate, when the price height enterprise of Current commercial enzyme, is difficult to carry out scale operation.
The present invention is in order to overcome above-mentioned technical deficiency, employing maize straw is raw material, improve cellulosic enzymic hydrolysis by the diluted acid preimpregnation steam explosion preconditioning technique of uniqueness and reduce the generation of the fermentation inhibitor such as furfural, hydroxymethylfurfural, Mierocrystalline cellulose in stalk, hemicellulose and xylogen are separately converted to ethanol, biogas and electric energy, utilize remaining steam in electric energy and power generation process to solve the energy consumption in a part of ethanol production process, thus improve the utilization ratio of stalk, the production cost of reduction cellulosic ethanol.
Specifications is as follows:
Glucose after dilute sulphuric acid preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 102.4%, 99.6%.
Glucose after dilute sulphuric acid preimpregnation Steam explosion treatment, xylose rate: 7.8%, 75.4%.
The furfural, the hydroxymethylfurfural that generate after dilute sulphuric acid preimpregnation Steam explosion treatment: 0.69g furfural/100g Dry corn stalk stalk, 0.21g hydroxymethylfurfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after sulfuric acid preimpregnation Steam explosion treatment: 22.5g/l, 15.0g ethanol/100g Dry corn stalk stalk.
Methane yield: 8.1g/100g Dry corn stalk stalk.
Fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 22.5g/l, 14.3g ethanol/100g Dry corn stalk stalk.
Methane yield: 8.0g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 24.2g/l, 15.2g ethanol/100g Dry corn stalk stalk.
Methane yield: 8.0g/100g Dry corn stalk stalk
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after dilute sulphuric acid preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 102.4%, 99.6%.
Glucose after dilute sulphuric acid preimpregnation Steam explosion treatment, xylose rate: 7.8%, 75.4%.
The furfural, the hydroxymethylfurfural that generate after dilute sulphuric acid preimpregnation Steam explosion treatment: 0.69g furfural/100g Dry corn stalk stalk, 0.21g hydroxymethylfurfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after dilute sulphuric acid preimpregnation Steam explosion treatment: 22.6g/l, 15.0g ethanol/100g Dry corn stalk stalk.
Methane yield: 10.3g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 26.6g/l, 15.3g ethanol/100g Dry corn stalk stalk.
Methane produces yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 34.1g/l, 16.4g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 37.7g/l, 14.9g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 45.1g/l, 14.5g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 49.9g/l, 13.6g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 42.8g/l, 13.8g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Specifications is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, the yield of maize straw after acetic acid preimpregnation Steam explosion treatment: 47.2g/l, 12.9g ethanol/100g Dry corn stalk stalk.
Methane yield: 11.5g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Summary of the invention
The invention provides a kind of method utilizing maize straw to produce ethanol, biogas coproduction generating, the method high integration following steps: preimpregnation, steam explosion treatment, simultaneous saccharification and fermentation, combustion power generation, anaerobically fermenting.
Production Flow Chart after integration, can significantly improve the comprehensive utilization ratio of maize straw, energy co-producing fuel ethanol and biogas, and co-production generates electricity, and significantly improves the capacity usage ratio of maize straw.By utilizing electric energy and the steam of xylogen and biogas combustion generation in production process, greatly reduce the production cost of cellulosic ethanol.
Provide a kind of method utilizing maize straw to produce ethanol, biogas coproduction generating in a technical scheme of the present invention, the method comprises the following steps:
1. preimpregnation: use acid dipping for some time after corn straw smashing;
2. Steam explosion treatment: the maize straw of preimpregnation is placed in reactor and carries out Steam explosion treatment;
3. simultaneous saccharification and fermentation: the straw pulp formed after step 2. Steam explosion treatment is carried out simultaneous saccharification and fermentation, wherein solid-liquid mass percent is 10% ~ 20%, apply suitable genetic engineering bacterium or yeast saccharomyces cerevisiae and suitable enzyme, under suitable conditions after fermentation, distillation obtains ethanol, and reclaims the CO of fermentation generation
2, separate fermentation product, obtains solid residue and fermented liquid;
4. solid residue combustion power generation: send into biomass power plant combustion power generation after solid residue drying step 3. obtained.Wherein the main component of solid residue is xylogen.
5. anaerobically fermenting: fermented liquid step 3. obtained carries out anaerobically fermenting, collects the biogas produced.
Maize straw described in aforesaid method can be dry straw, also can be wet stalk.
In a specific embodiment of the present invention, described method, before carrying out step simultaneous saccharification and fermentation 3., also has the step being separated straw pulp, the straw pulp formed after step 2. Steam explosion treatment is carried out solid-liquid separation, carrying out the 3. described simultaneous saccharification and fermentation of step by being separated the solid obtained, being separated the liquid obtained and carrying out the 5. described anaerobically fermenting of step together with the fermented liquid suddenly 3. obtained;
Preferably, by being separated before the solid that obtains carries out simultaneous saccharification and fermentation, first adding suitable enzyme and carrying out prehydrolysis, then add suitable genetic engineering bacterium or yeast ferments;
Preferred prehydrolysis condition is 40 ~ 50 DEG C of hydrolysis 3 ~ 5 hours, and preferred prehydrolysis condition is 45 DEG C of prehydrolysis 4h.
