CN105733905A - Method for preparing alcohol through slagless distillation - Google Patents
Method for preparing alcohol through slagless distillation Download PDFInfo
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- CN105733905A CN105733905A CN201410751356.9A CN201410751356A CN105733905A CN 105733905 A CN105733905 A CN 105733905A CN 201410751356 A CN201410751356 A CN 201410751356A CN 105733905 A CN105733905 A CN 105733905A
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Abstract
The invention relates to a method for preparing alcohol through slagless distillation. In matured fermenting mash, alcohol, water and fermentation by-products are completely separated from insoluble solids by adopting a secondary separation technology, so that the inactive ingredients do not participate in the distillation process. With the adoption of the technology, the matured fermenting mash is effectively separated by adopting the secondary separation technology, so that the inactive ingredients do not participate in the distillation process, therefore, the heat loss is reduced by 20-30% compared with that of the traditional total-slag distillation, and finally, the operation cost of an enterprise is greatly reduced; the stripping of the inactive ingredients is beneficial for the purification for the final product, namely, alcohol; the impurities including peel, dregs, fiber and protein are separated and removed before distillation, so that the formation of mash scale in a tower is reduced, the operational stability is improved, and meanwhile, the overhaul and maintenance of the device are facilitated; the insoluble solids are removed, so that the content of waste dregs in residual liquor generated by distillation is reduced, and the sewage treatment pressure in the environmental emission is reduced.
Description
Technical field
The present invention relates to ethanol preparing technical field, especially relate to a kind of method producing ethanol without slag distillation.
Background technology
In Alcohol Production, with potato class, frumentum etc. has multiple operation for raw material production ethanol, and including pulverizing steaming and decocting, fermentation and distillation process, wherein main power consumption is steaming and decocting and distillation workshop section, wherein again to distill workshop section's power consumption.Distillation is the key link in alcohol production process, and it is not only related to yield and the quality of final products, and the energy expenditure of distillation procedure accounts for the 60%-80% of whole production process energy consumption.The edible ethanol production industry of full slag distillation procedure is adopted for the existing ubiquity of China and great majority, there is some drawback following: (1) fermenting-ripening wine with dregs is a heterogeneous mixed liquor of complicated multicomponent, it is by water (75%-90%, w/w), dry (4%-10%, w/w), ethanol and other volatile material (6%-15%, w/w) constitute, full slag fermenting-ripening wine with dregs enters the distillation stage, invalid solid content dregs participate in heating power and separate, and cause meaningless heat energy loss；(2) the useless component that still-process participates in is too much, is unfavorable for the purification of ethanol；(3) distillation column (wine with dregs tower or preheater) fouling and clogging problem can be caused, especially the stifled tower problem of wine with dregs tower, it is that Distallation systm can not the main restricting factor of long-term operation, wine with dregs dirt is deposited on equipment, by insoluble salt on inner surface of pipeline, silt particle, fiber, starch, protein, dextrin, sugar, the multi-component compound that yeast thalline and other glycolysis metabolism by-product etc. form, generally it is attached to ripe wine with dregs preheater, on the tube wall of reboiler and distillation column tower tray and tower part, often result in feeding temperature to reduce, at the bottom of tower, between each plate, the temperature difference strengthens, top vacuum degree raises, race wine at the bottom of tower can be caused time serious, ultimately result in production can not be normally carried out；(4) what affect that distillation column runs stablizes, and interrelates between each variable, and Rhizoma Nelumbinis of intersecting is closed, and technology controlling and process is complex, due to the composition of distilling material too much make still-process reach material balance, heat balance time long, power consumption is big；(5) full slag enters still-process, slightly evaporating with the waste liquid of stage of rectification generation, residue too much, subsequent evaporation concentration operation very easily causes fouling and blocking, strengthens sewage treatment load.
Summary of the invention
It is an object of the invention to provide a kind of method producing ethanol without slag distillation, solve in the edible ethanol production process of prior art, full slag distillation process high energy consumption, residual liquid impurity content are high, equipment operating pressure is high and the problem of environment protection emission high in cost of production.
