CN102286544B - A kind of clean preparation method of starch base alcohol fuel - Google Patents
A kind of clean preparation method of starch base alcohol fuel Download PDFInfo
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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
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- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
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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
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Abstract
The present invention relates to a kind of clean preparation method of starch base alcohol fuel, comprise following workshop section: (1) liquefies, (2) saccharification, (3) ferment, (4) distillation and dehydration, also comprises useless poor comprehensive treating process and byproduct recycles workshop section.Wherein liquefy workshop section's employing low pressure ejector will continuous steaming-boiling technology; Fermentation workshop section adopts semicontinuous fermentation system, makes karusen be in flow state, promotes the uniform contact of yeast and mash; Distillation and dehydration workshop section adopt live steam heat supply rectifying tower, rectifying tower tower top wine vapour heat supply combined column, the thermal coupling scheme of combined column tower top wine vapour heat supply topping still, the dehydrated alcohol obtained obtains fuel ethanol after mixture, quality meets standard GB/T 18350-2001, and recycles the useful matter in the useless grain of workshop section's recycling and waste gas by useless poor comprehensive treating process and byproduct.Each production workshop section heat exchanger network and network of rivers network rational Match in the method, achieve material consumption and energy consumption is low, the sufficient cleaner production target of the utilization of resources.
Description
Technical field
The invention belongs to biological technical field, relate to a kind of clean preparation method of starch base alcohol fuel, particularly the starch-based initial material such as a kind of corn, cassava, Ipomoea batatas produces the method for alcohol fuel.
Background technology
Alcohol industry refers to cereal, potato class, molasses for raw material, through fermentation, distillation and produce the industry of edible ethanol, industrial spirit and alcohol fuel, is the important basic material industry of national economy.In recent decades, along with skyrocketing of oil price and making rapid progress of biotechnology, be that raw material production is increasingly extensive for the alcohol fuel application of alternative vehicle fuel, minimizing vehicle exhaust objectionable impurities with biomass.
China's alcohol industry waste discharge total amount about 400,000,000 tons in 2007, year discharge COD about 4,000,000 tons, BOD about 2,000,000 tons is one of industry that organic pollutant quantity discharged is higher.Meanwhile, it is low to there is level of automation in traditional production of alcohol fuel, and the problems such as material consumption and energy consumption high, full factory systematic integration optimization difference, remain in larger gap with the alcohol fuel big country such as the U.S., Brazil.
Summary of the invention
In order to solve above-mentioned the deficiencies in the prior art part, primary and foremost purpose of the present invention is the clean preparation method providing a kind of starch base alcohol fuel, is the method for producing alcohol fuel with starch-based initial material such as corn, cassava, Ipomoea batatas.This production method has material consumption and energy consumption is low, level of automation is high, can realize the advantage of water and hot integrated optimization.
Object of the present invention is achieved through the following technical solutions: a kind of clean preparation method of starch base alcohol fuel, and the technical process of this production method is: starchy material → liquefaction → saccharification → fermentation → distillation → dehydration → alcohol fuel, as shown in Figure 1.
A clean preparation method for starch base alcohol fuel, this production method realizes mainly through following workshop section:
(1) liquefy: by starchy material and water and α-amylase mixing and stirring, obtain the powder slurry that dry biomass content is 20% ~ 34%, pre liquefied tank is sent into after being preheated to 70 ~ 85 DEG C, stir, powder slurry is heated to 80 ~ 90 DEG C simultaneously, the insoluble substance stirred during powder mix is starched reaches stable suspended state, carry out low-pressure steam injection liquefaction again, drop temperature is 100 ~ 110 DEG C, then 1 ~ 2h is kept to carry out boiling slaking at 100 ~ 110 DEG C, flash cooling is carried out after mash after gained slaking is cooled to 65 ~ 80 DEG C, obtain liquefied fermented glutinous rice.
Described starchy material is 60% ~ 70% by starch content, and biodiversity content is the corn of 10% ~ 20%, a kind of median size that is crushed in cassava and Ipomoea batatas is the starch granules that 1 ~ 3mm obtains; The consumption of described α-amylase is by 1.5 ~ 2.0kg/t process of alcohol products.
The working pressure of the flash tank that described flash cooling uses is-90 ~-60kPa; The flash steam temperature obtained after flash distillation is 50 ~ 70 DEG C, as liquefaction workshop section water after flash steam condensation.
The continuous steaming-boiling technology of boiling after described liquefaction workshop section employing low-pressure steam injection, powder mix is starched and is heated evenly, starch-based initial material gelatinization is thorough, compares, can improve the rate of getting alcohol 0.5% with high-temperature cooking process, and energy-conservation 30%.The temperature of the mash after described slaking heats from the heats that 100 ~ 110 DEG C are down to 65 ~ 80 DEG C of releases for starching the powder before feeding liquefied pot, thus realizes making full use of of energy; After pre liquefied tank sent into by powder slurry, the residence time in tank is 20 ~ 50min.