In a specific embodiment of the present invention, described method, before carrying out step simultaneous saccharification and fermentation 3., also has the step being separated straw pulp, the straw pulp formed after step 2. Steam explosion treatment is carried out solid-liquid separation, applying suitable genetic engineering bacterium by being separated the liquid obtained, carry out the pre fermentation regular hour under suitable fermentation condition after, fermented liquid being carried out the 3. described simultaneous saccharification and fermentation of step in the lump together with being separated the solid obtained;
Preferably, described pre-fermented fermentation condition is: be 30 DEG C ~ 35 DEG C in temperature, and pH value is under the condition of 5.0 ~ 6.0, ferments 45 ~ 50 hours, is preferably under the condition of 5.5 in pH value, ferments 48 hours.
In a specific embodiment of the present invention, the step of wherein said separation straw pulp is separated by pressure filter, and preferred separating pressure is 270bar.The water content of the solid part after separation is about 47% ~ 55%.
In a specific embodiment of the present invention, wherein said step 1. in, the grinding mode of preferred maize straw is that beater grinder is pulverized;
Preferably, corn stalk powder is broken to 1 ~ 5cm;
Preferably, described acid is sulfuric acid or acetic acid;
Preferably, the concentration of described sulfuric acid is 0.1 ~ 2%, and the concentration of described acetic acid is 0.5 ~ 2%; More preferably, the concentration of described sulfuric acid is 0.2%, and the concentration of described acetic acid is 1%;
Preferably, described dipping is after the acid taking respective quality, is diluted to suitable concn with water, then is used for soaking maize stalk;
Preferably, dipping time is 60 ~ 120 minutes;
In a specific embodiment of the present invention, wherein said step 2. in, the condition of described steam explosion reaction is: pressure 1.25 ~ 1.90MPa, temperature 190 DEG C ~ 210 DEG C, 5 ~ 10 minutes reaction times;
In a specific embodiment of the present invention, wherein said suitable genetic engineering bacterium or the concentration of yeast are 2 ~ 4g/L, and the consumption of described suitable enzyme is 9 ~ 11FPU/g solid substance;
Preferably, described suitable genetic engineering bacterium or the concentration of yeast are 3g/L, and the consumption of described suitable enzyme is 10FPU/g solid substance;
Preferably, described suitable genetic engineering bacterium is KE6-12 bacterium (is also Taurus04, provided by TaurusEnergyAB company of Sweden), described yeast be yeast saccharomyces cerevisiae (by
aB company provides), described suitable enzyme is cellulase (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2);
Preferably, also the Secondary ammonium phosphate of 0.4 ~ 0.6g/l and the magnesium sulfate of 0.02 ~ 0.03g/l is contained in described pre fermentation system or in step simultaneous saccharification and fermentation system 3.; More preferably, the Secondary ammonium phosphate containing 0.5g/l and the magnesium sulfate of 0.025g/l;
Preferably, step fermentation condition is 3.: at the temperature bottom fermentation 72 ~ 120 hours of 30 DEG C ~ 35 DEG C;
Preferably, the step 3. separate mode of middle fermented liquid is be separated with pressure filter, and preferred pressure filter is plate-and-frame filter press.
In a specific embodiment of the present invention, wherein step 4. in the drying mode of solid residue be seasoning;
Preferably, step 4. in the electricity that produces be used for 1. required to the step production process 3. energy consumption of replenish step, step 4. in the exhaust steam that produces be used for step Steam explosion treatment 2. and step 3. in distillation.
In a specific embodiment of the present invention, wherein the condition of step 5. anaerobically fermenting is temperature 55 DEG C, oxygen-free environment, and inoculum is for active sludge is (containing the flora needed for biogas fermentation in mud, thered is provided by Domsjo company of Sweden), preferred oxygen-free environment is nitrogen environment.
The dry solids obtained after straw pulp filtration drying after " solid substance " described in the present invention refers to Steam explosion treatment.More specifically, this solid substance is water insoluble solids, refer to water-fast solid matter, maize straw is after explosion pre-treatment, the grease contained in stalk, protein can be dissolved in water, also have part hemicellulose can be hydrolyzed to oligose or monose and soluble in water, remaining composition in stalk, then still water insoluble with solid form existence, what solid substance referred to is exactly the insoluble material of this part.
" solid-liquid mass percent " described in the present invention refers to the per-cent of the quality of the fermented liquid in the quality of the solid substance in simultaneous saccharification and fermentation system and whole simultaneous saccharification and fermentation system.
The concentration of described sulfuric acid refers to the mass percent of sulfuric acid in aqueous sulfuric acid.
" exhaust steam " described in the present invention, refer to that xylogen is after biomass combustion boiler combustion, its heat produced is used for heating water, make it change steam into, this Steam Actuation steam turbine rotates, for generating, steam after generating reduces due to kinetic energy, can not continue on for generating again, but it also has certain temperature, is therefore referred to as exhaust steam.
The beneficial effect of the invention
The present invention is that raw material is improved cellulosic enzymic hydrolysis by unique diluted acid preimpregnation steam explosion preconditioning technique and reduced the generation of the fermentation inhibitor such as furfural, hydroxymethylfurfural with maize straw, Mierocrystalline cellulose in stalk, hemicellulose and xylogen are separately converted to ethanol, biogas and electric energy, utilize remaining steam in electric energy and power generation process to solve the energy consumption in a part of ethanol production process, thus improve the utilization ratio of stalk, the production cost of reduction cellulosic ethanol.Concrete advantage comprise following some:
(1) produce biogas and lignin residue combustion power generation with the cellulose raw producing and ethanol in the pretreated maize straw of diluted acid dipping steam explosion, hemicellulose, and steam remaining in the electricity of production and power generation process is used for the alcohol electricity co-production technology of alcohol production.