This invention address that technical problem be the technical scheme is that a kind of method producing ethanol without slag distillation, comprise the following steps that
A, by fermentation ripe wine with dregs pressure filter filter pressing obtain mash；
B, by described mash centrifuge secondary separation, remove further residue and obtain fermentation liquid；
C, undertaken distilling prepared ethanol by described fermentation liquid.
In the method producing ethanol without slag distillation of the present invention, in step, the filter press cloth in described pressure filter is 60 order-100 orders.
In the method producing ethanol without slag distillation of the present invention, in stepb, described centrifuge is butterfly centrifugal machine.
In the method producing ethanol without slag distillation of the present invention, in step C, still-process includes:
S1, Wen Ta: regulate steam pressure at 0.1-0.3Mpa, when topping still top temperature is raised to 98 DEG C-100 DEG C, starts to steam water and keep topping still top temperature to be 102 DEG C-104 DEG C；
S2, slightly evaporate: send in topping still after the fermentation liquor preheater after separating in step B is preheated to 70 DEG C-75 DEG C, the tower top temperature of topping still is down to 98 DEG C-100 DEG C by 102 DEG C-104 DEG C, the column bottom temperature of topping still controls at 110 DEG C-113 DEG C, the Steam pressure control of topping still is at 0.12-0.15Mpa, cool down then through condenser after slightly evaporating, obtain the wine vapour mixture of concentration 40%-50%；
S3, rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.3Mpa-0.6Mpa, temperature in rectifying column controls at 92 DEG C-94 DEG C, in at the bottom of rectifying column, Stress control is at 0.02Mpa-0.025Mpa, the column bottom temperature of rectifying column controls at 108 DEG C-110 DEG C, condenser temperature controls at 65 DEG C-70 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at the ethanol of rectifying column middle and upper part volume withdrawl concentration >=95%.
In the method producing ethanol without slag distillation of the present invention, in step S2, fermentation liquid was first sent into impurity discharging device before sending in topping still and is separated by low boiling point component, then via condenser, low boiling point component was cooled down.
In the method producing ethanol without slag distillation of the present invention, in step S3 after extraction ethanol, by plate type heat exchanger, ethanol cooling is water-cooled to 20 DEG C.
In the method producing ethanol without slag distillation of the present invention, the ripe wine with dregs in step A is by obtaining carrying out fermentation after Rhizoma Dioscoreae starch liquefacation, saccharifying.
In the method producing ethanol without slag distillation of the present invention, described Rhizoma Dioscoreae starch carries out saccharifying by the saccharifying enzyme that vigor is 80000u/ml-120000u/ml, and the consumption of described saccharifying enzyme is according to 100u/g-200u/g starch.
In the method producing ethanol without slag distillation of the present invention, add yeast wine zymocyte after described Rhizoma Dioscoreae starch saccharification and carry out biofermentation, obtain ripe wine with dregs；Described yeast wine zymocyte is by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518 is cultivated and obtained, wherein the Classification And Nomenclature of Wine brewing yeast strain is saccharomyces cerevisiae (Saccharomycescerevisaie), this bacterial strain on August 15th, 2014 in China Committee for Culture Collection of Microorganisms's common micro-organisms center (address: Yard 1, BeiChen xi Road, Chaoyang District, Beijing City 3, Institute of Microorganism, Academia Sinica) preservation.
In the method producing ethanol without slag distillation of the present invention, the zymogenic interpolation mass ratio of described yeast wine is 10-15%.
