CN103243023B - Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof - Google Patents
Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof Download PDFInfo
- Publication number
- CN103243023B CN103243023B CN201310165238.5A CN201310165238A CN103243023B CN 103243023 B CN103243023 B CN 103243023B CN 201310165238 A CN201310165238 A CN 201310165238A CN 103243023 B CN103243023 B CN 103243023B
- Authority
- CN
- China
- Prior art keywords
- fermentation
- enzymatic hydrolysis
- fermentor tank
- filtration membrane
- membrane separation
- 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.)
- Expired - Fee Related
Links
- 238000000855 fermentation Methods 0.000 title claims abstract description 83
- 230000004151 fermentation Effects 0.000 title claims abstract description 83
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 230000007071 enzymatic hydrolysis Effects 0.000 title claims abstract description 35
- 238000006047 enzymatic hydrolysis reaction Methods 0.000 title claims abstract description 35
- 239000010902 straw Substances 0.000 title claims abstract description 32
- 239000000446 fuel Substances 0.000 title claims abstract description 28
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 8
- 239000000919 ceramic Substances 0.000 claims abstract description 49
- 239000012528 membrane Substances 0.000 claims abstract description 45
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims abstract description 43
- 238000004821 distillation Methods 0.000 claims abstract description 38
- 108090000790 Enzymes Proteins 0.000 claims abstract description 23
- 102000004190 Enzymes Human genes 0.000 claims abstract description 23
- 238000000926 separation method Methods 0.000 claims abstract description 23
- 230000001954 sterilising effect Effects 0.000 claims abstract description 20
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 18
- 239000001913 cellulose Substances 0.000 claims abstract description 11
- 229920002678 cellulose Polymers 0.000 claims abstract description 11
- 238000004659 sterilization and disinfection Methods 0.000 claims abstract description 6
- 238000001914 filtration Methods 0.000 claims description 44
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 claims description 34
- 108010059892 Cellulase Proteins 0.000 claims description 33
- 229940106157 cellulase Drugs 0.000 claims description 33
- 239000007788 liquid Substances 0.000 claims description 25
- 239000000843 powder Substances 0.000 claims description 23
- 229940088598 enzyme Drugs 0.000 claims description 22
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 20
- 238000013019 agitation Methods 0.000 claims description 19
- 239000000706 filtrate Substances 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 11
- 150000003384 small molecules Chemical class 0.000 claims description 11
- 229910001220 stainless steel Inorganic materials 0.000 claims description 10
- 239000010935 stainless steel Substances 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 238000002203 pretreatment Methods 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 6
- 239000006052 feed supplement Substances 0.000 claims description 6
- 241000233866 Fungi Species 0.000 claims description 5
- 230000031018 biological processes and functions Effects 0.000 claims description 5
- 230000015556 catabolic process Effects 0.000 claims description 5
- 238000006731 degradation reaction Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 229920005610 lignin Polymers 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 239000011148 porous material Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 17
- 238000004064 recycling Methods 0.000 abstract description 3
- 238000004887 air purification Methods 0.000 abstract description 2
- 150000001413 amino acids Chemical class 0.000 abstract description 2
- 238000010907 mechanical stirring Methods 0.000 abstract 3
- 239000003242 anti bacterial agent Substances 0.000 abstract 1
- 229940088710 antibiotic agent Drugs 0.000 abstract 1
- 238000012544 monitoring process Methods 0.000 abstract 1
- 238000003756 stirring Methods 0.000 abstract 1
- 240000008042 Zea mays Species 0.000 description 4
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 4
- 240000007594 Oryza sativa Species 0.000 description 3
- 235000007164 Oryza sativa Nutrition 0.000 description 3
- 240000006394 Sorghum bicolor Species 0.000 description 3
- 235000015505 Sorghum bicolor subsp. bicolor Nutrition 0.000 description 3
- 235000011684 Sorghum saccharatum Nutrition 0.000 description 3
- 238000005520 cutting process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 235000009566 rice Nutrition 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 2
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 2
- 235000005822 corn Nutrition 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000008236 heating water Substances 0.000 description 2
- 235000009973 maize Nutrition 0.000 description 2
- 230000002572 peristaltic effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 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 1
- 229920002488 Hemicellulose Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000012262 fermentative production Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 210000005253 yeast cell Anatomy 0.000 description 1
Images
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
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and a reaction method thereof. The reactor comprises a mechanical stirring fermentation tank, an air purification device, a steam generation device, a temperature control system, a distillation tower, a lower computer control system, an upper computer monitoring system, a speed regulator, a stirring motor, and a pressure pump, as well as a ceramic ultrafiltration membrane separation device, wherein the upper end of the ceramic ultrafiltration membrane separation device is connected with a return port at the upper end of the mechanical stirring fermentation tank, and the lower end of the ceramic ultrafiltration membrane separation device is connected with a fermentation residue discharge outlet at the lower end of the mechanical stirring fermentation tank through the pressure pump. The reactor integrates sterilization, enzymatic hydrolysis and fermentation, thus not only being used for production of synchronous straw enzymatic hydrolysis fermentation fuel ethanol, but also being used for production of fuel ethanol through step-by-step straw enzymatic hydrolysis and fermentation technique; the recycling of cellulose and yeast can be realized by adopting the ceramic ultrafiltration membrane separation device; and the reactor not only can be used for production of the straw enzymatic hydrolysis fermentation fuel ethanol, but also can be used for fermentation production of antibiotics, amino acids, enzymes and other biological products.