(2) before stalk carries out Steam explosion treatment, carry out preimpregnation with diluted acid, improve cellulosic enzymic hydrolysis in maize straw.Compare conventional vapor explosion, while raising cellulase hydrolysis efficiency, effectively can also reduce the generation of the fermentation inhibitor such as furfural, hydroxymethylfurfural.
(3) dry, wet two kinds of maize straws all can the system of entering be produced.
(4) bioenergy of production solid, liquid, gas three kinds of forms in same system.Solid refers to the solid molding fuel that the residues such as xylogen are formed, can for biomass electric power plant fuel, and gas refers to biogas, after being separated, purifying, obtain methane, and can be used for civilian or biomass electric power plant fuel use, liquid refers to alcohol fuel.
(5) by alcohol electricity co-production technology of the present invention, the production of cellulosic ethanol is organically combined with generating power with biomass combustion, take full advantage of these three kinds of main components of the Mierocrystalline cellulose in stalk, hemicellulose and xylogen, improve the comprehensive utilization ratio of maize straw.The systems simulation that process simulation software AspenPlus, AspenIcarus carry out shows, the capacity usage ratio that production model is produced in alcohol Electricity Federation of the present invention can reach more than 70%, higher than the 50-60% of cellulosic ethanol production and the 30-35% of biomass direct combustion power generation.
(6) by the electric energy that utilizes xylogen and biogas combustion to produce and steam in the production process of cellulosic ethanol, greatly reduce the production cost of cellulosic ethanol, by the simulation of Aspen software, the more single cellulosic ethanol production of investment that is produced from alcohol Electricity Federation and biomass direct combustion power generation project investment summation can save more than 20-30%, and working cost can reduce more than 10-15%.Cellulosic ethanol of the present invention and biomass power generation coproduction, by the network coupling of efficient, the energy-conservation alcohol electricity total system network of rivers and ther mal network coupling, realize logistics, the flow-optimized coupling of energy, significantly can reduce fresh water consumption and live steam consumption, gas, liquid, solid three bioenergies of co-producing fuel ethanol, biogas, solid bio-fuel, significantly improve capacity usage ratio.
Accompanying drawing explanation
Fig. 1 bambusa textile grass transforms the process flow sheet of the generating of dyestuff co-productiono f ethanol, paper pulp;
The process flow sheet of Fig. 2 embodiment of the present invention 1;
The process flow sheet of Fig. 3 embodiment of the present invention 2;
The process flow sheet of Fig. 4 embodiment of the present invention 3.
Embodiment
Below in conjunction with embodiment, embodiment of the present invention are described in detail, but it will be understood to those of skill in the art that the following example only for illustration of the present invention, and should not be considered as limiting scope of the present invention.Unreceipted actual conditions person in embodiment, the condition of conveniently conditioned disjunction manufacturers suggestion is carried out.Agents useful for same or the unreceipted production firm person of instrument, being can by the conventional products of commercial acquisition.
Technical indicator described in following examples kind is by high performance liquid chromatography, with the concentration of the inhibitions such as the glucose in external standard method solution, wood sugar, furfural and hydroxymethylfurfural, then obtains the total amount of respective substance according to the volume of solution.
The rate of recovery obtains divided by the initial mass of this material in maize straw with the total amount of respective substance.
Inversion rate of glucose is with the initial mass of its total amount divided by dextran in maize straw, then is multiplied by that transformation ratio 0.9 draws.Dextran is formed glycosidic link by many glucose molecules be connected to form by dehydration, and so the method for calculation of its transformation ratio 0.9 are: the molecular weight of glucose is 180, and to lose the quality after a water molecules be 162,162 equal 0.9 divided by 180.
Xylose rate is with the initial mass of its total amount divided by xylan in maize straw, then is multiplied by that transformation ratio 0.88 draws.Also to be wood sugar molecule form glycosidic link by dehydration to xylan is connected to form, and the method for calculation of its transformation ratio 0.88 are: wood sugar molecular weight is 150, and to lose the quality after a water molecules be 132,132 equal 0.88 divided by 150.
Yield obtains divided by maize straw initial mass with the total amount of respective substance.
Liquid chromatography used is purchased from Japanese Shimadzu Corporation.
Calorific value is measured by calorimeter.
Embodiment 1
Shown in schema as shown in Figure 2, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. preimpregnation: first get maize straw, with beater grinder by crushed stalk to 1 ~ 5cm, is then the sulfuric acid of 0.2% by concentration, by maize straw preimpregnation 120min at normal temperatures and pressures.
2. Steam explosion treatment: will be placed in after steam explosion reactor keeps 10min at temperature 190 DEG C (pressure 1.25MPa) through the stalk of preimpregnation, (be less than 0.5 second) instantaneously and open valve, the straw pulp formed after pretreatment by stalk pours in flash tank.
