CN106399388A - Ethyl alcohol processing method by clear solution of distiller grain and corn - Google Patents
Ethyl alcohol processing method by clear solution of distiller grain and corn Download PDFInfo
- Publication number
- CN106399388A CN106399388A CN201610858697.5A CN201610858697A CN106399388A CN 106399388 A CN106399388 A CN 106399388A CN 201610858697 A CN201610858697 A CN 201610858697A CN 106399388 A CN106399388 A CN 106399388A
- Authority
- CN
- China
- Prior art keywords
- wine
- tower
- rectifying column
- reboiler
- water scrubber
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/58—Reaction vessels connected in series or in parallel
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
- C12M43/02—Bioreactors or fermenters combined with devices for liquid fuel extraction; Biorefineries
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
Landscapes
- Organic Chemistry (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Zoology (AREA)
- Health & Medical Sciences (AREA)
- Wood Science & Technology (AREA)
- Engineering & Computer Science (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Genetics & Genomics (AREA)
- Microbiology (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Biotechnology (AREA)
- Biochemistry (AREA)
- Sustainable Development (AREA)
- Biomedical Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Molecular Biology (AREA)
- Clinical Laboratory Science (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
The invention relates to an ethyl alcohol processing method, and particularly relates to an ethyl alcohol processing method by clear solution of distillers grain and corn; the method includes steps (1) pretreatment; (2) cooking; (3) saccharification; (4) fermentation; (5) distilling; (6) back recycling treatment of distiller grain. According to the invention, ethyl alcohol is fermented by recycling and using corn powder after starch is extracted; meanwhile, distiller grain is further recycled to produce high protein feed and edible oil; during the whole alcoholic fermentation process, the fermentation technique applies acid-free diastatic fermentation, improved five-tower distilling process and other processes, so as to further reach the purposes of prolonging the industrial chain of ethyl alcohol production by corn, improving the product additional value, saving energy and reducing consumption, reducing cost and improving the economic benefit.
Description
【Technical field】
The present invention relates to a kind of biomass to alcohol conversion process, add adding of Maize Production ethanol particularly to a kind of utilization distiller's grains liquor
Work method.
【Background technology】
With the continuous consumption of the energy, using fermentative Production ethanol, gradually petroleum replacing Chemical Manufacture ethanol becomes now
One main trend of Biomass Energy Development, due to grain in storage for years to be processed, using Semen Maydiss for the Technology of raw material production ethanol be
The initial pattern of China's alcohol industry development, and more and more ripe, but, in corn alcohol evolution, due to Semen Maydiss
Content of starch is high, and does not allow disposable in processing procedure containing Semen Maydis oil, and corn price is high, for producing ethanol
This is very high, therefore, improves value-added content of product to the Multi-class propagation of raw material, reduce energy during corn fermentation produces ethanol
Consumption is the domestic at present direction studied, and it is using five tower differential pressures that present main flow produces the most frequently used method of corn alcohol process
The way of distillation, such as Chinese patent CN 1736527 A discloses alcohol quinque-towel differential pressure distilling arrangement and its technique, and this technology utilizes
The technical combinations of multinomial recycling heat, make steam consumption index reduce, reach energy-saving effect, but, using the method
Carry out device improvement, relative complex, improving cost is higher, therefore, in corn alcohol processing method it is necessary to solve below several
Individual problem (1) passes through rational modification, reduces the energy resource consumption of alcohol production process further；(2) course of processing of corn alcohol
Improve added value of product, lengthening manufacturing chain further, carry out variation production；(3) the corn alcohol course of processing uses mineral acid
Equipment loss rate is big.
【Content of the invention】
In view of the above is it is necessary to provide the processing method that a kind of utilization distiller's grains liquor adds Maize Production ethanol, can be right
Reducing energy consumption, improves added value of product, reduces the purpose of equipment loss.