Description
Technical field
The invention belongs to microorganism fermentation equipment technical field, relate to a kind of take stalk as raw material, adopt synchronous enzymatic hydrolysis and fermentation technique, can reuse integrated reactor and the reaction method thereof of the fermented liquid production alcohol fuel that contains cellulase, zytase and yeast.
Background technology
Take reproducible straw refuse as raw material, adopt microbial fermentation technology to produce alcohol fuel, become and alleviated China's energy dilemma, comprehensive utilization straw refuse, ensures the grand strategy measure of energy security.But also do not form at present extensive, suitability for industrialized production, chief reason is exactly that production cost is too high.The technique of utilizing cellulose raw producing and ethanol in stalk take maize straw as representative generally comprises pre-treatment, enzymolysis and three steps of fermentation.Wherein enzymolysis is mainly that hydrocellulose and hemicellulose decompose saccharogenesis, and fermentation mainly changes into alcohol by sugar.At present, the enzymolysis of stalk accounts for 60% left and right in whole Fuel Ethanol Production Cost, is simplified apparatus, shortens the production cycle, often adopts synchronous enzymatic hydrolysis and fermentation (SSF) processing method.The method is that cellulase and suitable yeast are placed on and in same container, carry out continuously cellulosic enzymolysis and fermentation.This technological advantage has reduced the feedback inhibition of glucose, has improved spirit yield and production efficiency.How improving the utilization ratio of cellulase and yeast, is further to improve the efficiency of synchronous enzymatic hydrolysis and fermentation and the output of ethanol, reduces the consumption of cellulase and yeast, reduces the key of alcohol production cost.And research and develop suitable reactor (patent of invention ZL200680034205.5, cellulose materials is converted into the method and apparatus of ethanol, mention the importance of reactor), trying to explore for producing fuel ethanol using stalk material industrialization advances to make, is one of this technical field scientific research personnel urgent problem.
Traditional synchronous enzymatic hydrolysis and fermentation reactor adopts mechanical stir-reactor mostly, cellulase and yeast and stalk are once thrown in simultaneously, after fermentation ends, residual cellulose enzyme is emitted together with fermentation residue with yeast, cause the waste of cellulase and yeast, do not given full play to the utilising efficiency of enzyme and yeast.And the consumption cost of cellulase accounts for the more than 70% of enzymatic hydrolysis and fermentation cost.
Summary of the invention
For the problems referred to above that in synchronous enzymatic hydrolysis and fermentation process in prior art, reactor exists, for solving the abundant recycle problem of mixed bacteria liquid of rich cellulose enzyme and yeast, the invention provides that a kind of technique is simple, the significant circulating integrated reactor of effect and reaction method thereof.
Technical scheme of the present invention is:
The synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor, comprise 50～100000L mechanical agitation type fermentor tank, air cleaning unit, steam generation device, temperature controlling system, distillation tower, lower computer Controlling System, Monitor Computer Control System, sensor and instrumental system, speed regulator and agitator motor, supporting piping system and valve, 0.098MPa～4.0MPa pressure pump, the upper end of described mechanical agitation type fermentor tank is provided with opening for feed and feedback outlet, and lower end is provided with fermentation residue relief outlet; It is characterized in that: also comprise Ceramic excessive filtration membrane separation unit, the upper end of described Ceramic excessive filtration membrane separation unit is connected with the feedback outlet of mechanical agitation type fermentor tank upper end, lower end is connected with the fermentation residue relief outlet of mechanical agitation type fermentor tank lower end through pressure pump.