3. simultaneous saccharification and fermentation and distillation: the straw pulp in flash tank is positioned in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, wherein also contain the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in fermentation system, use yeast saccharomyces cerevisiae to ferment, the addition of yeast is 3g/l, and the consumption of cellulase is 10FPU/g solid substance, in temperature 35 DEG C, pH is after the condition bottom fermentation 96h of 5, obtains ethanol by distillation, reclaims the CO that fermentation produces
2.Solid residue and fermented liquid is obtained with plate-and-frame filter press separate fermentation product.
4. solid residue combustion power generation: the step 3. middle solid residue obtained that is separated is mainly xylogen, biomass power plant combustion power generation is sent into after seasoning, the electricity of production is used for the energy consumption that replenish step is 1. required to step production process 3., the exhaust steam of generation be used for step Steam explosion treatment 2. and step 3. in distillation.
5. anaerobically fermenting: the step fermented liquid that 3. middle separation obtains is placed in fermentor tank and carries out anaerobically fermenting, collects the biogas produced.Anaerobically fermenting carries out at 55 DEG C, fermentor tank is full of nitrogen, to ensure oxygen-free environment before fermentation.Inoculum is active sludge (containing the flora needed for biogas fermentation in mud, being provided by Domsjo company of Sweden).The content gas-chromatography (Japanese Shimadzu) of methane measures.
Embodiment 2
Shown in schema as shown in Figure 2, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. preimpregnation: first get maize straw, with beater grinder by crushed stalk to 1 ~ 5cm, is then the acetic acid of 1% by concentration, by maize straw preimpregnation 120min at normal temperatures and pressures.
2. Steam explosion treatment: will be placed in after steam explosion reactor keeps 5min at temperature 200 DEG C (pressure 1.55MPa) through the stalk of preimpregnation, (be less than 0.5 second) instantaneously and open valve, the straw pulp formed after pretreatment by stalk pours in flash tank.
3. the operation of simultaneous saccharification and fermentation and distillation, 4. solid residue combustion power generation, 5. anaerobically fermenting step is with embodiment 1.
Embodiment 3
Shown in schema as shown in Figure 2, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. preimpregnation: first get maize straw, with beater grinder by crushed stalk to 1 ~ 5cm, is then the acetic acid of 1% by concentration, by maize straw preimpregnation 120min at normal temperatures and pressures.
2. Steam explosion treatment: will be placed in after steam explosion reactor keeps 5min at temperature 200 DEG C (pressure 1.55MPa) through the stalk of preimpregnation, (be less than 0.5 second) instantaneously and open valve, the straw pulp formed after pretreatment by stalk pours in flash tank.
3. simultaneous saccharification and fermentation and distillation: the straw pulp in flash tank is positioned in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, wherein also contain the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in fermentation system, gene engineering yeast KE6-12 (Taurusenergy company provides) is used to ferment, the addition of yeast is 3g/l, the consumption of cellulase is 10FPU/g solid substance, ferment in temperature 35 DEG C, pH obtains ethanol by distillation after carrying out 144h under the condition of 5.5, reclaims the CO that fermentation produces
2.Solid residue and fermented liquid is obtained with plate-and-frame filter press separate fermentation product.
4. the operation of solid residue combustion power generation, 5. anaerobically fermenting is with embodiment 1.
Embodiment 4
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 1.
2. Steam explosion treatment: the stalk through preimpregnation is placed in steam explosion reactor, reacts 10min at temperature 190 DEG C (pressure is 1.25MPa).At the end of reaction, (be less than 0.5s) instantaneously and open valve, the straw pulp formed after pretreatment by stalk pours in flash tank.
3. solid-liquid separation: the liquid portion in straw pulp pretreated in making step 2. by plate-and-frame filter press with the pressure of 270bar is separated with solid part, about 47% ~ 55%, (47 ~ 55% water content refer to that the quality of the water contained in solid accounts for the per-cent of whole solid masses to the water content of solid part.This solid is the wet solid obtained after press filtration).Liquid portion is directly sent into anaerobic fermentation tank and is produced biogas, and solid part carries out step simultaneous saccharification and fermentation 4. and produces ethanol.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 96h under the condition of 5, obtain ethanol finally by distillation, reclaim the CO that fermentation produces
2.Solid residue and fermented liquid is obtained with plate-and-frame filter press separate fermentation product.
5. the operation of solid residue combustion power generation is with embodiment 1.
6. anaerobically fermenting: the pretreated liquid portion of stalk steam explosion directly with simultaneous saccharification and fermentation after remaining fermented liquid be placed in fermentor tank and carry out anaerobically fermenting, collect the biogas of generation.Anaerobically fermenting carries out at 55 DEG C, fermentor tank is full of nitrogen, to ensure oxygen-free environment before fermentation.Inoculum is active sludge (containing the flora needed for biogas fermentation in mud, being provided by Domsjo company of Sweden).The content gas-chromatography (Japanese Shimadzu) of methane measures.
Embodiment 5
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 96h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 6
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 12.5%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Solid residue and fermented liquid is obtained with plate-and-frame filter press separate fermentation product.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 7
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 15%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 8
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 17.5%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 9
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 20%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, cellulase is (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) consumption be 10FPU/g solid substance, ferment in temperature 35 DEG C, pH carries out 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 10
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 17.5%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, the consumption of cellulase (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) is 10FPU/g solid substance.First enzyme-added before fermentation, with 45 DEG C of first prehydrolysis 4h, then add yeast saccharomyces cerevisiae, in temperature 35 DEG C, pH carries out fermentation 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 11
Shown in schema as shown in Figure 3, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 4.