For reaching above-mentioned purpose, the technical solution adopted in the present invention is：
The processing method that a kind of utilization distiller's grains liquor adds Maize Production ethanol, methods described procedure of processing is as follows：
(1) pretreatment：The Distillers' grains centrifugation clear liquid that the Semen Maydiss slurry after partial starch is discharged will be extracted with topping still
Carry out spice, obtain the pretreatment slurry that corn starch concentration is 15%-20%；
(2) steaming and decocting：Add the thermostable α-amylase of 10u/g-15u/g to be precooked in the slurry of step (1), precook
Temperature is 50 DEG C -60 DEG C, and the time of precooking is 20min-30min, is heated to 95-105 DEG C and maintains through after-ripening device after the completion of precooking
90min-120min obtains liquefied fermented glutinous rice；
(3) saccharifying：Liquefied fermented glutinous rice entrance brew kettle carries out saccharifying and obtains converted mash, and saccharifying saccharifying enzyme addition is
200u/g-250u/g saccharification temperature is 50 DEG C -65 DEG C, and saccharificatinn period is 20min-30min；
(4) ferment：Fermentation is carried out using continuous fermentation method and obtains ripe wine with dregs, wine part concentration of ripe wine with dregs is 12%-15%
(v/v) distilled when；
(5) distill：Ripe wine with dregs is distilled, distillation mode selects five column distillations, obtains ethanol after distillation；
(6) recycle after distiller grains：The Distillers' grains that still-process topping still is discharged are centrifuged, will after separating
The clear liquid return to step (1) of 50%-60% carries out spice, and the clear liquid of 40%-50% is carried out vacuum evaporation, will after concentration
Albumen feedstuff, with the distiller grains dregs of rice carry out combination drying, pelletize obtains graininess high protein feed, also can be carried out further by concentrated solution
Extraction, carries out refine and produces edible corn oil.
Further, the fermentation tank of described continuous fermentation has 5-10, and continuous ferment process is, to the sugar of the first fermentation tank
Change in wine with dregs and add the active dry yeast after activation according to mass concentration for 40mg/g-60mg/g, after fermentation 12-16h, from first
Fermentation tank is partitioned into about 1/3 mash to the second fermentation tank, then first, second fermentation tank is filled it up with material again；Second fermentation tank is just
Often separate about 1/3 mash after fermentation 12-16h again to the 3rd fermentation tank, then fill it up with material, fermentation, thus along passing down.
Further, described activated yeast method is：By active dry yeast according to dry yeast：Technique water weight ratio is 1:
The ratio of 15-25 is thrown in and is activated in activated yeast tank, and rehydration temperature is 30 DEG C -35 DEG C, and soak time is 20min-
30min, pumps into, after the completion of activation, the tank that spreads cultivation, and adds liquefied fermented glutinous rice in the tank that spreads cultivation, and activated yeast with the weight ratio of liquefied fermented glutinous rice is
1:10-20, incubation time is 6h-8h, delivers to fermentation tank, and 7-10d changes and plants once.
Further, described five column distillations include prefractionation device, topping still, rectifying column, water scrubber, eparating methanol tower and recovery
Tower, is provided with feed exchanger and charging condenser before described prefractionation device, prefractionation device top is connected with pumped vacuum systems, institute
State feed exchanger discharging opening to be connected with prefractionation device charging aperture, feed exchanger air inlet and prefractionation device top gas outlet phase
Even, feed exchanger gas outlet is connected with charging condenser charging aperture, described prefractionation device discharging opening and topping still charging aperture phase
Even, prefractionation device air inlet is connected with topping still top gas outlet, and it is respectively excellent that described charging condenser is provided with two discharging openings
Wine outlet and light wine outlet, charging condenser excellent wine outlet is connected with water scrubber charging aperture, and charging condenser light wine exports and returns
The preposition recycling can installed before receiving tower is connected；
Described topping still bottom is provided with topping still reboiler, and top is connected with pumped vacuum systems, and described topping still boils again
Device is connected with the gas outlet at rectifying column top；
Described rectifying column bottom is provided with rectifying column reboiler, and total number of plates is 95-100 layer, and middle part is provided with Alcohols,fusel and goes out
Mouth d1, top is provided with and is respectively equipped with the excellent wine of rectifying column, the outlet of rectifying column light wine, described rectifying column reboiler and rectifying column top
Gas outlet is connected, and is provided with primary steam Z air inlet, and the excellent wine outlet of described rectifying column is located above the outlet of rectifying column light wine, institute
State the outlet of rectifying column excellent wine to be connected with eparating methanol tower, the preposition recycling can phase of installation before the outlet of described rectifying column light wine and recovery tower
Even；
Described water scrubber top is provided with impurity discharging port and light wine outlet, and bottom is provided with water scrubber reboiler, described water scrubber
Impurity discharging port is located above light wine outlet, is provided with impurity condenser, the outlet of water scrubber light wine and recovery tower after water scrubber impurity discharging port
The preposition recycling can of front installation is connected, and described water scrubber reboiler is connected with rectifying column top gas outlet, described water scrubber discharging
Mouth is connected with rectifying column charging aperture；
Described eparating methanol tower bottom is provided with eparating methanol tower reboiler, and bottom is provided with and takes wine mouth, and middle part is provided with light wine outlet,
Top is provided with impurity discharging port, and top is connected with pumped vacuum systems, and the impurity discharging port of described eparating methanol tower goes out positioned at the light wine of eparating methanol tower
Above mouthful, light wine outlet takes above wine mouth positioned at eparating methanol tower, installs before the light wine outlet of described eparating methanol tower and recovery tower
Preposition recycling can is connected, and described eparating methanol tower reboiler is connected with water scrubber and eparating methanol tower top gas outlet respectively；
Before described recovery tower charging aperture, preposition recycling can is installed, middle part is provided with fusel oil export d2, bottom is provided with
Recovery tower reboiler, described recovery tower reboiler is connected with reclaiming top of tower gas outlet.