As a further improvement on the present invention, also comprise 30 × 30～500 × 500mm fie screen, described fie screen is arranged at the fermentation residue relief outlet place of mechanical agitation type fermentor tank lower end.
As a further improvement on the present invention, described Ceramic excessive filtration membrane separation unit is made up of the tubular type zirconia ceramics ultra-filtration membrane of 1～10 Φ 50 × 5500, and the membrane pore size of ceramic super-filtering film is 0.05 μ m～10 μ m.
As a further improvement on the present invention, described Ceramic excessive filtration membrane separation unit is wholy set in stainless steel tube.
As a further improvement on the present invention, described fermentation residue relief outlet place is provided with upper flange and lower flange, and described fie screen is arranged at upper and lower flange connections or is arranged in upper flange.
A reaction method for the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor, specifically comprises the following steps:
(1) pulverize: stalk is pulverized, be screened into straw powder;
(2) biological process pre-treatment: straw powder is carried out lignin degradation processing through white-rot fungi;
(3) sterilizing: pack straw powder into the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor and carry out high-temperature sterilization processing;
(4) double enzymes saccharification, fermentation: spray the mixing solutions of cellulase, zytase and yeast saccharomyces cerevisiae downwards from fermentor tank top, residual sugar finishes fermentation while no longer variation;
(5) filtering fermentation liquor: pass into aseptic compressed air from fermentor tank top, the fermented liquid that contains cellulase and yeast after preliminary filtration of fie screen of pot bottom, is discharged from fermentation residue relief outlet by fermentation;
(6) Ceramic excessive filtration membrane sepn: the fermented liquid of discharging from fermentor tank bottom is through pressure pump, squeeze into the pipeline that zirconia ceramics ultra-filtration membrane is housed, separate with micromolecular through macromole, small molecules ethanol is through the micropore of ceramic super-filtering film inside and side, lower outlet by membrane separation unit is discharged in alcohol distillation tower, and the macromole cellulase, zytase and the yeast refluxing that have not utilized are in fermentor tank;
(7) feed supplement double enzymes saccharification, fermentation: add straw powder from opening for feed, under the effect of the fermented liquid of rich cellulose enzyme, zytase and yeast, substratum continues enzymolysis and becomes reducing sugar, is fermented into alcohol;
(8) distillation: filtrate flows into alcohol distillation tower, chuck heats up, distillation;
(9) deslagging: after fed-batch fermentation, separate through the pipeline of pressure pump and ceramic super-filtering film, small molecules filtrate is discharged to distillation tower distillation, and residual macromole cellulase and yeast refluxing, in fermentor tank, are utilized again; Fermentation residue is discharged through fermentor tank bottom.
As a further improvement on the present invention, the air flow of described mechanical agitation type fermentor tank is stabilized in 0.1～3
; When fermentor tank sterilizing, keep tank pressure 0.11～0.12MPa, when cooling, keep tank pressure 0.03～0.05MPa; Air cleaning unit air flow 10～500L/min, pressure 0.25～0.8MPa; The steam research on maximum utilized quantity of steam generation device is 10kg/h, pressure 0.25～0.85MPa, low-pressure steam pressure 0.16～0.5 MPa.
The invention has the beneficial effects as follows:
(1) this reactor integrates sterilizing, enzymolysis and ferments, and both can be used for the production of the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk, also can be used for stalk substep enzymolysis, zymotechnique production alcohol fuel.Greatly improve plant factor.
(2) this reactor has adopted Ceramic excessive filtration membrane separation unit, can realize the iterative cycles utilization of cellulase, yeast, greatly reduces the consumption of enzyme and yeast, saves production cost, and enhances productivity.
(3) this reactor not only can be for the production of stalk enzymatic hydrolysis and fermentation alcohol fuel, but also can be used for the fermentative production of the biological products such as microbiotic, amino acid, enzyme.
Accompanying drawing explanation
Fig. 1 is the structural representation of the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk of the present invention loop reactor.