4. simultaneous saccharification and fermentation and distillation: solid part step 3. obtained is placed in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 20%, wherein the substratum of fermentation system contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l, the addition of yeast saccharomyces cerevisiae is 3g/l, the consumption of cellulase (purchased from letter (Novozymes) company of Novi, commodity are called CellicCtec2.) is 10FPU/g solid substance.First enzyme-added before fermentation, with 45 DEG C of first prehydrolysis 4h, then add yeast saccharomyces cerevisiae, in temperature 35 DEG C, pH carries out fermentation 120h under the condition of 5.Obtain ethanol by distillation afterwards, reclaim the CO that fermentation produces
2.Separate fermentation product obtains solid residue and fermented liquid.
5. solid residue combustion power generation: with embodiment 1.
6. anaerobically fermenting: with embodiment 4.
Embodiment 12
Shown in schema as shown in Figure 4, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with the pressure of 270bar, the liquid portion in straw pulp is separated by plate-and-frame filter press with solid part, the water content of solid part is about 47% ~ 55%.
4. pre fermentation: by the liquid portion after being separated first with the gene engineering yeast KE6-12(of hexose and pentose can be utilized also to be Taurus04 simultaneously, Taurusenergy company provides) be 35 DEG C in temperature, pH is pre fermentation 48h under the condition of 5.5.Containing the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in the substratum of fermentation system, the addition of KE6-12 is 3g/l.
5. simultaneous saccharification and fermentation and distillation: by after pre fermentation fermented liquid is separated together with step the solid part 3. obtained and adds in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, add the cellulase of 10FPU/g solid substance, ferment in temperature 35 DEG C, pH proceeds 96h under the condition of 5.5, obtain ethanol finally by distillation, reclaim the CO that fermentation produces
2.Separate fermentation product, obtains solid residue and fermented liquid.
6. solid residue combustion power generation: 5. step is separated the solid residue obtained and is mainly xylogen, sends into biomass power plant combustion power generation after seasoning, the electricity of production and remaining steam are used further to energy consumption required in supplementary fibre element ethanol production process.The electricity of production is used for the energy consumption that replenish step is 1. required to step production process 5., the exhaust steam of generation be used for step Steam explosion treatment 2. and step 5. in distillation.
7. anaerobically fermenting: 5. step is separated the fermented liquid obtained and is placed in fermentor tank and carries out anaerobically fermenting, collects the biogas produced.Anaerobically fermenting carries out at 55 DEG C, fermentor tank is full of nitrogen, to ensure oxygen-free environment before fermentation.Inoculum is active sludge (containing the flora needed for biogas fermentation in mud, being provided by Domsjo company of Sweden).The content gas-chromatography (Japanese Shimadzu) of methane measures.
All technical is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, yield: 22.7g/l, 14.3g ethanol/100g Dry corn stalk stalk.
Methane yield: 7.3g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Embodiment 13
Shown in schema as shown in Figure 4, maize straw following methods processes, coproduction generating while producing ethanol, biogas.
1. flood: with embodiment 2.
2. Steam explosion treatment: with embodiment 2.
3. solid-liquid separation: with embodiment 12.
4. pre fermentation: by the liquid portion after being separated first with the gene engineering yeast KE6-12(of hexose and pentose can be utilized also to be Taurus04 simultaneously, Taurusenergy company provides) be 30 DEG C in temperature, pH is pre fermentation 48h under the condition of 5.5.Containing the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in the substratum of fermentation system, the addition of KE6-12 is 3g/l.
5. simultaneous saccharification and fermentation and distillation: by after pre fermentation fermented liquid is separated together with step the solid part 3. obtained and adds in fermentor tank, the solid-liquid mass percent in fermentation system is made to be 10%, add the cellulase of 10FPU/g solid substance, ferment in temperature 30 DEG C, pH proceeds 96h under the condition of 5.5, obtain ethanol finally by distillation, reclaim the CO that fermentation produces
2.Separate fermentation product, obtains solid residue and fermented liquid.
6. solid residue combustion power generation: with embodiment 12.
7. anaerobically fermenting: with embodiment 12.
All technical is as follows:
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, the wood sugar rate of recovery: 107.7%, 101.3%.
Glucose after acetic acid,diluted preimpregnation Steam explosion treatment, xylose rate: 9.0%, 65.6%.
The furfural, the hydroxymethylfurfural that generate after acetic acid,diluted preimpregnation Steam explosion treatment: 0.19g hydroxymethylfurfural/100g Dry corn stalk stalk, 0.24g furfural/100g Dry corn stalk stalk.
Simultaneous saccharification and fermentation alcohol concn, yield: 28.2g/l, 16.9g ethanol/100g Dry corn stalk stalk.
Methane yield: 7.3g/100g Dry corn stalk stalk.
Maize straw fermentation residue calorific value: 22MJ/kg.
Methane yield in the alcohol concn of the simultaneous saccharification and fermentation step of embodiment 1-12, alcohol getting rate and anaerobically fermenting step and the contrast of Chinese patent CN101519671B are see table 1.