Further, described rectifying column and recovery tower bottom are provided with slag-drip opening, are connected with waste water drainage system, waste water is arranged
The indirect steam that place system produces is reclaimed through vapor-recovery system, and indirect steam is passed through recovery tower reboiler to recovery tower
Heated.
Further, described prefractionation device, topping still operating pressure are negative pressure, and rectifying column operating pressure is malleation, described
Water scrubber operating pressure is normal pressure, and eparating methanol tower operating pressure is negative pressure, and recovery tower operating pressure is normal pressure.
Further, the bottom gauge pressure of described prefractionation device be -40kPa～-30kPa, top gauge pressure be -60kPa～-
70kPa；Topping still tower reactor gauge pressure is -40kPa～-30kPa, and tower top gauge pressure is 0kPa～5kPa；Rectifying tower kettle meter pressure is 90
～200kPa, tower top gauge pressure is 70kPa～180kPa；Water scrubber tower reactor gauge pressure be 25～60kPa, tower top gauge pressure be 0kPa～
20kPa；Eparating methanol tower tower reactor gauge pressure is -5kPa～10kPa, and tower top gauge pressure is -25kPa～-40kPa；Recovery tower tower reactor gauge pressure
For 25kPa～30kPa, tower top gauge pressure is 0kPa～5kPa.
Further, described five column distillation work process are：Fermenting-ripening wine with dregs is preheated through feed exchanger, preheating
Enter prefractionation device afterwards and carry out vacuum distillation, the fume that prefractionation device still-process produces is back to feed exchanger and ripe wine with dregs
Carry out heat exchange maturation wine with dregs, then fume carries out condensation and obtains liquid alcohol through charging condenser, and wine degree is less than 50% (v/
V) it is referred to as light wine, wine degree is that 50%-60% (v/v) is referred to as excellent wine, and condensed light wine flows into the preposition recycling can of recovery tower, excellent
Wine enters water scrubber；The part that can not evaporate in prefractionation device is referred to as distiller grains, and distiller grains further flow into topping still and carry out negative pressure steaming
Evaporate；While the fume that topping still produces enters prefractionation device as heating gas, it is incorporated to the fume of prefractionation generation and ripe wine with dregs
Carry out heat exchange in feed exchanger, the distiller grains that topping still produces enter waste water drainage system, the heat of topping still through bottom discharge
Source derives from topping still reboiler, and the steam of topping still reboiler is derived from the indirect steam of rectifying column tower top；Charging condenser
The excellent wine producing enters water scrubber and is washed, and impurity condenses through impurity condenser from tower top and discharges, and water scrubber (4) is in distillation
Process produces excellent wine entrance rectifying column (3) that wine degree is 60%-70% (v/v) and carries out rectification, and water scrubber (4) produces wine degree and is less than
The light wine of 60% (v/v) enters preposition recycling can and is reclaimed, and the thermal source of water scrubber derives from reboiler, water scrubber reboiler
Steam is derived from the indirect steam of rectifying column tower top；Excellent wine from water scrubber is distilled in rectifying column, and still-process produces wine
Spend the excellent wine for 95%-96% (v/v) to collect in the 72-80 layer column plate of rectifying column, produce wine degree and be less than the light of 95% (v/v)
Wine is collected in the 62-70 layer column plate of rectifying column, enters preposition recycling can and is reclaimed, Alcohols,fusel passes through fusel oil export d1Receive
Collection, the thermal source of rectifying column derives from rectifying column reboiler and heats, and a steam part for rectifying column is come from primary steam, a part
Indirect steam from rectifying column tower top；The excellent wine that rectifying column is collected enters eparating methanol tower and carries out vacuum distillation separating methanol, wherein,
Methanol passes through impurity removal port e to be collected and removes, and finished wine was proficient in and takes wine mouth a to collect, and the thermal source of eparating methanol tower derives from eparating methanol tower
Reboiler, the steam source of eparating methanol tower reboiler is in the indirect steam of washing column overhead and eparating methanol tower；Above-mentioned preposition recovery
The light wine that tank reclaims carries out distilling concentration through recovery tower, and the ethanol after distillation concentration sequentially enters water scrubber, rectifying column and takes off
Methanol column carries out washing, rectification, separating methanol, obtain finished product ethanol.