In figure: 1, mechanical agitation type fermentor tank; 2, air cleaning unit; 3, steam generation device; 4, distillation tower; 5, lower computer Controlling System; 6, Monitor Computer Control System; 7, speed regulator; 8, agitator motor; 9, pressure pump; 10, opening for feed; 11, feedback outlet; 12, fermentation residue relief outlet; 13, Ceramic excessive filtration membrane separation unit; 14, fie screen; 15, stainless steel tube; 16, upper flange; 17, lower flange; 18, heating water tank; 19, peristaltic pump; 20, chuck; 21, pH transmitter; 22, DO transmitter.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
The structure of the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk of the present invention loop reactor as shown in Figure 1, mainly comprise: 50～100000L mechanical agitation type fermentor tank 1, air cleaning unit 2, Ceramic excessive filtration membrane separation unit 13, steam generation device 3, comprise the temperature controlling system of heating water tank 18, distillation tower 4, lower computer Controlling System 5, Monitor Computer Control System 6 and supporting piping system, valve, sensor and instrumental system, be arranged at the junction of upper flange 16 and lower flange 17 or be arranged at the stainless steel fie screen 14 in upper flange, speed regulator 7 and agitator motor 8, 0.098MPa～4.0MPa pressure pump 9, peristaltic pump 19, the chuck 20 at mechanical agitation type fermentor tank 1 outer wall place, pH transmitter 21 and DO transmitter 22 etc.The upper end of mechanical agitation type fermentor tank 1 is provided with opening for feed 10 and feedback outlet 11, lower end is provided with fermentation residue relief outlet 12, the upper end of Ceramic excessive filtration membrane separation unit 13 is connected with the feedback outlet 11 of mechanical agitation type fermentor tank 1 upper end, and lower end is connected with the fermentation residue relief outlet 12 of mechanical agitation type fermentor tank 1 lower end.
Loop reactor disclosed by the invention has adopted 30 × 30mm～500 × 500mm stainless steel fie screen to carry out initial filter to fermented liquid in fermentor tank bottom, by 0.098MPa～4.0MPa pressure pump, squeeze into Φ 50 × 5500mm tubular type zirconia ceramics ultra-filtration membrane device filter, this ultra-filtration membrane has holds back yeast cell and macromolecular ability from fermented liquid, small molecules ethanol and fermented liquid enter in alcohol distillation tower by ceramic super-filtering film, and macromole cellulase, zytase and the yeast refluxing of holding back continues to use in fermentor tank.It is 0.05～10 μ m that this ultra-filtration membrane membrane pore size requires, and pressure requires to remain on 0.05～0.5MPa.Ceramic super-filtering film separator tube 13 is wholy set in stainless steel tube 15.
Stainless steel fie screen is installed on the centre of fermentor tank submerged fermentation sludge discharge tube upper flange 16 and lower flange 17 junctions or is arranged on 16 li of the upper flanges of lower upper flange, is convenient to dismounting, cleans and changes.Zirconia ceramics ultra-filtration membrane device is directly positioned in stainless steel tube, rotates stainless steel tube upper valve, can take out or placing ceramic ultra-filtration membrane.
The air flow of mechanical agitation type fermentor tank disclosed by the invention should be stabilized in 0.1～3
.When fermentor tank sterilizing, keep tank pressure 0.11～0.12MPa, when cooling, keep tank pressure 0.03～0.05MPa; Air-purification system requires air flow 10～500L/min, pressure 0.25～0.8MPa.It is 10kg/h that steam generating system requires steam research on maximum utilized quantity (sterilizing is used), pressure 0.25～0.85MPa, low-pressure steam pressure (purify and use) 0.16～0.5 MPa.
Ferment filtrate flows into after alcohol distillation tower, and chuck heats up, and holding temperature is 85～90 ℃, distills out alcohol.
Stalk through pre-treatment, sterilising treatment, two enzyme enzymatic hydrolysis and fermentation, fermented liquid and alcohol through ultra-filtration membrane separate, fermented liquid recycling, alcohol distillation, feed supplement enzymatic hydrolysis and fermentation again, membrane sepn, fermented liquid recycling, alcohol redistillation, row's residue, cyclic production.The method can make the bacterium liquid recycle of rich cellulose enzyme and yeast, reduces the consumption of cellulase and yeast, reduces production costs, and improves alcohol getting rate.Waste residue after fermentation can also be through processing again, is produced into the required protein fodder of livestock industry.
In order further to set forth related material and the technique of technical scheme of the present invention, provided following examples, but these embodiment do not limit the scope of the invention in any form.
Embodiment 1:
(1) pulverize: after fresh broomcorn straw is cleaned, with hay cutter cutting or pulverize with beater grinder, be screened into the straw powder of 40mm, moisture control is below 55%.
(2) biological process pre-treatment: broomcorn straw powder carries out lignin degradation processing through white-rot fungi.
(3) sterilizing: pack broomcorn straw powder into circulating integrated reactor and carry out high-temperature sterilization, 121 ℃, 30min sterilising treatment.
(4) double enzymes saccharification, fermentation: the mixing solutions that sprays cellulase, zytase and yeast saccharomyces cerevisiae from fermentor tank top downwards, the add-on of the active cellulase for 1000IU/g is 1.5% of stalk weight, activity is that the yeast saccharomyces cerevisiae add-on of 6,000,000,000/g is 1% of stalk weight, the add-on of water is 2.5 times of straw powder weight, enzymolysis, leavening temperature are controlled at 37 ℃, pH is 4.5, and mixing speed is controlled at 30rpm; 2.5 days enzymatic hydrolysis and fermentation total times, residual sugar finishes fermentation while no longer variation.
(5) filtering fermentation liquor: pass into aseptic compressed air from fermentor tank top, the fermented liquid that contains cellulase and yeast after preliminary filtration of fie screen of pot bottom, is discharged from fermentation residue relief outlet by fermentation;
(6) Ceramic excessive filtration membrane sepn: the fermented liquid of discharging from fermentor tank bottom is through pressure pump, squeeze into the pipeline that zirconia ceramics ultra-filtration membrane is housed, separate with micromolecular through macromole, small molecules ethanol is through the micropore of ceramic super-filtering film inside and side, lower outlet by membrane separation unit is discharged in alcohol distillation tower, and the macromole cellulase, zytase and the yeast refluxing that have not utilized are in fermentor tank.
(7) feed supplement double enzymes saccharification, fermentation: add a certain amount of straw powder from opening for feed, under the effect of the fermented liquid of rich cellulose enzyme, zytase and yeast, substratum continues enzymolysis and becomes reducing sugar, is fermented into alcohol.
(8) distillation: filtrate flows into alcohol distillation tower, chuck heats up, and temperature is 88 ℃, distillation, alcohol getting rate reaches 8.5%.
(9) deslagging: fed-batch fermentation is after 2.5 days, and after the pipeline of pressure pump and ceramic super-filtering film separates, small molecules filtrate is discharged to distillation tower distillation, and residual macromole cellulase and yeast refluxing, in fermentor tank, can utilize again.Fermentation residue is discharged through fermentor tank bottom.
Embodiment 2:
(1) pulverize: after fresh maize straw is cleaned, with hay cutter cutting or pulverize with beater grinder, be screened into the straw powder of 30mm, moisture control is 50%.
(2) biological process pre-treatment: corn stalk powder carries out lignin degradation processing through white-rot fungi.
(3) sterilizing: pack corn stalk powder into circulating integrated reactor and carry out high-temperature sterilization, 121 ℃, 30min sterilising treatment.
(4) double enzymes saccharification, fermentation: the mixing solutions that sprays cellulase, zytase and yeast saccharomyces cerevisiae from fermentor tank top downwards, the add-on of the active cellulase for 1000IU/g is 2% of stalk weight, activity is that the yeast saccharomyces cerevisiae add-on of 8,000,000,000/g is 0.8% of stalk weight, the add-on of water is 2.5 times of straw powder weight, enzymolysis, leavening temperature are controlled at 38 ℃, pH is 4.5, and mixing speed is controlled at 40rpm; 3 days enzymatic hydrolysis and fermentation total times, residual sugar finishes fermentation while no longer variation.
(5) filtering fermentation liquor: pass into aseptic compressed air from fermentor tank top, the fermented liquid that contains cellulase and yeast after preliminary filtration of fie screen of pot bottom, is discharged from fermentation residue relief outlet by fermentation;
(6) Ceramic excessive filtration membrane sepn: the fermented liquid of discharging from fermentor tank bottom is through pressure pump, squeeze into the pipeline that zirconia ceramics ultra-filtration membrane is housed, separate with micromolecular through macromole, small molecules ethanol is through the micropore of ceramic super-filtering film inside and side, lower outlet by membrane separation unit is discharged in alcohol distillation tower, and the macromole cellulase, zytase and the yeast refluxing that have not utilized are in fermentor tank.
(7) feed supplement double enzymes saccharification, fermentation: add a certain amount of straw powder from opening for feed, under the effect of the fermented liquid of rich cellulose enzyme, zytase and yeast, substratum continues enzymolysis and becomes reducing sugar, is fermented into alcohol.
(8) distillation: filtrate flows into alcohol distillation tower, chuck heats up, and temperature is 88 ℃, distillation, alcohol getting rate 7.8%.
(9) deslagging: fed-batch fermentation is after 3 days, and after the pipeline of pressure pump and ceramic super-filtering film separates, small molecules filtrate is discharged to distillation tower distillation, and residual macromole cellulase and yeast refluxing, in fermentor tank, can utilize again.Fermentation residue is discharged through fermentor tank bottom.
Embodiment 3:
(1) pulverize: after fresh rice straw is cleaned, with hay cutter cutting or pulverize with beater grinder, be screened into the straw powder of 30mm, moisture control is 53%.
(2) biological process pre-treatment: rice straw powder carries out lignin degradation processing through white-rot fungi.
(3) sterilizing: pack rice straw powder into circulating integrated reactor and carry out high-temperature sterilization, 121 ℃, 30min sterilising treatment.
(4) double enzymes saccharification, fermentation: the mixing solutions that sprays cellulase, zytase and yeast saccharomyces cerevisiae from fermentor tank top downwards, the add-on of the active cellulase for 1000IU/g is 2% of stalk weight, activity is that the yeast saccharomyces cerevisiae add-on of 8,000,000,000/g is 1% of stalk weight, the add-on of water is 2 times of straw powder weight, enzymolysis, leavening temperature are controlled at 36 ℃, pH is 4.5, and mixing speed is controlled at 30rpm; 3 days enzymatic hydrolysis and fermentation total times, residual sugar finishes fermentation while no longer variation.
(5) filtering fermentation liquor: pass into aseptic compressed air from fermentor tank top, the fermented liquid that contains cellulase and yeast after preliminary filtration of fie screen of pot bottom, is discharged from fermentation residue relief outlet by fermentation;
(6) Ceramic excessive filtration membrane sepn: the fermented liquid of discharging from fermentor tank bottom is through pressure pump, squeeze into the pipeline that zirconia ceramics ultra-filtration membrane is housed, separate with micromolecular through macromole, small molecules ethanol is through the micropore of ceramic super-filtering film inside and side, lower outlet by membrane separation unit is discharged in alcohol distillation tower, and the macromole cellulase, zytase and the yeast refluxing that have not utilized are in fermentor tank.
(7) feed supplement double enzymes saccharification, fermentation: add a certain amount of straw powder from opening for feed, under the effect of the fermented liquid of rich cellulose enzyme, zytase and yeast, substratum continues enzymolysis and becomes reducing sugar, is fermented into alcohol.
(8) distillation: filtrate flows into alcohol distillation tower, chuck heats up, and temperature is 90 ℃, distillation, alcohol getting rate 7.5%.
(9) deslagging: fed-batch fermentation is after 3 days, and after the pipeline of pressure pump and ceramic super-filtering film separates, small molecules filtrate is discharged to distillation tower distillation, and residual macromole cellulase and yeast refluxing, in fermentor tank, can utilize again.Fermentation residue is discharged through fermentor tank bottom.
In the specific embodiment of the invention, fermentation liquid circulation has utilized twice, but is not limited to twice, can Reusability.The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention.All any modifications of doing within the spirit and principles in the present invention, be equal to and replace and improvement etc., within all should being included in protection scope of the present invention.
Claims (9)
1. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor, comprise 50～100000L mechanical agitation type fermentor tank (1), air cleaning unit (2), steam generation device (3), temperature controlling system, distillation tower (4), lower computer Controlling System (5), Monitor Computer Control System (6), sensor and instrumental system, speed regulator (7) and agitator motor (8), supporting piping system and valve, 0.098MPa～4.0MPa pressure pump (9), the upper end of described mechanical agitation type fermentor tank (1) is provided with opening for feed (10) and feedback outlet (11), lower end is provided with fermentation residue relief outlet (12), it is characterized in that: also comprise Ceramic excessive filtration membrane separation unit (13), the upper end of described Ceramic excessive filtration membrane separation unit (13) is connected with the feedback outlet (11) of mechanical agitation type fermentor tank (1) upper end, and lower end is connected with the fermentation residue relief outlet (12) of mechanical agitation type fermentor tank (1) lower end through pressure pump.
2. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 1 loop reactor, it is characterized in that: also comprise 30 × 30～500 × 500mm fie screen (14), described fie screen (14) is arranged at the fermentation residue relief outlet (12) of mechanical agitation type fermentor tank (1) lower end and locates.
3. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 1 loop reactor, it is characterized in that: described Ceramic excessive filtration membrane separation unit (13) is made up of the tubular type zirconia ceramics ultra-filtration membrane of 1～10 Φ 50 × 5500, the membrane pore size of ceramic super-filtering film is 0.05 μ m～10 μ m.
4. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 2 loop reactor, it is characterized in that: described Ceramic excessive filtration membrane separation unit (13) is made up of the tubular type zirconia ceramics ultra-filtration membrane of 1～10 Φ 50 × 5500, the membrane pore size of ceramic super-filtering film is 0.05 μ m～10 μ m.
5. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 1 loop reactor, is characterized in that: described Ceramic excessive filtration membrane separation unit (13) is wholy set in stainless steel tube (15).
6. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 2 loop reactor, is characterized in that: described Ceramic excessive filtration membrane separation unit (13) is wholy set in stainless steel tube (15).
7. the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 2 loop reactor, it is characterized in that: described fermentation residue relief outlet (12) locates to be provided with upper flange (16) and lower flange (17), described fie screen (14) is arranged at upper and lower flange connections or is arranged at upper flange (16) inner.
8. the reaction method of the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor described in any one in claim 1 to 7, specifically comprises the following steps:
(1) pulverize: stalk is pulverized, be screened into straw powder;
(2) biological process pre-treatment: straw powder is carried out lignin degradation processing through white-rot fungi;
(3) sterilizing: pack straw powder into the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk loop reactor and carry out high-temperature sterilization processing;
(4) double enzymes saccharification, fermentation: spray the mixing solutions of cellulase, zytase and yeast saccharomyces cerevisiae downwards from fermentor tank top, residual sugar finishes fermentation while no longer variation;
(5) filtering fermentation liquor: pass into aseptic compressed air from fermentor tank top, the fermented liquid that contains cellulase and yeast after preliminary filtration of fie screen of pot bottom, is discharged from fermentation residue relief outlet by fermentation;
(6) Ceramic excessive filtration membrane sepn: the fermented liquid of discharging from fermentor tank bottom is through pressure pump, squeeze into the pipeline that zirconia ceramics ultra-filtration membrane is housed, separate with micromolecular through macromole, small molecules ethanol is through the micropore of ceramic super-filtering film inside and side, lower outlet by membrane separation unit is discharged in alcohol distillation tower, and the macromole cellulase, zytase and the yeast refluxing that have not utilized are in fermentor tank;
(7) feed supplement double enzymes saccharification, fermentation: add straw powder from opening for feed, under the effect of the fermented liquid of rich cellulose enzyme, zytase and yeast, substratum continues enzymolysis and becomes reducing sugar, is fermented into alcohol;
(8) distillation: filtrate flows into alcohol distillation tower, chuck heats up, distillation;
(9) deslagging: after fed-batch fermentation, separate through the pipeline of pressure pump and ceramic super-filtering film, small molecules filtrate is discharged to distillation tower distillation, and residual macromole cellulase and yeast refluxing, in fermentor tank, are utilized again; Fermentation residue is discharged through fermentor tank bottom.
9. the reaction method of the synchronous enzymatic hydrolysis and fermentation alcohol fuel of stalk according to claim 8 loop reactor, is characterized in that: the air flow of described mechanical agitation type fermentor tank is stabilized in 0.1～3
; When fermentor tank sterilizing, keep tank pressure 0.11～0.12MPa, when cooling, keep tank pressure 0.03～0.05MPa; Air cleaning unit air flow 10～500L/min, pressure 0.25～0.8MPa; The steam research on maximum utilized quantity of steam generation device is 10kg/h, pressure 0.25～0.85MPa, low-pressure steam pressure 0.16～0.5 MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310165238.5A CN103243023B (en) | 2013-05-08 | 2013-05-08 | Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310165238.5A CN103243023B (en) | 2013-05-08 | 2013-05-08 | Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103243023A CN103243023A (en) | 2013-08-14 |
| CN103243023B true CN103243023B (en) | 2014-05-28 |
Family
ID=48922903
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310165238.5A Expired - Fee Related CN103243023B (en) | 2013-05-08 | 2013-05-08 | Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103243023B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104342358B (en) * | 2013-08-07 | 2016-09-21 | 国家电网公司 | Fermentation fuel reactor and the method producing fermentation fuel |