Implement the method producing ethanol without slag distillation of the present invention, have the advantages that present invention process utilizes secondary separation technology by the ethanol in fermenting-ripening wine with dregs, water and fermentation byproduct (alcohol, aldehyde, acid, the components such as ester) and insolubility solid content (yeast thalline, skin slag, fiber, the impurity such as insoluble starch and albumen) it has been completely separated, nullified composition is not involved in still-process, this technique is adopted to be advantageous in that: (1) adopts secondary separation technology to efficiently separate fermenting-ripening wine with dregs, nullified composition is not involved in still-process, heat energy loss is compared the full slag distillation of tradition and is reduced 20-30%, enterprise operation cost is substantially reduced；(2) stripping of invalid components is conducive to the purification of final products ethanol；(3) separating removal skin slag before distillation, fiber, the impurity such as insoluble starch and albumen reduces the formation of wine with dregs dirt in tower, also makes the maintenance of equipment and maintenance be more easy to and carry out while increasing operational stability；(4) insolubility solid content removes the waste liquid, the waste residue that decrease distillation and produce, reduces the pressure of environment protection emission.
Detailed description of the invention
Below in conjunction with embodiment, the method without slag distillation production ethanol of the present invention is described further:
The power-saving technology of research still-process, distillation procedure is made to reach Optimal Control energy-saving effect on the basis realize qualified products, this is conducive to enterprise to reduce operating cost in energy-conservation process, and the pressure of environment thus improving the market competitiveness, is reached good sustainable development by emissions-reducing.
Present invention process utilizes secondary separation technology the ethanol in fermenting-ripening wine with dregs, water and fermentation byproduct components such as () alcohol, aldehyde, acid, esters and insolubility solid content impurity such as () yeast thalline, cot, fiber, insoluble starch and albumen to be completely separated, nullified composition is not involved in still-process, namely the present invention adopts and prepares ethanol without slag distillation technique, and detailed process includes:
A, by fermentation the pressure filter filter pressing that ripe wine with dregs filter press cloth is 60 order-100 orders obtain mash；Preferred maturity wine with dregs is by obtaining carrying out fermentation after Rhizoma Dioscoreae starch liquefacation, saccharifying；
B, fermentation liquid is put into disk centrifugal separator, under the rotating speed of at least 2000 revs/min, carry out secondary centrifuging separation, obtain fermentation residue and fermentation liquid；
C, being undertaken distilling prepared ethanol by fermentation liquid, its still-process includes:
S1, Wen Ta: regulate steam pressure at 0.1-0.3Mpa, when topping still top temperature is raised to 98 DEG C-100 DEG C, starts to steam water and keep topping still top temperature to be 102 DEG C-104 DEG C；
S2, slightly evaporate: first sending into impurity discharging device after the fermentation liquor preheater after separating in step B is preheated to 70 DEG C-75 DEG C and be re-fed in topping still, the purpose sending into impurity discharging device is to be separated by lower boiling aldehydo-ester composition, is further purified the fermentation liquid entering distillation；The tower top temperature of topping still is down to 98 DEG C-100 DEG C by 102 DEG C-104 DEG C, the column bottom temperature of topping still controls at 110 DEG C-113 DEG C, the column bottom temperature of rectifying column controls at 108 DEG C-110 DEG C, the Steam pressure control of topping still is at 0.12-0.15Mpa, cool down then through condenser after slightly evaporating, obtain the fume mixture of 40%-50%；The above-mentioned lower boiling aldehydo-ester composition discharged by impurity discharging device cools down via condenser, it is possible to be applied, and improves comprehensive utilization ratio；
S3, rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.3Mpa-0.6Mpa, temperature in rectifying column controls at 92 DEG C-94 DEG C, in at the bottom of rectifying column, Stress control is at 0.02Mpa-0.025Mpa, condenser temperature controls at 65 DEG C-70 DEG C, the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, ethanol at rectifying column middle and upper part volume withdrawl concentration >=95%, it is preferably the ethanol of 95%-96.5%, when extraction ethanol, the temperature of ethanol must not be higher than 28 DEG C, preferably by plate type heat exchanger, ethanol cooling is water-cooled to 20 DEG C.