Table 1
Method of the present invention can make the Mierocrystalline cellulose in corn stalk, hemicellulose utilization ratio and ethanol conversion reach more than 90%.The yield of ethanol and methane is the highest can reach 16.9g ethanol/100g Dry corn stalk stalk, 11.5g methane/100g Dry corn stalk stalk.And the alcohol getting rate of method is only 12.9g/100g substrate disclosed in Chinese patent CN101519671B.On alcohol concn, the present invention is the highest can reach 49.9g/L, effectively can reduce energy consumption required in ethanol rectifying.In addition, method of the present invention also reduces the consumption of cellulase used in fermentation, the consumption of method cellulase of the present invention is 10FPU/g substrate, and the consumption in method disclosed in Chinese patent CN101519671B is up to 20FPU/g substrate, be 2 times of the consumption of method of the present invention enzyme used.
Claims (35)
1. utilize maize straw to produce a method for ethanol, biogas coproduction generating, the method comprises the following steps:
1. preimpregnation: use acid dipping for some time after corn straw smashing, described acid is acetic acid;
2. Steam explosion treatment: the maize straw of preimpregnation is placed in reactor and carries out Steam explosion treatment;
3. simultaneous saccharification and fermentation and distillation: the straw pulp formed after step 2. Steam explosion treatment is carried out simultaneous saccharification and fermentation, wherein solid-liquid mass percent is 10% ~ 20%, apply suitable genetic engineering bacterium or yeast and suitable enzyme, under suitable conditions after fermentation, distillation obtains ethanol, and reclaims the CO of fermentation generation
2, separate fermentation product, obtains solid residue and fermented liquid;
4. solid residue combustion power generation: send into biomass power plant combustion power generation after solid residue drying step 3. obtained;
5. anaerobically fermenting: fermented liquid step 3. obtained carries out anaerobically fermenting, collects the biogas produced.
2. the process of claim 1 wherein that electricity that 4. step produce is for 1. required to the step production process 3. energy consumption of replenish step, the exhaust steam of generation be used for step Steam explosion treatment 2. and step 3. in distillation.
3. the method for claim 1, wherein before carrying out step simultaneous saccharification and fermentation 3., also has the step being separated straw pulp, the straw pulp formed after step 2. Steam explosion treatment is carried out solid-liquid separation, carrying out the 3. described simultaneous saccharification and fermentation of step by being separated the solid obtained, being separated the liquid obtained and carrying out the 5. described anaerobically fermenting of step together with the fermented liquid suddenly 3. obtained.
4. the method for claim 3, wherein, by being separated before the solid that obtains carries out simultaneous saccharification and fermentation, first adding suitable enzyme and carrying out prehydrolysis, then adds suitable genetic engineering bacterium or yeast ferments.
5. the method for claim 4, wherein prehydrolysis condition is 40 ~ 50 DEG C of hydrolysis 3 ~ 5 hours.
6. the method for claim 4, wherein prehydrolysis condition is 45 DEG C of prehydrolysis 4h.
7. the method for claim 1, wherein, before carrying out step simultaneous saccharification and fermentation 3., also has the step being separated straw pulp, the straw pulp formed after step 2. Steam explosion treatment is carried out solid-liquid separation, applying suitable genetic engineering bacterium by being separated the liquid obtained, carry out the pre fermentation regular hour under suitable fermentation condition after, fermented liquid being carried out the 3. described simultaneous saccharification and fermentation of step in the lump together with being separated the solid obtained.
8. the method for claim 7, wherein, described pre-fermented fermentation condition is: be 30 DEG C ~ 35 DEG C in temperature, and pH value is under the condition of 5.0 ~ 6.0, ferments 45 ~ 50 hours.
9. the method for any one of claim 3 to 8, the step of wherein said separation straw pulp is separated by pressure filter.
10. the method for claim 9, wherein the separating pressure of pressure filter is 270bar.
The method of 11. any one of claim 1 to 8, wherein said step 1. in, the grinding mode of maize straw is that beater grinder is pulverized.
The method of 12. claims 11, wherein said step 1. in, corn stalk powder is broken to 1 ~ 5cm.
The method of 13. any one of claim 1 to 8, wherein said step 1. in, the concentration of acetic acid is 0.5 ~ 2%.
The method of 14. claims 13, wherein, the concentration of acetic acid is 1%.
The method of 15. any one of claim 1 to 8, wherein said step 1. in, described dipping is after the acid taking respective quality, after being diluted to suitable concn, then is used for soaking maize stalk with water.
The method of 16. claims 15, wherein, dipping time is 60 ~ 120 minutes.
The method of 17. any one of claim 1 to 8, wherein said step 2. in, the condition of described steam explosion reaction is: temperature 190 DEG C ~ 210 DEG C, 5 ~ 10 minutes reaction times.
The method of 18. any one of claim 1 to 8, wherein said suitable genetic engineering bacterium or the concentration of yeast are 2 ~ 4g/L, and the consumption of described suitable enzyme is 9 ~ 11FPU/g solid substance.
The method of 19. claims 18, wherein said suitable genetic engineering bacterium or the concentration of yeast are 3g/L, and the consumption of described suitable enzyme is 10FPU/g solid substance.
The method of 20. claims 1 to 8,19 any one, wherein, described suitable genetic engineering bacterium is KE6-12 bacterium, and described yeast is yeast saccharomyces cerevisiae, and described suitable enzyme is cellulase.