(2) saccharification: the pH value regulating liquefied fermented glutinous rice in saccharifying tank with sulfuric acid is 4.0 ~ 4.5, α-1 is added while stirring, 4-glucose hydrolysis enzyme, its consumption is 3.2 ~ 4.0kg/t process of alcohol products, is incubated 30 ~ 60min and carries out saccharification after adding at 50 ~ 70 DEG C; Liquefied fermented glutinous rice after saccharification is cooled to 28 ~ 32 DEG C and obtains converted mash, is sent to fermentation workshop section.
The cooling of the liquefied fermented glutinous rice after described saccharification uses two-stage cooler, cools step by step, and water cooler is the one in spiral plate type and plate cooler.
(3) ferment: adopt semicontinuous fermentation process, use 1 distiller's yeast tank and n fermentor tank jointly to ferment.Its zymotechnique flow process is: first in distiller's yeast tank, add converted mash, active dry yeast and urea, carry out after stirring breeding and fermenting, the yeast wash obtained and the mixed mash of remaining converted mash flow into 1# continuous fermentation tank, after filling it up with, naturally 2# continuous fermentation tank is flowed into, after 2# continuous fermentation tank is filled it up with, naturally 3# continuous fermentation tank is flowed into, after 3# continuous fermentation tank is filled it up with, 4# batch fermentation tank is flowed into by 3# continuous fermentation tank, after 4# batch fermentation tank is filled it up with, then changed by 3# continuous fermentation tank and flow to 5# batch fermentation tank, 5# ~ n# batch fermentation tank is filled it up with one by one by 3# continuous fermentation tank by this step, then batch fermentation is carried out, after fermentation ends, obtain fermenting-ripening wine with dregs.
Described n=6 ~ 10,1 ~ 3# is continuous fermentation tank, and mash fermentation time is wherein 24 ~ 30h, temperature is 30 ~ 33 DEG C, and 4 ~ n# tank is batch fermentation tank, and mash fermentation time is wherein 35 ~ 45h, temperature is 30 ~ 36 DEG C.
The quality of the described converted mash added in distiller's yeast tank is 30% ~ 40% of gained converted mash total mass in workshop section (2), the quality adding active dry yeast, by 0.1 ~ 0.15kg/t process of alcohol products, adds the quality of urea by 1 ~ 3kg/t process of alcohol products; The temperature of carrying out breeding and ferment in distiller's yeast tank is 28 ~ 32 DEG C, and the time is 10 ~ 12h.
The CO produced from the fermenting process of distiller's yeast tank and fermentor tank in described fermentation workshop section
2with in workshop section (4) from topping still degassing stages discharge CO
2jointly enter the recovery that washing tower carries out carbonic acid gas.
Described fermentation workshop section adopts semicontinuous fermentation process, and karusen is in flow state, can promote the uniform contact of yeast and mash, be beneficial to CO
2discharge and recovery, strengthen the fermentation activity of yeast simultaneously, improve starch utilization ratio.The continuous fermentation tank of semicontinuous fermentation scrubs sterilization tank body for usual about 10 ~ 15 days, saves non-cutting time of fermenting, improves plant factor.
(4) distillation and dehydration: undertaken degassed by introducing topping still degassing stages after the preheating of fermenting-ripening wine with dregs, the CO2 deviate from enters de-vapour section condenser condenses with alcohol steam, discharges CO2 and noncondensable gas; Ripe wine with dregs after degassed is divided into two strands, one accounts for 30% ~ 60% of total mass flow rate, introduce topping still stripping section and carry out predistillation, obtain giving up at the bottom of alcohol steam and topping still tower wine with dregs, described alcohol steam obtains thick wine after de-vapour section condenser condenses, introduce crude alcohol tank, described useless wine with dregs is discharged by bottom topping still; Another strand degassed after ripe wine with dregs from lateral line withdrawal function bottom degassing stages, after wine with dregs preheating of giving up at the bottom of combined column tower, introduce combined column again distill, obtain giving up at the bottom of tower top alcohol steam and combined column tower wine with dregs; A described tower top alcohol steam part introduces condensation in the forced circulating reboiler of topping still, and condensation latent heat is for heating topping still, and phlegma is as trim the top of column; Another part alcohol steam introduces molecular sieve dehydration unit, obtain light wine that concentration is 60% ~ 80%V/V and dehydrated alcohol finished product steam, crude alcohol tank introduced by light wine, namely process of alcohol products is obtained after dehydrated alcohol finished product vapor condensation, obtain fuel ethanol finished product after adding denaturing agent in this product, quality product meets standard GB/T 18350-2001; Described useless wine with dregs is discharged by bottom combined column;
Being undertaken concentrating and being separated by introducing rectifying tower after the thick wine preheating in crude alcohol tank, obtaining respectively heating up in a steamer water more than at the bottom of the alcohol of potato spirit, tower top alcohol steam and tower; The described alcohol containing potato spirit cools after drawing above charging layer, then dilute with water washing, and the lower floor shifted out after layering is potato spirit dilution washing light wine, enters crude alcohol tank; Described tower top alcohol steam introduces condensation in the forced circulating reboiler of combined column, and the latent heat of condensation is used for heating in combination tower, and 40% ~ 70% of phlegma mass rate is back to rectifying tower top layer column plate, and all the other phlegmas are introduced combined column and again distilled; Heat up in a steamer water more than at the bottom of described tower to draw by the bottom of rectifying tower.