Still-process further particularly as follows:
S1, Wen Ta: supply water to each condenser, observe flow；By the liquid level adjustment of topping still and rectifier bottoms glass tubing 1/2-2/3 height；Regulate the admission valve of topping still, rectifying column, bleed off the cooling water of gas-distributing cylinder and pipeline, slowly open total device door to steam supply in each tower, start temperature tower, and progressively steam pressure is regulated at 0.1-0.3Mpa, when topping still jacking is to 98-100 DEG C, start to steam water and keep temperature 102--104 DEG C of topping still top, when having backflow and topping still and rectifier bottoms normally can discharge waste water depending on each condenser, carry out equipment again, instrument, pipeline, valve check comprehensively, whether normal operation, with or without running leakage phenomenon, can start to feed intake；
S2, slightly evaporate: with pump, fermentation liquor preheater is sent into impurity discharging device, subsequently into topping still；When topping still top temperature is dropped to 98-100 DEG C by 102--104 DEG C, carry out normal operating, and require to determine each tower steam consumption, progressively adjust condenser reflux liquid temp；Topping still bottom temp drops to 110--113 DEG C, when rectifier bottoms temperature drops to 108-110 DEG C, can carry out continuing normal operating；The Steam pressure control of topping still is 0.12-0.15Mpa., and steam is entered by the bottom of tower, adopts direct steam heating, and the height of steam consumption and pressure can change at any time according to operation planning, does not run wine with waste liquid at the bottom of tower and is as the criterion；Before wherein fermentation liquid enters impurity discharging device, preheating temperature to 70-75 DEG C, the aldehydo-ester of impurity discharging device becomes dispensing impurity discharging device cooled device to cool down；Topping still enters the amount of fermentation liquid, determines according to plan workload, when ensureing that each tower is temperature-resistant, adjusts input and the steam input of fermentation liquid；Topping still top temperature controls at 98--100 DEG C, the height of the stable 1/2-2/3 in glass tubing liquid level at the bottom of topping still；
S3, rectification: enter steam, the steam pressure of rectifying column is 0.3-0.6Mpa.；Level stability at the bottom of rectifying column the 1/2 2/3 of glass-tube liquid level meter height, the concentration slightly evaporating the semi-finished product (fume mixture) obtained controls at 45-50% (V)；In rectifying column, temperature is stable at 92--94 DEG C；The extraction process of finished product ethanol is as follows: extracted by the 1-6 valve liquid phase of rectifying column, sends into finished product cooler and first cools down, is then delivered to finished product measuring tank, the ethanol (V) of finished wine precision >=95%, and finished product ethanol temperature must not exceed 28 DEG C；Extract output number, in rectifying column, temperature 92--94 DEG C is reference frame, if exceeding this temperature, then takes finished product less, otherwise then takes finished product more；Finished product ethanol is self-produced from the used time, takes the 1-2, top of finished product unlatching valve and takes, and extracts foreshot again；During finished product export trade, take finished product position to be displaced downwardly to the 5-6 valve and take, in rectifying column, add alkali or potassium permanganate simultaneously, for reducing acid in ethanol finished product, ester content, foreshot's extracted amount accounts for the 1.5-2% of finished product ethanol, and this finished wine extract Iuality meets GB10343 2002 and eats general grade standard；In at the bottom of rectifying column, Stress control is at 0.02-0.025Mpa.；The temperature of second and third condenser controls at 65--70 DEG C；The condensed fluid of each condenser is transported to rectifying tower top by reflux pump, enters measuring tank at the condensed device of rectifier extraction finished product ethanol, takes out Alcohols,fusel from rectifying column middle and upper part and enters basin, and essence tower bottom discharges exhausted water.
Table 1 shows that the present invention distills the full slag distillation with prior art without slag and prepares the contrast experiment of ethanol, by experimental result it can be seen that consume energy few without slag distillation, the pollution that residual liquid in turn results in less is little, still-process tower stable, not stifled, equipment requirements is low, reduces preparation cost.Table 1:
| Distill without slag | Full slag distills | |
| The steam consumption quantity of ethanol per ton | 0.73 ton | 0.86 ton |
| Discharge: residual liquid COD | 6000-8000 | 18000-23000 |
| Produce preparation process | Not stifled tower tray, crucial manufacturing parameter controls stable | Very easily block tower tray, poor stability |
| Select implementation difference | Ordinary Centrifugal Pumps | Without blocking volume type rotor pump or piston pump |
Illustrate below by multiple embodiments and carry out the detailed process without slag distillation with different material.