The method of 21. claims 18, wherein, described suitable genetic engineering bacterium is KE6-12 bacterium, and described yeast is yeast saccharomyces cerevisiae, and described suitable enzyme is cellulase.
The method of 22. claims 1 to 8,19 any one, wherein, also contains the Secondary ammonium phosphate of 0.4 ~ 0.6g/l and the magnesium sulfate of 0.02 ~ 0.03g/l in described pre fermentation system or in step simultaneous saccharification and fermentation system 3..
The method of 23. claims 18, wherein, also contains the Secondary ammonium phosphate of 0.4 ~ 0.6g/l and the magnesium sulfate of 0.02 ~ 0.03g/l in described pre fermentation system or in step simultaneous saccharification and fermentation system 3..
The method of 24. claims 1 to 8,19 any one, wherein, also contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in described pre fermentation system or in step simultaneous saccharification and fermentation system 3..
The method of 25. claims 18, wherein, also contains the Secondary ammonium phosphate of 0.5g/l and the magnesium sulfate of 0.025g/l in described pre fermentation system or in step simultaneous saccharification and fermentation system 3..
The method of 26. claims 1 to 8,19 any one, wherein, step fermentation condition is 3.: at the temperature bottom fermentation 72 ~ 120 hours of 30 DEG C ~ 35 DEG C.
The method of 27. claims 18, wherein, step fermentation condition is 3.: at the temperature bottom fermentation 72 ~ 120 hours of 30 DEG C ~ 35 DEG C.
The method of 28. claims 1 to 8,19 any one, wherein, step 3. in the separate mode of fermented liquid for be separated with pressure filter.
The method of 29. claims 18, wherein, step 3. in the separate mode of fermented liquid for be separated with pressure filter.
The method of 30. claims 28, wherein said pressure filter is plate-and-frame filter press.
The method of 31. claims 29, wherein said pressure filter is plate-and-frame filter press.
The method of 32. any one of claim 1 to 8, wherein step 4. in the drying mode of solid residue be seasoning.
The method of 33. any one of claim 3 to 8, wherein step 4. in the electricity that produces be used for 1. required to the step production process 3. energy consumption of replenish step, step 4. in the exhaust steam that produces be used for step Steam explosion treatment 2. and step 3. in distillation.
The method of 34. any one of claim 1 to 8, wherein the condition of step 5. anaerobically fermenting is oxygen-free environment; Temperature 50 ~ 60 DEG C, inoculum is active sludge.
The method of 35. claims 34, wherein said oxygen-free environment is nitrogen environment, and temperature is 55 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210211831.4A CN103509827B (en) | 2012-06-25 | 2012-06-25 | A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210211831.4A CN103509827B (en) | 2012-06-25 | 2012-06-25 | A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103509827A CN103509827A (en) | 2014-01-15 |
| CN103509827B true CN103509827B (en) | 2015-12-16 |
Family
ID=49893259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210211831.4A Active CN103509827B (en) | 2012-06-25 | 2012-06-25 | A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103509827B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111560415A (en) * | 2020-05-20 | 2020-08-21 | 华北电力大学 | Method for adjusting bacteria for biomass power generation in real time |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI125914B (en) * | 2014-09-17 | 2016-04-15 | Petteri Salonen | System and method for biomass treatment |
| CN104356663A (en) * | 2014-12-03 | 2015-02-18 | 松原光禾能源有限公司 | Preparation method of lignin thermoplastic material |
| CN104561111A (en) * | 2015-01-11 | 2015-04-29 | 北京化工大学 | Method for increasing anaerobic digestion and gas production properties by using methanation discharged material to acidify and pre-process corn straws |
| CN105506027A (en) * | 2015-12-30 | 2016-04-20 | 中国石油天然气股份有限公司 | Method for preparing saccharified liquid through low-temperature dilute acid and instant steam explosion combined biomass pretreatment |
| FR3053969B1 (en) * | 2016-07-18 | 2019-12-20 | IFP Energies Nouvelles | PROCESS OF TREATING LIGNOCELLULOSIC BIOMASS BY IMPREGNATION AND EXPLOSION WITH STEAM |
| CN107987856B (en) * | 2016-08-05 | 2020-10-30 | 国家电网公司 | Method for preparing biomass gas and active carbon and products thereof |
| CN109988782A (en) * | 2017-12-29 | 2019-07-09 | 中粮营养健康研究院有限公司 | A method of using corn and sugarcane coproduction sucrose and ethyl alcohol |
| CN108998479A (en) * | 2018-08-15 | 2018-12-14 | 山东宝力生物质能源股份有限公司 | A method of biological fuel gas is prepared using pure stalk |
| CN109504405A (en) * | 2018-11-02 | 2019-03-22 | 石首市博锐德生物科技有限公司 | The system and method for handling corn stover |
| CN111349502B (en) * | 2018-12-21 | 2021-08-06 | 中国石油化工股份有限公司 | Method for preparing formed fuel by using cellulosic ethanol rectification residues |
| CN109504724A (en) * | 2018-12-24 | 2019-03-22 | 北京鑫泽清源植物秸杆技术有限公司 | Stalk cleans co-production technology |
| CN109678988A (en) * | 2019-02-11 | 2019-04-26 | 北京鑫泽清源植物秸杆技术有限公司 | Agricultural-forestry biomass classified use and low-carbon combined production device and its green technology |
| CN110564779A (en) * | 2019-09-16 | 2019-12-13 | 华南农业大学 | Method for co-producing biogas by fermenting ethanol with bagasse-molasses mixed raw material |