| CN105316366A (en) * | 2015-10-20 | 2016-02-10 | 陈国章 | Production method for comprehensively utilizing biological straw |
| CN106669887B (en) * | 2016-12-30 | 2018-11-09 | 天津替代医学科技股份有限公司 | A kind of production fermented product raw material crushing digesting apparatus |
| CN106987523B (en) * | 2017-03-06 | 2019-05-14 | 上海交通大学 | A kind of method and system continuously fermented |
| CN108641896B (en) * | 2018-05-17 | 2021-09-21 | 福建达邦蛋白生物科技有限公司 | Aquatic feed rapid fermentation manufacturing machine |
| CN108841576B (en) * | 2018-06-29 | 2022-01-04 | 铜陵盛牛菌业有限责任公司 | Straw fermentation device |
| CN109239141B (en) * | 2018-08-21 | 2020-07-24 | 北京化工大学 | Fermentation process feedback material supplementing control device and method based on alcohol gas concentration online detection |
| CN114041621A (en) * | 2021-11-22 | 2022-02-15 | 红云红河烟草(集团)有限责任公司 | Method for preparing tobacco flavor sugar material by utilizing industrial tobacco waste |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011188791A (en) * | 2010-03-15 | 2011-09-29 | Toray Ind Inc | Method for operating continuous fermentation apparatus |
| WO2012077742A1 (en) * | 2010-12-09 | 2012-06-14 | 東レ株式会社 | Method for producing chemical by continuous fermentation |
| KR101190647B1 (en) * | 2010-12-31 | 2012-10-17 | 대한민국 | Pretreatment system and method for manufacturing substrate for ethanol fermentation from cellulose biomass |
| CN202415532U (en) * | 2011-12-31 | 2012-09-05 | 常州益菌加生物科技有限公司 | Equipment system for preparing probiotics |
| CN102634454B (en) * | 2012-04-27 | 2013-09-25 | 镇江江工生物工程成套设备有限公司 | Solid-state rapid sterilizing microorganism reactor and control method thereof |
| CN202808773U (en) * | 2012-07-20 | 2013-03-20 | 江苏南天农科化工有限公司 | Series connection device of multiple stages of acrylamide reaction kettles |
| CN203247263U (en) * | 2013-05-08 | 2013-10-23 | 江苏大学 | Straw synchronized enzymolysis and fermentation fuel alcohol circulation reactor |
-
2013
- 2013-05-08 CN CN201310165238.5A patent/CN103243023B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN103243023A (en) | 2013-08-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103243023B (en) | Circulating synchronous straw enzymatic hydrolysis fermentation fuel ethanol reactor and reaction method thereof | |
| CN100572543C (en) | Utilize corn cob or agriculture and forestry organic waste material to prepare the method for Xylitol | |
| CN104774876B (en) | A kind of method of lignocellulose biomass comprehensive utilization | |
| CN104611381B (en) | A kind of method of lignocellulosic continuous enzymolysis fermentation producing and ethanol | |
| KR20100095994A (en) | Procedure for concentration of microorganisms in aqueous substrates | |
| CN104342358A (en) | Fermentation fuel reactor and fermentation fuel production method | |
| CN108676788A (en) | A kind of fixed yeast continuously ferments technology | |
| CN105368703A (en) | Device and technique for preparing fuel ethanol through corn straw solid-liquid parallel method | |
| CN203546025U (en) | Enclosed simultaneous saccharification lactic acid production line | |
| CN102051329B (en) | Biomass ferment-separation coupling device and method for preparing ethanol | |
| CN101768545B (en) | Cycling elution biomimetic peristaltic enzymolysis reactor and method thereof | |
| CN203474776U (en) | Fermented fuel reactor | |
| CN203247263U (en) | Straw synchronized enzymolysis and fermentation fuel alcohol circulation reactor | |
| CN103409333A (en) | Recombinant saccharomyces cerevisiae strain for continuously and efficiently secreting beta-glucosidase and applications thereof | |
| CN104357428A (en) | Liquid submerged fermentation method of xylanase | |
| CN108203710B (en) | Method for inducing trichoderma reesei to produce cellulase by using pure straw solid material supplementing and material supplementing device used in method | |
| CN220867403U (en) | Straw biomass anaerobic fermentation hydrolysis station system | |
| CN103382489A (en) | Method for producing alcohol through liquor fermentation | |
| CN102605003B (en) | Method for producing alcohol from potato raw materials | |
| CN109988757A (en) | A kind of method that surface immobilized yeast semicontinuous fermentation prepares ethyl alcohol | |
| CN105154494B (en) | A kind of method that lignocellulosic continuous enzymolysis mentions high glucose concentration | |
| CN102051386A (en) | Method for producing organic acid at high production rate through fermentation of intermittent backflow cells | |
| CN104531777A (en) | Acid-free fermentation method for producing ethyl alcohol with fresh cassava full pulp as raw materials | |
| CN101988077B (en) | Method for preparing ethanol from potato raw material | |
| CN108841580B (en) | Hydrogen-producing and methane-producing reactor for treating solid waste |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140528 |