Embodiment 1:
nullDioscorea zingiberensis is carried out，Carry out remove impurity simultaneously，Washings use through natural sedimentation Posterior circle，To clean、Dioscorea zingiberensis pulverizer after remove impurity is pulverized，Add water and grind to form the slurry of granularity 2mm，Wherein the solid content of slurry is 20% by weight percentage，The vigor of adding slurry into is the α-amylase of 40000u/ml，Consumption is according to 10u/g starch，Carry out enzymatic liquefaction and obtain starch fluid，Temperature during enzymatic liquefaction controls at 100 DEG C，The time of enzymatic liquefaction is 90min，The starch fluid temperature of post liquefaction is down to 60 DEG C，In starch fluid, addition vigor is the α-1 of 100000u/ml,4-glucose hydrolysis enzyme glycolysis 40min obtains converted mash，α-1,4-glucose hydrolysis enzyme dosage is according to 150u/g starch，Converted mash adds yeast wine zymocyte and carries out biofermentation，Obtain ripe wine with dregs，This yeast wine zymocyte is cultivated obtain by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518，The zymogenic adding proportion of yeast wine is 10%，The temperature that converted mash carries out fermenting controls at 30 DEG C，Fermentation time is 40h，Ripe wine with dregs is obtained mash by being furnished with the pressure filter filter pressing of 100 orders，Then again through butterfly centrifugal machine mash separated further and obtain fermentation liquid.
Then, being undertaken distilling prepared ethanol by distillation column by fermentation liquid, still-process includes: 1. temperature tower: regulate steam pressure at 0.1Mpa, when topping still top temperature is raised to 98 DEG C, starts to steam water and keeps topping still top temperature to be 102 DEG C；2. slightly evaporate: the fermentation liquor preheater after separating is preheated to 70 DEG C, send into impurity discharging device and enter back into topping still, the tower top temperature of topping still is down to 98 DEG C by 102 DEG C, the column bottom temperature of topping still controls at 110 DEG C, the column bottom temperature of rectifying column controls at 108 DEG C, the Steam pressure control of topping still, at 0.12Mpa, obtains the fume mixture of 45% after slightly evaporating；3. rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.3Mpa, temperature in rectifying column controls at 92 DEG C, in at the bottom of rectifying column, Stress control is at 0.02Mpa, condenser temperature controls at 65 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at rectifying tower top extraction finished product ethanol, finished wine was proficient in plate type heat exchanger and ethanol cooling was water-cooled to 20 DEG C, and ethanol finished-product volume concentration is 95.5%.
Embodiment 2:
nullDioscorea zingiberensis is carried out，Carry out remove impurity simultaneously，Washings use through natural sedimentation Posterior circle，To clean、Dioscorea zingiberensis pulverizer after remove impurity is pulverized，Add water and grind to form the slurry of granularity 1mm，Wherein the solid content of slurry is 30% by weight percentage，The vigor of adding slurry into is that the beta amylase of 30000u/ml carries out enzymatic liquefaction and obtains starch fluid，Beta amylase consumption is according to 12u/g starch，Temperature during enzymatic liquefaction controls at 85 DEG C，The time of enzymatic liquefaction is 110min，The starch fluid temperature of post liquefaction is down to 65 DEG C，In starch fluid, addition vigor is that the beta-glucosidase enzyme glycolysis 60min of 110000u/ml obtains converted mash，Beta-glucosidase enzyme dosage is according to 200u/g starch，Converted mash adds yeast wine zymocyte and carries out biofermentation，Obtain the karusen of maturation，This yeast wine zymocyte is cultivated obtain by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518，The zymogenic adding proportion of yeast wine is 15%，The temperature that converted mash carries out fermenting controls at 34 DEG C，Fermentation time is 72h，Ripe wine with dregs is obtained mash by being furnished with the pressure filter filter pressing of 60 orders，Then again through butterfly centrifugal machine, mash is carried out solid-liquid separation further and obtain fermentation liquid.
Then, being undertaken distilling prepared ethanol by distillation column by fermentation liquid, still-process includes: 1. temperature tower: regulate steam pressure at 0.3Mpa, when topping still top temperature is raised to 100 DEG C, starts to steam water and keeps topping still top temperature to be 104 DEG C；2. slightly evaporate: the fermentation liquor preheater after separating is preheated to 75 DEG C, send into impurity discharging device and enter back into topping still, the tower top temperature of topping still is down to 100 DEG C by 104 DEG C, the column bottom temperature of topping still controls at 113 DEG C, the column bottom temperature of rectifying column controls at 110 DEG C, the Steam pressure control of topping still, at 0.15Mpa, obtains the fume mixture of 50% after slightly evaporating；3. rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.6Mpa, temperature in rectifying column controls at 94 DEG C, in at the bottom of rectifying column, Stress control is at 0.025Mpa, condenser temperature controls at 70 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at rectifying tower top extraction finished product ethanol, finished wine was proficient in plate type heat exchanger and ethanol cooling was water-cooled to 28 DEG C, and ethanol finished-product volume concentration is 95%.
Embodiment 3:
nullDioscorea zingiberensis is carried out，Carry out remove impurity simultaneously，Washings use through natural sedimentation Posterior circle，To clean、Dioscorea zingiberensis pulverizer after remove impurity is pulverized，Add water and grind to form the slurry of granularity 1.5mm，Wherein the solid content of slurry is 15% by weight percentage，The vigor of adding slurry into is the α-1 of 20000u/ml，6 key debranching enzymes carry out enzymatic liquefaction and obtain starch fluid，α-1，6 key debranching enzyme consumptions are according to 8u/g starch，Temperature during enzymatic liquefaction controls at 110 DEG C，The time of enzymatic liquefaction is 120min，The starch fluid temperature of post liquefaction is down to 63 DEG C，In starch fluid, addition vigor is the α-1 of 120000u/ml,4-glucose hydrolysis enzyme glycolysis 20min obtains converted mash，α-1,4-glucose hydrolysis enzyme dosage is according to 100u/g starch，Converted mash adds yeast wine zymocyte and carries out biofermentation，Obtain maturing fermentation wine with dregs，This yeast wine zymocyte is cultivated obtain by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518，The zymogenic adding proportion of yeast wine is 13%，The temperature that converted mash carries out fermenting controls at 36 DEG C，Fermentation time is 68h，Ripe wine with dregs is obtained mash by being furnished with the pressure filter filter pressing of 80 orders，Then again through butterfly centrifugal machine, mash is carried out further solid-liquid separation and obtain fermentation liquid.
Then, being undertaken distilling prepared ethanol by distillation column by fermentation liquid, still-process includes: 1. temperature tower: regulate steam pressure at 0.2Mpa, when topping still top temperature is raised to 99 DEG C, starts to steam water and keeps topping still top temperature to be 103 DEG C；2. slightly evaporate: the fermentation liquor preheater after separating is preheated to 73 DEG C, send into impurity discharging device and enter back into topping still, the tower top temperature of topping still is down to 99 DEG C by 103 DEG C, the column bottom temperature of topping still controls at 112 DEG C, the column bottom temperature of rectifying column controls at 109 DEG C, the Steam pressure control of topping still, at 0.14Mpa, obtains the fume mixture of 40% after slightly evaporating；3. rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.5Mpa, temperature in rectifying column controls at 93 DEG C, in at the bottom of rectifying column, Stress control is at 0.022Mpa, condenser temperature controls at 68 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at rectifying tower top extraction finished product ethanol, finished wine was proficient in plate type heat exchanger and ethanol cooling was water-cooled to 25 DEG C, and ethanol finished-product volume concentration is 96.5%.
Embodiment 4:
nullDioscorea zingiberensis is carried out，Carry out remove impurity simultaneously，Washings use through natural sedimentation Posterior circle，To clean、Dioscorea zingiberensis pulverizer after remove impurity is pulverized，Add water and grind to form the slurry of granularity 1.8mm，Wherein the solid content of slurry is 23% by weight percentage，The vigor of adding slurry into is that the α-amylase of 30000u/ml carries out enzymatic liquefaction and obtains starch fluid，α-amylase consumption is according to 11u/g starch，Temperature during enzymatic liquefaction controls at 105 DEG C，The time of enzymatic liquefaction is 60min，The starch fluid temperature of post liquefaction is down to 62 DEG C，In starch fluid, addition vigor is the α-1 of 100000u/ml,4-glucose hydrolysis enzyme glycolysis 30min obtains converted mash，α-1,4-glucose hydrolysis enzyme dosage is according to 165u/g starch，Converted mash adds yeast wine zymocyte and carries out biofermentation，Obtain maturing fermentation wine with dregs，This yeast wine zymocyte is cultivated obtain by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518，The zymogenic adding proportion of yeast wine is 12%，The temperature that converted mash carries out fermenting controls at 28 DEG C，Fermentation time is 50h，Ripe wine with dregs is obtained mash by being furnished with the pressure filter filter pressing of 90 orders，Then again through butterfly centrifugal machine, mash is carried out solid-liquid separation further and obtain fermentation liquid.
Then, being undertaken distilling prepared ethanol by distillation column by fermentation liquid, still-process includes: 1. temperature tower: regulate steam pressure at 0.15Mpa, when topping still top temperature is raised to 99 DEG C, starts to steam water and keeps topping still top temperature to be 104 DEG C；2. slightly evaporate: the fermentation liquor preheater after separating is preheated to 74 DEG C, send into impurity discharging device and enter back into topping still, the tower top temperature of topping still is down to 99 DEG C by 104 DEG C, the column bottom temperature of topping still controls at 111 DEG C, the column bottom temperature of rectifying column controls at 108 DEG C, the Steam pressure control of topping still, at 0.13Mpa, obtains the fume mixture of 47% after slightly evaporating；3. rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.4Mpa, temperature in rectifying column controls at 93 DEG C, in at the bottom of rectifying column, Stress control is at 0.024Mpa, condenser temperature controls at 66 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at rectifying tower top extraction finished product ethanol, finished wine was proficient in plate type heat exchanger and ethanol cooling was water-cooled to 20 DEG C, and ethanol finished-product volume concentration is 99%.
Embodiment 5:
After fermented for the Caulis Sacchari sinensis after pulverizing, obtain ripe wine with dregs, by ripe wine with dregs by be furnished with 100 order filter press cloths pressure filter filter pressing, then carry out solid-liquid separation again through butterfly centrifugal machine and obtain fermentation liquid.Then, being undertaken distilling prepared ethanol by distillation column by fermentation liquid, still-process includes: 1. temperature tower: regulate steam pressure at 0.1Mpa, when topping still top temperature is raised to 98 DEG C, starts to steam water and keeps topping still top temperature to be 102 DEG C；2. slightly evaporate: the fermentation liquor preheater after separating is preheated to 70 DEG C, send into impurity discharging device and enter back into topping still, the tower top temperature of topping still is down to 98 DEG C by 102 DEG C, the column bottom temperature of topping still controls at 110 DEG C, the column bottom temperature of rectifying column controls at 108 DEG C, the Steam pressure control of topping still, at 0.12Mpa, obtains the fume mixture of 45% after slightly evaporating；3. rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.3Mpa, temperature in rectifying column controls at 92 DEG C, in at the bottom of rectifying column, Stress control is at 0.02Mpa, condenser temperature controls at 65 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at rectifying tower top extraction finished product ethanol, finished wine was proficient in plate type heat exchanger and ethanol cooling was water-cooled to 20 DEG C, and ethanol finished-product volume concentration is 95.5%.
It should be appreciated that for those of ordinary skills, it is possible to being improved according to the above description or convert, all these improve or convert within the protection domain that all should belong to claims of the present invention.
Claims (10)
1. the method producing ethanol without slag distillation, it is characterised in that comprise the following steps that
A, by fermentation ripe wine with dregs pressure filter filter pressing obtain mash；
B, by described mash centrifuge secondary separation, remove further residue and obtain fermentation liquid；
C, undertaken distilling prepared ethanol by described fermentation liquid.
2. the method producing ethanol without slag distillation according to claim 1, it is characterised in that in step, the filter press cloth in described pressure filter is 60 order-100 orders.
3. the method producing ethanol without slag distillation according to claim 1, it is characterised in that in stepb, described centrifuge is butterfly centrifugal machine.
4. the method producing ethanol without slag distillation according to claim 1, it is characterised in that in step C, still-process includes:
S1, Wen Ta: regulate steam pressure at 0.1-0.3Mpa, when topping still top temperature is raised to 98 DEG C-100 DEG C, starts to steam water and keep topping still top temperature to be 102 DEG C-104 DEG C；
S2, slightly evaporate: send in topping still after the fermentation liquor preheater after separating in step B is preheated to 70 DEG C-75 DEG C, the tower top temperature of topping still is down to 98 DEG C-100 DEG C by 102 DEG C-104 DEG C, the column bottom temperature of topping still controls at 110 DEG C-113 DEG C, the Steam pressure control of topping still is at 0.12-0.15Mpa, cool down then through condenser after slightly evaporating, obtain the wine vapour mixture of concentration 40%-50%；
S3, rectification: fume mixture enters in rectifying column and carries out rectification, rectifying column Steam pressure control is at 0.3Mpa-0.6Mpa, temperature in rectifying column controls at 92 DEG C-94 DEG C, in at the bottom of rectifying column, Stress control is at 0.02Mpa-0.025Mpa, the column bottom temperature of rectifying column controls at 108 DEG C-110 DEG C, condenser temperature controls at 65 DEG C-70 DEG C, and the condensed fluid of each condenser is transported to rectifying tower top by reflux pump, at the ethanol of rectifying column middle and upper part volume withdrawl concentration >=95%.
5. the method producing ethanol without slag distillation according to claim 4, it is characterised in that in step S2, fermentation liquid was first sent into impurity discharging device before sending in topping still and separated by low boiling point component, then via condenser, low boiling point component was cooled down.
6. the method producing ethanol without slag distillation according to claim 4, it is characterised in that in step S3 after extraction ethanol, by plate type heat exchanger, ethanol cooling is water-cooled to 20 DEG C.
7. the method producing ethanol without slag distillation according to claim 1, it is characterised in that the ripe wine with dregs in step A is by obtaining carrying out fermentation after Rhizoma Dioscoreae starch liquefacation, saccharifying.
8. the method producing ethanol without slag distillation according to claim 7, it is characterised in that described Rhizoma Dioscoreae starch carries out saccharifying by the saccharifying enzyme that vigor is 80000u/ml-120000u/ml, and the consumption of described saccharifying enzyme is according to 100u/g-200u/g starch.
9. the method producing ethanol without slag distillation according to claim 7, it is characterised in that add yeast wine zymocyte after described Rhizoma Dioscoreae starch saccharification and carry out biofermentation, obtain ripe wine with dregs；Described yeast wine zymocyte is by being deposited in China Committee for Culture Collection of Microorganisms's common micro-organisms center and Wine brewing yeast strain that preserving number is CGMCCNo.9518 is cultivated and obtained.
10. the method producing ethanol without slag distillation according to claim 9, it is characterised in that the zymogenic interpolation mass ratio of described yeast wine is 10-15%.
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