| CN113674597B (en) * | 2021-09-02 | 2022-11-22 | 广东科学中心 | Interactive display device for biomass energy power generation |
| CN113943757B (en) * | 2021-11-22 | 2023-10-27 | 国网内蒙古东部电力有限公司电力科学研究院 | Method for producing biogas by combined pretreatment of wheat straw |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101392270A (en) * | 2008-11-04 | 2009-03-25 | 安徽六安市春成绿色化工有限公司 | Production process of natural gas by using paddy hull |
| CN101519671A (en) * | 2008-02-27 | 2009-09-02 | 中国科学院过程工程研究所 | Technological method for transforming fuel alcohol in stages and cogenerating electricity and paper pulp with pennisetum hydridum |
| CN101748156A (en) * | 2009-12-25 | 2010-06-23 | 陈福库 | Comprehensive utilization method of soybean straws for producing fuel ethanol, lignin and marsh gas |
-
2012
- 2012-06-25 CN CN201210211831.4A patent/CN103509827B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101519671A (en) * | 2008-02-27 | 2009-09-02 | 中国科学院过程工程研究所 | Technological method for transforming fuel alcohol in stages and cogenerating electricity and paper pulp with pennisetum hydridum |
| CN101392270A (en) * | 2008-11-04 | 2009-03-25 | 安徽六安市春成绿色化工有限公司 | Production process of natural gas by using paddy hull |
| CN101748156A (en) * | 2009-12-25 | 2010-06-23 | 陈福库 | Comprehensive utilization method of soybean straws for producing fuel ethanol, lignin and marsh gas |
Non-Patent Citations (1)
| Title |
|---|
| 蒸汽爆破预处理技术及其对纤维乙醇生物转化的研究进展;王鑫;《林产化学与工业》;20100831;第30卷(第4期);第121页2.1部分 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111560415A (en) * | 2020-05-20 | 2020-08-21 | 华北电力大学 | Method for adjusting bacteria for biomass power generation in real time |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103509827A (en) | 2014-01-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103509827B (en) | A kind of method utilizing maize straw to produce ethanol, biogas coproduction generating | |
| Ayodele et al. | An overview of integration opportunities for sustainable bioethanol production from first-and second-generation sugar-based feedstocks | |
| CN102352381B (en) | Method using xylose production waste liquid to produce acetone and butanol | |
| Velásquez-Arredondo et al. | Ethanol production process from banana fruit and its lignocellulosic residues: energy analysis | |
| Ranjan et al. | Comparative study of various pretreatment techniques for rice straw saccharification for the production of alcoholic biofuels | |
| CN101514349B (en) | Method for preparing fuel ethanol from bamboo fibers | |
| CN104774877B (en) | A kind of method of lignocellulose biomass co-producing ethanol, acetone and butanol | |
| CN101182551B (en) | Method for producing fuel alcohol through alkaline method preprocessing plant fibre | |
| CN105385724A (en) | Method for improving conversion efficiency of lignocellulose through combined treatment and method for efficiently preparing ethyl alcohol | |
| CN101392270A (en) | Production process of natural gas by using paddy hull | |
| CN104031946A (en) | Detoxification treatment-free cellulosic ethanol production method | |
| CN102766703B (en) | Hydrolysis method for hemicelluloses of lignocelluloses | |
| CN102250974A (en) | Preparation method of microbial oil | |
| CN103409470A (en) | Method for producing ethanol, butanol and acetone by utilizing segmented and mixed fermentation of mixed sugar containing pentose and hexose | |
| WO2005079190A2 (en) | Production of ethanol and high-protein feed co-products from high-solids conversion of cereal grains and legumes | |
| CN105779512B (en) | A kind of method that wood fibre waste mixed hydrolysis produces alcohol fuel | |
| CN103352057B (en) | Method for preparing fuel ethanol by taking bamboo shoot processing residues as raw materials | |
| CN102191280B (en) | Method for preparing ethanol from furfural dregs and corn through co-fermentation | |
| CN103509828B (en) | Method for preparing ethanol with manioc wastes as raw materials through synergic saccharification fermentation | |
| CN102321674B (en) | Two-phase reaction method for raising efficiency of energy grass to prepare bio-gas | |
| Yu et al. | DLCA (ch) pretreatment brings economic benefits to both biomass logistics and biomass conversion for low cost cellulosic ethanol production | |
| CN109423507A (en) | A kind of method of anaerobic-aerobic mixing fungin butanol solid state fermentation | |
| CN102465152A (en) | Cellulose ethanol internal circulation production method without pretreatment | |
| JP5953045B2 (en) | Ethanol production method using biomass | |
| CN101475976A (en) | Multi-strain combined fermentation process for preparing fuel ethanol from wood fiber |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20151118 Address after: 100031 Xicheng District West Chang'an Avenue, No. 86, Beijing Applicant after: State Grid Corporation of China Applicant after: STATE GRID ENERGY SAVING SERVICE CO., LTD. Address before: 101206 Beijing City Village Yu Meiyukou town Pinggu District Street No. 9 room 223 Applicant before: Technology R & D Center is produced in Fei Liangchun Electricity Federation, State Grid Xinyuan Co., Ltd. Beijing Applicant before: State Grid Corporation of China |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |