CN102226204B - Method for detoxifying sugar solution in lignocellulose ethanol fermentation - Google Patents
Method for detoxifying sugar solution in lignocellulose ethanol fermentation Download PDFInfo
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- CN102226204B CN102226204B CN2011101211608A CN201110121160A CN102226204B CN 102226204 B CN102226204 B CN 102226204B CN 2011101211608 A CN2011101211608 A CN 2011101211608A CN 201110121160 A CN201110121160 A CN 201110121160A CN 102226204 B CN102226204 B CN 102226204B
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000000855 fermentation Methods 0.000 title claims abstract description 22
- 230000004151 fermentation Effects 0.000 title claims abstract description 22
- 239000012528 membrane Substances 0.000 claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 238000004821 distillation Methods 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Chemical compound OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 30
- 150000003839 salts Chemical class 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- 230000002209 hydrophobic effect Effects 0.000 claims description 9
- 239000012982 microporous membrane Substances 0.000 claims description 7
- -1 polypropylene Polymers 0.000 claims description 5
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 239000002033 PVDF binder Substances 0.000 claims description 2
- 239000004698 Polyethylene Substances 0.000 claims description 2
- 229920000573 polyethylene Polymers 0.000 claims description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 2
- 239000011148 porous material Substances 0.000 claims description 2
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 6
- 238000004939 coking Methods 0.000 abstract description 3
- 239000002440 industrial waste Substances 0.000 abstract description 2
- 239000003792 electrolyte Substances 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 30
- 238000001784 detoxification Methods 0.000 description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 230000005764 inhibitory process Effects 0.000 description 13
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 12
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 9
- 230000007062 hydrolysis Effects 0.000 description 9
- 238000006460 hydrolysis reaction Methods 0.000 description 9
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- 239000011780 sodium chloride Substances 0.000 description 6
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 4
- 239000001110 calcium chloride Substances 0.000 description 4
- 229910001628 calcium chloride Inorganic materials 0.000 description 4
- 239000008103 glucose Substances 0.000 description 3
- 238000004128 high performance liquid chromatography Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- JOOXCMJARBKPKM-UHFFFAOYSA-N 4-oxopentanoic acid Chemical compound CC(=O)CCC(O)=O JOOXCMJARBKPKM-UHFFFAOYSA-N 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000007781 pre-processing Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- NOEGNKMFWQHSLB-UHFFFAOYSA-N 5-hydroxymethylfurfural Chemical compound OCC1=CC=C(C=O)O1 NOEGNKMFWQHSLB-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 229920002488 Hemicellulose Polymers 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000036983 biotransformation Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012262 fermentative production Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- RJGBSYZFOCAGQY-UHFFFAOYSA-N hydroxymethylfurfural Natural products COC1=CC=C(C=O)O1 RJGBSYZFOCAGQY-UHFFFAOYSA-N 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229940040102 levulinic acid Drugs 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 239000012978 lignocellulosic material Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 235000009973 maize Nutrition 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000002798 spectrophotometry method Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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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
- Y02E50/10—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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses a method for detoxifying a sugar solution in lignocellulose ethanol fermentation, comprising the steps of: adding soluble electrolyte into the sugar solution to be processed, followed by heating to obtain a constant-temperature raw material liquid; letting the constant-temperature raw material liquid pass through a membrane module for membrane distillation; removing substances which inhibit the subsequent fermentation process from the sugar solution while trying not to minimize effective sugar components. The method provided by the invention requires short operation time and low temperature, and low-quality industrial waste heat and other economical heat sources can be directly used, thus achieving the purpose of saving energy and reducing cost; simultaneously, the coking of sugar in the solution will not happen.
Description
Technical field
The invention belongs to lignocellulosic material biological degradation and bio-transformation production alcohol fuel and other derivative fields in the biological chemistry, be specifically related to a kind of improved film distillation technology as the method for lignocellulose raw material hydrolysis sugar liquid detoxification.
Background technology
Energy dilemma aggravation impels the fast development of biofuel, and wherein bio-ethanol is subject to people and more and more pays close attention to.And being raw material production ethanol, lignocellulose comprises three large steps: pre-treatment, hydrolysis and fermentation.The final purpose of pre-treatment and hydrolysis is carbohydrate polymer in the degrading plant cell walls, and making it to become can be by the low molecular sugar of production of ethanol from microbial fermentation.In various preprocessing method of raw materials, dilute acid pretreatment and steam explosion pretreatment process generally are considered to comparatively effective.In various preprocessing process, because degraded occurs in heat or sour effect, part Mierocrystalline cellulose, hemicellulose and xylogen and Decomposition generation formic acid, acetic acid, levulinic acid, furfural, hydroxymethylfurfural and phenolic compound etc. have inhibiting material to follow-up fermentation.Inhibition raises along with pretreatment temperature and the prolongation in treatment time and increasing, and the produced simultaneously amount also kind with lignin material is relevant, and these materials must detoxification removal before fermenting.
The poison-removing method of hydrolysis sugar liquid mainly contains charcoal absorption, lime neutralization, ion-exchange, vacuum concentration stripping at present, organic solvent extraction etc., but these methods exist that detoxification efficiency is poor, cost is high, complex operation or the shortcoming such as sugar loss is large when fermentation inhibitor removes.Therefore, the lignocellulose ethanol industry is badly in need of the good poison-removing method of a kind of detoxification efficiency.
Membrane distillation is that a kind of dewatering microporous film that adopts is take the poor membrane sepn process as the mass transfer motivating force of film both sides vapor pressure.When the solution temperature of film both sides not simultaneously, the water vapor pressure of the hot side aqueous solution and membrane interface is higher than cold side, water vapor will see through fenestra enter cold side and condensation.Also remove by the method for hot side vaporization, cold side condensation for volatile organic inhibition.
Summary of the invention
The invention provides a kind of poison-removing method of effective sugar solution in lignocellulose ethanol fermentation, in removing liquid glucose, follow-up fermentation produced inhibiting material in, do not reduce effective sugar component as far as possible.
A kind of poison-removing method of sugar solution in lignocellulose ethanol fermentation adds solubility electrolytic salt post-heating and obtains the constant temperature stock liquid in pending liquid glucose, the constant temperature stock liquid is carried out membrane distillation by membrane module.
Because film itself does not have selectivity in the membrane distillation process, just play an effect of separating cold fluid and hot fluid, therefore the present invention adds the vapour pressure that the solubility electrolytic salt optionally changes inhibition in separated system, improve the relative volatility of inhibition, make organic inhibition more see through film and condensation, thereby reach higher inhibition clearance.The trace soluble electrolytic salt that adds is that follow-up fermentation there is not impact or even a favourable class material, so can not affect the yield of ethanol.
Described pending liquid glucose refers to the prehydrolysis liquid glucose of lignocellulose fermentative production of ethanol process Raw.
Described solubility electrolytic salt and water have certain binding ability, can change acetic acid with respect to the relative volatility of water, thereby can improve acetic acid in the concentration that sees through side, pay the utmost attention to the salt that needs interpolation in the fermention medium of downstream, such as preferred CaCl
2, NaCl or (NH
4)
2SO
4
Described solubility electrolytic salt add-on is 0.5%～5% of liquid glucose quality.For the hydrolysis sugar liquid that different pretreatments obtains, inhibition concentration is slightly different, sets out according to inhibition removal situation and cost-effective angle, and preferred solubility electrolytic salt add-on is 0.5%～2% of liquid glucose quality.
From preventing sugared coking and considering that from Energy Angle the temperature of described constant temperature stock liquid optimum is 50 ℃～70 ℃.
Described membrane module preferably adopts hydrophobic microporous membrane, and the optimum strong microporous membrane of hydrophobicity that adopts is such as polyvinylidene fluoride dewatering microporous film, tetrafluoroethylene dewatering microporous film, hydrophobic polypropylene microporous membrane or polyethylene dewatering microporous film.Preferred 0.1～1.0 μ m of described hydrophobic micropore membrane pore size.
Flow through under the effect of feedstock pump valve and under meter of the stock liquid of constant temperature enters the tube side of membrane module, carries out mass transfer, heat transfer on the film surface, oozes remaining sugar soln by concentrate and detoxification, is circulated back in the head tank in the thermostatic bath.Be evacuated to condenser system condensation in per-meate side by vacuum pump and see through water vapor and the volatile organic inhibition that fenestra enters the membrane module shell side, after condenser condenses, be collected in the water tank.The sugar soln continuous circulation of hot side, its organic inhibition that contains constantly is removed, reach preset requirement after, obtain the sugar soln after the detoxification.
The membrane distillation process is conventional membrane distillation process, and downstream general vacuum type, direct contact type, GAP TYPE or the gas that the adopts formula of sweeping realizes condensation, and the present invention preferably adopts vacuum type to realize.The membrane module feed side is for necessarily being heated to the constant temperature stock liquid of constant temperature, seeing through side is vacuum state, water in the constant temperature stock liquid and volatile components (inhibition) from constant temperature stock liquid main diffusion to contacted frictional belt, dewatering microporous film surface, and the interface in frictional belt and the formation of film surface is vaporizated into steam, steam diffuses to per-meate side by dewatering microporous film and solution can not see through hydrophobic membrane and is trapped, and the steam that sees through film is evacuated to the condenser system condensation by vacuum pump.The impellent of this process is the steam pressure difference that film both sides temperature head causes, water and volatile components constantly are removed by the circulation of hot side, thereby realizes the concentrated and detoxification purpose of liquid glucose.
The present invention have the operating time short, temperature is low, can directly utilize low-grade industrial waste heat and other economic thermals source, realizes save energy, reduces the purpose of cost, coking phenomenon can not occur in the sugar in the solution simultaneously.
Description of drawings
Fig. 1 is the vacuum membrane distillation device of liquid glucose detoxification;
Among the figure: 1 head tank; 2 thermals source; 3 feedstock pumps; 4 valves; 5 spinner-type flowmeters; 61 thermometers; 62 thermometers; 7 membrane modules; 81 condensers; 82 condensers; 9 receiving flasks; 10 circulating water type vacuum pumps
Fig. 2 is for adding CaCl
2Impact on acetic acid and furfural clearance;
Fig. 3 is for adding NaCl to the impact of acetic acid and furfural clearance;
Fig. 4 is Angel wine brewing high-activity yeast to the ethanol fermentation course of detoxification prehydrolysis liquid glucose not;
Fig. 5 is that wine brewing high-activity yeast in Angel is to the ethanol fermentation course of detoxification prehydrolysis liquid glucose.
Embodiment
The pending liquid glucose that the embodiment of the invention is selected is that the raw material maize straw adopts the pre-and enzymolysis processing technique acquisition hydrolysis sugar liquid of steam explosion, main sugar component before and after the membrane distillation adopts determined by ultraviolet spectrophotometry, and fermentation inhibitor adopts high performance liquid chromatography (HPLC) analysis.The main component of pending liquid glucose is as shown in table 1.
The pending liquid glucose main component of table 1
The membrane module that adopts is single tubular fibre formula assembly, and used film is the hydrophobic polypropylene microporous membrane, and the aperture is 0.15 μ m, and membrane area is about 0.08m
2, the vacuum type operation is adopted in the downstream.Be described in detail different salt concn to the situation that affects of liquid glucose detoxification efficiency below in conjunction with technical scheme and accompanying drawing.
Embodiment 1
Adopt as shown in Figure 1 device.Get pending liquid glucose 400ml in head tank 1, add respectively the solid CaCl of different mass mark
2Add-on is 0.5% of liquid glucose quality, 1%, 2% and 5%, be heated to 60 ℃ of constant temperature by thermal source 2, open feedstock pump 3, the constant temperature stock liquid is through valve 4 and spinner-type flowmeter 5, stock liquid enters membrane module 7 with the flow velocity of 0.5～2m/s, and the membrane module inlet and outlet is equipped with thermometer 61 and 62, can measure the temperature that enters assembly and flow out the assembly liquid glucose.Liquid glucose flows back into behind the mass-and heat-transfer in membrane module in the head tank 1 in the thermal source.(vacuum tightness 0.090～0.095MPa) is collected in the water tank 9 after condenser 8 condensations, and 81 and 82 is respectively import and the outlet of water coolant and the steam that sees through fenestra is aspirated by vacuum pump 10.After certain hour (60min) was carried out in operation, the HPLC analysis was carried out in sampling in head tank 1.The result as shown in Figure 2.
As can be seen from Figure 2, the rejection of glucose can both remain on more than 99.5%, and effectively the sugar component loss is considerably less; The maximum material removal rate of main inhibition acetic acid and furfural is respectively 58.3% and 87.4%, and with CaCl
2The rising of concentration slightly raises, and this is because the reactive force between calcium chloride and the water is far longer than the reactive force between calcium chloride and the acetic acid, has reduced the vapour pressure of water, has always improved the relative volatility of acetic acid with respect to water.The amount of adding calcium chloride is larger, and the degree that relative volatility improves is also larger, but considers in the fermenting process to the inorganic ion demand CaCl of interpolation
2Add-on is 0.5%～2% of liquid glucose quality.。
Equipment therefor as shown in Figure 1.Water intaking is separated liquid glucose 400ml in head tank 1, the solid NaCl that adds respectively the different mass mark, add-on is 0.5%, 1%, 2% and 5% of liquid glucose quality, be heated to 60 ℃ of constant temperature by thermal source 2, open feedstock pump 3, the constant temperature stock liquid is through valve 4 and spinner-type flowmeter 5, and stock liquid enters membrane module 7 with the flow velocity of 0.5～2m/s, the assembly inlet and outlet is equipped with thermometer 61 and 62, can measure the temperature that enters assembly and flow out the assembly liquid glucose.Liquid glucose flows back into the head tank in the thermal source behind the mass-and heat-transfer in membrane module.(vacuum tightness 0.090～0.095MPa) is collected in the water tank 9 after condenser 8 condensations, and 81 and 82 is respectively import and the outlet of water coolant and the steam that sees through fenestra is aspirated by vacuum pump 10.After certain hour (60min) was carried out in operation, the HPLC analysis was carried out in sampling in head tank.The result as shown in Figure 3.
As can be seen from Figure 3, the rejection of glucose can both remain on more than 99.5%; The maximum material removal rate of main inhibition acetic acid and furfural is respectively 50.4% and 83.8%, and slightly raises with the rising of NaCl concentration, but compares with interpolation calcium chloride, reach identical clearance, and the NaCl concentration that needs to add is greater than CaCl
2Concentration.This shows, NaCl improve acetic acid to the relative volatility degree of water on effect not as good as CaCl
2
Compare detoxification efficiency
For detoxification efficiency relatively, with the comparison of fermenting of the hydrolysis sugar liquid before and after the detoxification.Yeast adopts commercial Angel wine brewing high-activity yeast, fermention medium (L) composed as follows: 0.2g MgSO
4, 2g KH
2PO
4, 2g (NH
4)
2SO
4, 0.2g CaCl
2, the 2g yeast powder.Fermentation condition is, 35 ℃, and 150r/min, the fermentation situation is as shown in Figure 4 and Figure 5.
As can be seen from Figure 4, wine brewing high-activity yeast in Angel is to the hydrolysis sugar liquid fermentation of not detoxification, and in 12～24h, alcohol concn maintains between 9.25～18.80g/L, and the utilization ratio of glucose is the highest only has 49%, illustrates that the fermentation efficiency of detoxification hydrolyzed solution is not high.And Fig. 5 to be the hydrolysis sugar liquid of wine brewing high-activity yeast in Angel after to detoxification (add 2weight%CaCl
2) the fermentation course, alcohol concn reaches 41.71g/L when 24h, and sugared utilization ratio and alcohol getting rate are respectively 97.28% and 90.72%.Contrasting two figure can find out, pending liquid glucose is after the membrane distillation detoxification, and its ethanol fermentation performance is greatly improved.
Claims (6)
1. the poison-removing method of a sugar solution in lignocellulose ethanol fermentation is characterized in that: add solubility electrolytic salt post-heating and obtain the constant temperature stock liquid in pending liquid glucose, the constant temperature stock liquid is carried out membrane distillation by membrane module;
Described solubility electrolytic salt is CaCl
2, add-on is 0.5%～5% of liquid glucose quality; The temperature of described constant temperature stock liquid is 50 ℃～70 ℃.
2. poison-removing method as claimed in claim 1, it is characterized in that: described solubility electrolytic salt add-on is 0.5%～2% of liquid glucose quality.
3. poison-removing method as claimed in claim 1 is characterized in that: described membrane module employing hydrophobic microporous membrane.
4. poison-removing method as claimed in claim 3, it is characterized in that: described hydrophobic microporous membrane is polyvinylidene fluoride dewatering microporous film, tetrafluoroethylene dewatering microporous film, hydrophobic polypropylene microporous membrane or polyethylene dewatering microporous film.
5. poison-removing method as claimed in claim 4, it is characterized in that: described hydrophobic micropore membrane pore size is 0.1～1.0 μ m.
6. poison-removing method as claimed in claim 1 is characterized in that: described membrane distillation downstream employing vacuum type realization condensation.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101270372A (en) * | 2008-04-15 | 2008-09-24 | 中国石油化工股份有限公司 | Concentration method for sugar liquid in cellulose alcoholic fermentation |
| CN101691587A (en) * | 2009-10-15 | 2010-04-07 | 南京林业大学 | Detoxification method of wood fibre hydrolysis sugar liquid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101270372A (en) * | 2008-04-15 | 2008-09-24 | 中国石油化工股份有限公司 | Concentration method for sugar liquid in cellulose alcoholic fermentation |
| CN101691587A (en) * | 2009-10-15 | 2010-04-07 | 南京林业大学 | Detoxification method of wood fibre hydrolysis sugar liquid |
Non-Patent Citations (2)
| Title |
|---|
| 王许云等.膜蒸馏技术最新研究现状及进展.《化工进展》.2007,第26卷(第2期),168-172、179. |
| 膜蒸馏技术最新研究现状及进展;王许云等;《化工进展》;20070228;第26卷(第2期);168-172、179 * |
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