The described fermenting-ripening wine with dregs entering topping still degassing stages utilizes to give up wine with dregs at the bottom of topping still alcohol steam, topping still tower and carry out preheating from the dehydrated alcohol finished product steam of molecular sieve dehydration unit; Described rectifying tower passes into after live steam carries out heat supply by tower bottom reboiler, heat up in a steamer after water carries out secondary preheating to crude alcohol more than the vapour that steam generation condensation obtains coagulates at the bottom of water and rectifying tower, a part return boiler as reuse water, another part through cooling after for diluting the alcohol containing potato spirit.
This workshop section adopts multiple-effect thermal coupling rectification process, and thermal coupling scheme is: live steam heat supply rectifying tower, rectifying tower tower top alcohol steam heat supply combined column, combined column tower top alcohol steam heat supply topping still.Improve the utilising efficiency of heat energy thus, and reduce the consumption of recirculated water, reach energy-saving and cost-reducing effect.
As a kind of preferred version, working pressure, the tower top temperature of each distillation tower are respectively:
Topping still tower top operation pressure is-70 ~-30kPa, tower top temperature 55 ~ 75 DEG C;
Combined column tower top working pressure is 0 ~ 100kPa, tower top temperature 78 ~ 102 DEG C;
Rectifying tower tower top working pressure is 300 ~ 520kPa, tower top temperature 110 ~ 135 DEG C.
Described molecular sieve dehydration unit is made up of adsorbing tower with molecular sieve and Analytic Tower; Adsorbing tower with molecular sieve working pressure is 0 ~ 150kPa; Molecular sieve Analytic Tower working pressure is-80 ~ 0kPa.
The production method of a kind of starch base alcohol fuel of the present invention also comprises Fei Zao comprehensive treating process workshop section and byproduct recycles workshop section.Wherein, useless grain process is after carrying out solid-liquid separation to useless wine with dregs, process respectively in solid and liquid, make it to be converted into feed, organic fertilizer or other byproducts, the clear liquid that process produces and water of condensation are as liquefaction workshop section water, and residue waste water is by relevant national standard discharge or be directly used in irrigated farmland.
Such as, if take corn as raw material production alcohol, its useless poor treatment scheme is shown in Fig. 4, primarily of solid-liquid separation, evaporation concentration, drying, blower fan conveying, composition such as operation such as storage powder, packaging etc., facilities and equipment mainly contains: pump, basin, whizzer, evaporation concentration device, drying machine, blower fan, powder storehouse, wrapping machine, finished product bunker storehouse.Concrete treatment step is: the first step reclaims DDS in waste water, reduce the pollutent entering environment-friendly disposal system, comprise and press filtration process is carried out to the waste dregs liquid of Alcohol Production discharge, supernatant fraction reuse, part enters evaporation concentration system production underflow, and the mixing of underflow filter residue is obtained DDGS (white drying alcohol grain) through pipe bundle drier drying, granulation, cooling; Second step Treated sewage reusing: the secondary concentrating generation to clear liquid coagulates water and processes, and the middle water after process, as liquefaction workshop section water, realizes recycling of full factory water of productive use.The waste hot gas of described evaporation concentration device is after MVR mechanical steam recompression device, and grade improves, and is used as the supplemental heat source of evaporation concentration device self, can reduce the standard coal consumption of useless grain process workshop section 81%.
If do as raw material production alcohol with cassava, its poor liquid treatment scheme is primarily of operation compositions such as separation, anaerobic digestion, aerobic treatments.Its facilities and equipment mainly contains: basin (pond), water cooler, separating machine, marsh-gas fermentation tank (pond), pump, biogas, the effectively treatment facility such as aerobic, biogas is obtained after process, for generating after purification, remaining waste water is by relevant national standard discharge or be directly used in irrigated farmland.
Byproduct is recycled workshop section and is then comprised Liquid carbon dioxide recovery, and methane purification purification is separated with the precision of potato spirit, sees Fig. 1.Its main purpose improves the added value of byproduct, realizes the maximization of the full factory utilization of resources and the maximization of economic benefit.
Accompanying drawing explanation
Fig. 1 is the production general flow chart of starch base alcohol fuel.
Fig. 2 is the schema of liquefaction, saccharification and fermentation workshop section.
Fig. 3 is the schema of distillation and dehydration workshop section.
Fig. 4 is the schema of the Fei Zao comprehensive treating process workshop section taking W-Gum as raw material production alcohol fuel.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited thereto.
Embodiment 1
The technique taking W-Gum as raw material production alcohol fuel is as follows:
By 37.7t/h corn, (starch content is 65%, biodiversity content is 14%) to be crushed to median size be that 2mm sends into pre liquefied tank, add 84.6t/h spice water, α-amylase 22kg/h, obtain the powder slurry that dry biomass content is 26.5%, starch for making powder and mix, agitator is furnished with in tank, pre liquefied tank is sent into after powder slurry is preheated to 78 DEG C, in pre liquefied tank, above-mentioned powder is starched by direct steam heating to 86 DEG C, the suspended state that agitator impels insoluble substance to reach stable.When full load operation, the residence time of powder slurry in tank is 40min.
Then powder slurry removes Jet liquefier by pumping, and controlling steam injector drop temperature is 105 DEG C, obtains the mash after heating.Mash after heating is sent into boiling post, keeps 1.5h to carry out boiling slaking at 105 DEG C.Mash after slaking is pumped to powder slurry preheater, and after carrying out preheating to the powder slurry not entering liquefied pot, temperature enters flash tank after being down to 70 DEG C, and the pressure of described flash tank is-75kPa, and after flash distillation, the temperature of liquefied fermented glutinous rice is 65 DEG C.As liquefaction workshop section water after the flash steam condensation produced.Liquefied fermented glutinous rice after flash cooling flows in saccharifying tank voluntarily by action of gravity.
Be 4.2 by sulfuric acid adjust ph in saccharifying tank (outfit agitator), then α-1 is added, 4-glucose hydrolysis enzyme 43kg/h, 45min is incubated at 65 DEG C, mash after saccharification is cooled through two-stage plate cooler step by step by pump delivery, be cooled to 31 DEG C, obtain converted mash and be sent to fermentation workshop section.
Fermentation workshop section adopts semicontinuous fermentation process, uses 1 distiller's yeast tank and 10 fermentor tanks jointly to ferment.When starting to go into operation, after distiller's yeast tank cleaning and sterilization, add the converted mash accounting for total converted mash quality 35%, add the quality of active dry yeast by 0.15kg/t process of alcohol products, add the quality of urea by 2kg/t process of alcohol products, carry out saccharomycetic advantage propagation and fermentation after mixing, temperature is 30 DEG C, and the time is 12h; The yeast wash obtained and the mixed mash of remaining converted mash flow into 1# continuous fermentation tank, after filling it up with, naturally 2# continuous fermentation tank is flowed into, after 2# continuous fermentation tank is filled it up with, naturally flow into 3# continuous fermentation tank, after 3# continuous fermentation tank is filled it up with, 4# batch fermentation tank is flowed into by 3# continuous fermentation tank, after 4# batch fermentation tank is filled it up with, then changed by 3# continuous fermentation tank and flow to 5# batch fermentation tank, fill it up with 5# ~ 10# batch fermentation tank by this step one by one by 3# continuous fermentation tank.First three tank keeps continuous Primary Fermentation state, and fermentation time is 26h, temperature is 32 DEG C.The fermentation time of 4# ~ 10# batch fermentation tank is 40h, temperature is 35 DEG C, after fermentation ends, and the fermenting-ripening wine with dregs obtained sends to distillation and dehydration workshop section, and tank body repeats above operation again after scrubbing sterilizing.
Fermenting-ripening wine with dregs (112t/h, 14%V/V, 32 DEG C) after wine with dregs three grades of preheatings of giving up at the bottom of topping still alcohol steam, dehydrated alcohol finished product steam, topping still tower, enter topping still degassing stages carry out degassed, the CO2 deviate from enters de-vapour section condenser condenses with alcohol steam, discharges CO2 and noncondensable gas; Ripe wine with dregs after degassed is divided into two strands, and one enters topping still stripping section and carries out predistillation, and obtain alcohol steam and obtain thick wine after de-vapour section condenser condenses, enter crude alcohol tank, the useless wine with dregs obtained is discharged by bottom topping still, goes to useless grain process workshop section; Another strand degassed after ripe wine with dregs from lateral line withdrawal function bottom degassing stages, flow is 67.2t/h, after combined column tower reactor gives up wine with dregs preheating, enter combined column again distill, alcohol steam (95.8%V/V) part that tower top obtains enters condensation in the forced circulating reboiler of topping still, condensation latent heat is for heating topping still, phlegma, as trim the top of column, obtains useless wine with dregs and discharges by bottom combined column, goes to useless grain process workshop section; Another part alcohol steam is sent to molecular sieve dehydration unit, and obtain concentration for the light wine of (70%V/V) and dehydrated alcohol finished product steam, light wine enters crude alcohol tank, obtains process of alcohol products after dehydrated alcohol finished product vapor condensation; Mass rate is 12.6t/h, and quality product mark is 99.2%, water content < 0.5%, acid content 46ppm, meets standard GB/T 18350-2001, and distillation and dehydration workshop section steam consumption are 1.42t/t alcohol fuel.
Rectifying tower is (520kPa) operation under malleation operating mode, rectifying tower tower bottom reboiler passes into live steam and carries out heat supply, thick wine in crude alcohol tank coagulates and to enter rectifying tower through heating up in a steamer vapour at the bottom of water, tower more than at the bottom of rectifying tower after water two-stage is preheating to 132 DEG C and carry out the concentrated of thick wine and be separated, heats up in a steamer water more than obtaining respectively containing at the bottom of the alcohol of potato spirit, tower top alcohol steam and tower; The alcohol containing potato spirit obtained cools after drawing above charging layer, then dilute with water washing, and the lower floor shifted out after layering is potato spirit dilution washing light wine, enters crude alcohol tank; The tower top alcohol steam obtained introduces condensation in the forced circulating reboiler of combined column, the latent heat of condensation is used for heating in combination tower, flow is that the phlegma of 10.5t/h is back to rectifying tower top layer column plate, and all the other extraction enter combined column and again distill, and heats up in a steamer water more than drawing at the bottom of rectifying tower.
At the bottom of topping still and combined column tower, the useless wine with dregs of discharge is through plate-and-frame filter press press filtration process, liquefaction workshop section water is made in isolated clear liquid 30% reuse, 70% enters evaporation concentration system production underflow, underflow is mixed with pressure filter filter residue out, obtains through pipe bundle drier drying, granulation, cooling the DDGS feed that moisture is less than 11.5%.The waste hot gas of pipe bundle drier outlet is after MVR mechanical steam recompression device, and grade improves, for the supplemental heat source of evaporation concentration device.The secondary that clear liquid concentrates generation coagulates water and carries out sewage disposal, and the middle water after process is used as liquefaction workshop section water, and realize recycling of full factory water of productive use, Fig. 4 sees in this process workshop section.The total steam consumption of full factory is 3.45t/t alcohol fuel (containing Fei Zao comprehensive treating process workshop section).
Embodiment 2
As follows with the technique that cassava does as raw material production alcohol fuel:
By 20t/h tapioca slice, (starch content is 68%, biodiversity content is 12%) to be crushed to median size be send into pre liquefied tank after 3mm, add 40t/h spice water, add α-amylase 12.5kg/h simultaneously, obtain the powder slurry that dry biomass content is 29.3%, starch for making powder and mix, agitator is furnished with in tank, pre liquefied tank is sent into after powder slurry is heated to 75 DEG C, in pre liquefied tank, above-mentioned powder is starched by direct steam heating to 84 DEG C, the suspended state that agitator impels insoluble substance to reach stable.When full load operation, the residence time of powder slurry in tank is 30min.
Then powder slurry removes Jet liquefier by pumping, and controlling steam injector drop temperature is 106 DEG C, obtains the mash after heating.Mash after heating is sent into boiling post, keeps 2h to carry out boiling slaking at 106 DEG C.Mash after slaking is pumped to powder slurry preheater, and after carrying out preheating to the powder slurry not entering liquefied pot, temperature enters flash tank after being down to 68 DEG C, and the pressure of described flash tank is-80kPa, and after flash distillation, the temperature of liquefied fermented glutinous rice is 60 DEG C.As liquefaction workshop section water after the flash steam condensation produced.Liquefied fermented glutinous rice after flash cooling flows in saccharifying tank voluntarily by action of gravity.
Be 4.5 by sulfuric acid adjust ph in saccharifying tank (outfit agitator), then α-1 is added, 4-glucose hydrolysis enzyme 25kg/h, 50min is incubated at 60 DEG C, mash after saccharification is cooled through two-stage plate cooler step by step by pump delivery, be cooled to 29 DEG C, obtain converted mash and be sent to fermentation workshop section.
Fermentation workshop section adopts semicontinuous fermentation process, uses 1 distiller's yeast tank and 6 fermentor tanks jointly to ferment.When starting to go into operation, after distiller's yeast tank cleaning and sterilization, add the converted mash accounting for total converted mash quality 32%, add the quality of active dry yeast by 0.1kg/t process of alcohol products, add the quality of urea by 3kg/t process of alcohol products, carry out saccharomycetic advantage propagation and fermentation after mixing, temperature is 28 DEG C, and the time is 10h; The yeast wash obtained and the mixed mash of remaining converted mash flow into 1# continuous fermentation tank, after filling it up with, naturally flow into 2# continuous fermentation tank, after 2# continuous fermentation tank is filled it up with, naturally flow into 3# continuous fermentation tank, after 3# continuous fermentation tank is filled it up with, flow into 4# batch fermentation tank by 3# continuous fermentation tank, after 4# batch fermentation tank is filled it up with, then changed by 3# continuous fermentation tank and flow to 5# batch fermentation tank, after 5# batch fermentation tank is filled it up with, then changed by 3# continuous fermentation tank and flow to 6# batch fermentation tank.First three tank keeps continuous Primary Fermentation state, and fermentation time is 28h, and temperature is 33 DEG C.The fermentation time of 4# ~ 6# batch fermentation tank is 38h, temperature is 34 DEG C, after fermentation ends, and the fermenting-ripening wine with dregs obtained sends to distillation and dehydration workshop section, and tank body repeats above operation again after scrubbing sterilizing.
Fermenting-ripening wine with dregs (66.3t/h, 13.0%V/V, 33 DEG C) after wine with dregs three grades of preheatings of giving up at the bottom of topping still alcohol steam, dehydrated alcohol finished product steam, topping still tower, enter topping still degassing stages carry out degassed, the CO2 deviate from enters de-vapour section condenser condenses with alcohol steam, discharges CO2 and noncondensable gas; Ripe wine with dregs after degassed is divided into two strands, and one enters topping still stripping section and carries out predistillation, and obtain alcohol steam and obtain thick wine after de-vapour section condenser condenses, enter crude alcohol tank, the useless wine with dregs obtained is discharged by bottom topping still, goes to useless grain process workshop section; Another strand degassed after ripe wine with dregs from lateral line withdrawal function bottom degassing stages, flow is 32t/h, after combined column tower reactor gives up wine with dregs preheating, enter combined column again distill, alcohol steam (96.0%V/V) part that tower top obtains enters condensation in the forced circulating reboiler of topping still, condensation latent heat is for heating topping still, phlegma, as trim the top of column, obtains useless wine with dregs and discharges by bottom combined column, goes to useless grain process workshop section; Another part alcohol steam is sent to molecular sieve dehydration unit, and obtain concentration for the light wine of (65%V/V) and dehydrated alcohol finished product steam, light wine enters crude alcohol tank, namely obtains process of alcohol products after dehydrated alcohol finished product vapor condensation; Mass rate is 6.95t/h, and quality product mark is 99.4%, water content < 0.3%, acid content 39ppm, meets fuel ethanol standard GB/T 18350-2001, and distillation and dehydration workshop section steam consumption are 1.45t/t alcohol fuel.
Rectifying tower is (480kPa) operation under malleation operating mode, rectifying tower tower bottom reboiler passes into live steam and carries out heat supply, thick wine in crude alcohol tank coagulates and to enter rectifying tower through heating up in a steamer vapour at the bottom of water, tower more than at the bottom of rectifying tower after water two-stage is preheating to 132 DEG C and carry out the concentrated of thick wine and be separated, heats up in a steamer water more than obtaining respectively containing at the bottom of the alcohol of potato spirit, tower top alcohol steam and tower; The alcohol containing potato spirit obtained cools after drawing above charging layer, then dilute with water washing, and the lower floor shifted out after layering is potato spirit dilution washing light wine, enters crude alcohol tank; The tower top alcohol steam obtained introduces condensation in the forced circulating reboiler of combined column, the latent heat of condensation is used for heating in combination tower, flow is that the phlegma of 10.5t/h is back to rectifying tower top layer column plate, and all the other extraction enter combined column and again distill, and heats up in a steamer water more than drawing at the bottom of rectifying tower.
The process of the useless wine with dregs that distillation dehydration system is discharged is primarily of operation compositions such as separation, anaerobic digestion, aerobic treatments.Its facilities and equipment mainly contains: basin (pond), water cooler, separating machine, marsh-gas fermentation tank (pond), pump, biogas, the effectively treatment facility such as aerobic.Useless grain is after above-mentioned treatment process process, and the biogas of generation is used for combustion power generation, and remaining waste water (COD value is 197mg/L) discharges by relevant national standard.The total steam consumption of full factory owner's device is 2.51t/t alcohol fuel.
Above-described embodiment is the present invention's preferably embodiment, but embodiments of the present invention are not restricted to the described embodiments, change, the modification done under other any does not deviate from spirit of the present invention and principle, substitute, combine, simplify, all should be the substitute mode of equivalence, be included among spirit of the present invention, scope and content.
Claims (3)
1. a clean preparation method for starch base alcohol fuel, is characterized in that comprising following workshop section:
(1) liquefy: by starchy material and water and α-amylase mixing and stirring, obtain the powder slurry that dry biomass content is 20% ~ 34%, pre liquefied tank is sent into after being preheated to 70 ~ 85 DEG C, stir, then powder slurry is heated to 80 ~ 90 DEG C, carry out low-pressure steam injection liquefaction again, drop temperature is 100 ~ 110 DEG C, obtain liquefied fermented glutinous rice, 1 ~ 2h is kept to carry out boiling slaking at 100 ~ 110 DEG C, carry out flash cooling after liquefied fermented glutinous rice after slaking is cooled to 65 ~ 80 DEG C, obtain liquefied fermented glutinous rice;
Described starchy material is for being 60% ~ 70% by starch content, and biodiversity content is the corn of 10% ~ 20%, a kind of median size that is crushed in cassava and Ipomoea batatas is the starch granules that 1 ~ 3mm obtains; The consumption of described α-amylase is by 1.5 ~ 2.0kg/t process of alcohol products;
After pre liquefied tank sent into by described powder slurry, the residence time in tank is 20 ~ 50min; Liquefied fermented glutinous rice after described slaking heats from the heats that 100 ~ 110 DEG C are cooled to 65 ~ 80 DEG C of releases for starching the powder before feeding liquefied pot; The pressure of the flash tank that described flash cooling is used is-90 ~-60kPa, and the flash steam temperature obtained after flash distillation is 50 ~ 70 DEG C, is used as liquefaction workshop section water after flash steam condensation;
(2) saccharification: the pH value regulating liquefied fermented glutinous rice with sulfuric acid is 4.0 ~ 4.5, adds α-Isosorbide-5-Nitrae-glucose hydrolysis enzyme while stirring, its consumption, by 3.2 ~ 4.0kg/t process of alcohol products, is incubated 30 ~ 60min and carries out saccharification at 50 ~ 70 DEG C after adding; Mash after saccharification is cooled to 28 ~ 32 DEG C and obtains converted mash;
The cooling of the liquefaction mash after described saccharification uses two-stage cooler, cools step by step, and water cooler is the one in spiral plate type and plate cooler;
(3) ferment: add in distiller's yeast tank by 30% ~ 40% of gained converted mash total mass in workshop section (2) with active dry yeast and urea, carry out after stirring breeding and fermenting, the yeast wash obtained and the mixed mash of remaining converted mash flow into 1# continuous fermentation tank, after filling it up with, naturally 2# continuous fermentation tank is flowed into, after 2# continuous fermentation tank is filled it up with, naturally flow into 3# continuous fermentation tank; After 3# continuous fermentation tank is filled it up with, flow into 4# batch fermentation tank, after 4# batch fermentation tank is filled it up with, then changed by 3# continuous fermentation tank and flow to 5# batch fermentation tank, the laggard row batch fermentation of 5# ~ n# batch fermentation tank is filled it up with one by one by 3# continuous fermentation tank, wherein n=6 ~ 10 by this step; After fermentation ends, obtain fermenting-ripening wine with dregs;
The described quality adding active dry yeast in distiller's yeast tank, by 0.1 ~ 0.15kg/t process of alcohol products, adds the quality of urea by 1 ~ 3kg/t process of alcohol products; The temperature of carrying out breeding and ferment in distiller's yeast tank is 28 ~ 32 DEG C, and the time is 10 ~ 12h;
Described 1-3# is continuous fermentation tank, and in tank, the fermentation time of mash is 24 ~ 30h, and temperature is 30 ~ 33 DEG C, and 4-n# is batch fermentation tank, and in tank, the fermentation time of mash is 35 ~ 45h, and temperature is 30 ~ 36 DEG C;
(4) distillation and dehydration: undertaken degassed by introducing topping still degassing stages after the preheating of fermenting-ripening wine with dregs, the CO deviate from
2enter de-vapour section condenser condenses with alcohol steam, discharge CO
2and noncondensable gas; Ripe wine with dregs after degassed is divided into two strands, one accounts for 30% ~ 60% of total mass flow rate, introduce topping still stripping section and carry out predistillation, obtain giving up at the bottom of alcohol steam and topping still tower wine with dregs, described alcohol steam obtains thick wine after de-vapour section condenser condenses, introduce crude alcohol tank, described useless wine with dregs is discharged by bottom topping still; Another strand degassed after ripe wine with dregs from lateral line withdrawal function bottom degassing stages, after wine with dregs preheating of giving up at the bottom of combined column tower, introduce combined column again distill, obtain giving up at the bottom of tower top alcohol steam and combined column tower wine with dregs; A described tower top alcohol steam part introduces condensation in the forced circulating reboiler of topping still, and condensation latent heat is for heating topping still, and phlegma is as trim the top of column; Another part alcohol steam introduces molecular sieve dehydration unit, and obtain light wine that concentration is 60% ~ 80%V/V and dehydrated alcohol finished product steam, crude alcohol tank introduced by light wine, namely obtains process of alcohol products after dehydrated alcohol finished product vapor condensation; Described useless wine with dregs is discharged by bottom combined column;
Being undertaken concentrating and being separated by introducing rectifying tower after the thick wine preheating in crude alcohol tank, obtaining respectively heating up in a steamer water more than at the bottom of the alcohol of potato spirit, tower top alcohol steam and tower; The described alcohol containing potato spirit cools after drawing above charging layer, then dilute with water washing, and the lower floor shifted out after layering is potato spirit dilution washing light wine, enters crude alcohol tank; Described tower top alcohol steam introduces condensation in the forced circulating reboiler of combined column, and the latent heat of condensation is used for heating in combination tower, and 40% ~ 70% of phlegma mass rate is back to rectifying tower top layer column plate, and all the other phlegmas are introduced combined column and again distilled; Heat up in a steamer water more than at the bottom of described tower to draw by the bottom of rectifying tower;
The described fermenting-ripening wine with dregs entering topping still degassing stages utilizes to give up wine with dregs at the bottom of topping still alcohol steam, topping still tower and carry out preheating from the dehydrated alcohol finished product steam of molecular sieve dehydration unit; Described rectifying tower passes into live steam by tower bottom reboiler and carries out heat supply, heat up in a steamer after water carries out preheating to thick wine more than the vapour that after heat supply, steam generation condensation obtains coagulates at the bottom of water and rectifying tower, a part return boiler as reuse water, another part through cooling after for diluting the alcohol containing potato spirit;
In described workshop section (4), the working pressure of each distillation tower, tower top temperature are respectively:
Topping still tower top operation pressure is-70 ~-30kPa, tower top temperature 55 ~ 75 DEG C;
Combined column tower top working pressure is 0 ~ 100kPa, tower top temperature 78 ~ 102 DEG C;
Rectifying tower tower top working pressure is 300 ~ 520kPa, tower top temperature 110 ~ 135 DEG C.
2. the clean preparation method of a kind of starch base alcohol fuel according to claim 1, is characterized in that: from the CO that distiller's yeast tank and all fermentor tanks produce during the fermentation in described workshop section (3)
2with in workshop section (4) from topping still degassing stages discharge CO
2jointly enter the recovery that washing tower carries out carbonic acid gas.
3. the clean preparation method of a kind of starch base alcohol fuel according to claim 1, is characterized in that: the molecular sieve dehydration unit in described workshop section (4) is made up of adsorbing tower with molecular sieve and Analytic Tower; Described adsorbing tower with molecular sieve working pressure is 0 ~ 150kPa, and molecular sieve Analytic Tower working pressure is-80 ~ 0kPa.
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| CN102628067B (en) * | 2012-01-13 | 2013-11-20 | 安徽中粮生化燃料酒精有限公司 | Alcohol production method |
| WO2013139027A1 (en) * | 2012-03-22 | 2013-09-26 | 天津大学 | Method for producing alcohol from potato materials |
| CN104293839A (en) * | 2014-10-11 | 2015-01-21 | 吉林省博大生化有限公司 | Thick mash fermentation production process |
| CN106636223B (en) * | 2016-09-27 | 2020-08-14 | 台州中知英健机械自动化有限公司 | Processing method for producing alcohol by using cassava residues and cassava |
| CN106636221B (en) * | 2016-09-30 | 2020-10-30 | 台州中知英健机械自动化有限公司 | Acid-free fermentation method for producing alcohol by using starchy raw material |
| CN106480107A (en) * | 2016-11-03 | 2017-03-08 | 长春吉粮天裕生物工程有限公司榆树分公司 | The new method of Alcohol Production pre-cooked |
| CN109266694A (en) * | 2017-07-18 | 2019-01-25 | 冯长林 | A kind of multi-products joint production process such as ethyl alcohol |
| CN107974467A (en) * | 2017-12-06 | 2018-05-01 | 广东中科天元新能源科技有限公司 | A kind of technique that alcohol fuel is produced as raw material using starchiness and lignocellulosic |
| CN108103112B (en) * | 2018-02-09 | 2021-12-21 | 广东中科天元新能源科技有限公司 | Process for producing fuel ethanol by using corn starch as raw material |
| CN109762851B (en) * | 2018-12-27 | 2020-10-30 | 吉林中粮生化有限公司 | Method for producing fuel ethanol and byproduct rice DDGS by processing rice |
| CN110922302B (en) * | 2019-12-16 | 2023-02-17 | 广东中科天元新能源科技有限公司 | Differential pressure distillation dehydration production process of fuel ethanol double-negative-pressure rough distillation tower |
| CN111500648B (en) * | 2020-04-09 | 2022-08-19 | 中粮营养健康研究院有限公司 | Method for liquefying starchy material |
| CN112063659B (en) * | 2020-08-23 | 2021-09-17 | 宿州中粮生物化学有限公司 | Production process of absolute ethyl alcohol |
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