The present invention has the advantages that：
1st, the present invention using extract corn starch after Semen Maydiss slurry be raw material, simultaneously spice process using be useless
Clear liquid after centrifugation for the distiller grains, strengthens the comprehensive utilization in alcoholic fermentation process for the Semen Maydiss, for improving product further
Added value, strengthens the utilization to maize alcohol stillage, is centrifuged production maize gluten feed using maize alcohol stillage, then by jade
Rice gluten feedstuff is extracted further, refine produces edible corn oil, and the waste material that corn fermentation is produced ethanol is carried out effectively
Using prolongation corn processed produces the industrial chain of ethanol, improves value-added content of product, is reduced by diversified product mix
Only utilize the cost of Maize Production ethanol, meanwhile, the saccharifying of the present invention, do not use sulphuric acid, but pass through technique control
System is come antibacterial, that is,：In the saccharifying stage, increase saccharifying enzyme usage amount, reduce saccharificatinn period, improve conversion coefficient, in fermentation stage, increase
Plus yeast amount makes a concentrated effort to finish sweat, suppress the growth of miscellaneous bacteria using the good fertility of yeast, make whole process
Sulphuric acid is not used to decrease the loss to equipment for the sulphuric acid.
2nd, on Steam Recovery utilizes, the present invention adds prefractionation equipment in still-process, first by a part of ripe wine with dregs
Carry out prefractionation, decrease the steam consumption of topping still, reduce production cost, first thick mash is carried out pretreatment simultaneously, improve product
The quality of product charging, reduces the stopping state of equipment；Secondly, also utilize the pressure differential between each column distillation, malleation, normal pressure are steamed
Evaporate the topping still reboiler of the indirect steam waste gas recovery of generation to vacuum distillation, in eparating methanol tower reboiler, to topping still, de-
Methanol column is heated, and reaches secondary steam and utilizes, further up to the purpose of energy-conservation；Again, waste water is also produced by the present invention
Waste heat recycled, be passed through recovery tower reboiler and reused, make full use of still-process generation thermal source, subtract
Lack the waste of steam, reach energy-saving purpose.
3rd, the present invention also further improves to rectifying column, by improving total number of plies of rectifying column, improves and takes wine mouth
The impurity spatial cache of the separation of installation site, more conducively impurity and top of tower, stably improves the quality of alcohol product further.
【Brief description】
Fig. 1 is the process chart of five column distillations.
Figure elements are numbered：Prefractionation device, 2, topping still, 3, rectifying column, 4, water scrubber, 5, eparating methanol tower, 6, reclaim
Tower, 7, charging condenser, 8, feed exchanger, 9, topping still reboiler, 10, rectifying column reboiler, 11, eparating methanol tower boils again
Device, 12, preposition recycling can, 13, recovery tower reboiler, 14, impurity condenser, 15 water scrubber reboilers, d1、d2Fusel oil export,
E, impurity discharging port, a, take wine mouth, Z, primary steam, Z2Indirect steam.
【Specific embodiment】
Understandable for enabling the above objects, features and advantages of the present invention to become apparent from, below in conjunction with the accompanying drawings to the present invention
Specific embodiment be described in detail.Elaborate a lot of details in order to fully understand this in the following description
Bright.But the present invention can be much to implement different from alternate manner described here, and those skilled in the art can be not
Similar improvement is done, therefore the present invention is not embodied as being limited by following public in the case of running counter to intension of the present invention.
Embodiments of the invention 1-3 is all using the improved five tower differential distillation technology of the present invention：
Five column distillation devices and its connected mode：
As shown in figure 1, five column distillation devices include prefractionation device 1, topping still 2, rectifying column 3, water scrubber 4, eparating methanol tower 5
With recovery tower 6, feed exchanger 8 and charging condenser 7, prefractionation device 1 top and pumped vacuum systems are installed before prefractionation device 1
It is connected, feed exchanger 8 discharging opening is connected with prefractionation device 1 charging aperture, feed exchanger 8 air inlet and prefractionation device 1 top
Gas outlet is connected, and feed exchanger 8 gas outlet is connected with charging condenser 7 charging aperture, prefractionation device 1 discharging opening and topping still 2
Charging aperture is connected, and prefractionation device 1 air inlet is connected with topping still 2 top gas outlet, and charging condenser 7 is provided with two discharging openings and divides
Wei excellent wine outlet not export with light wine, charging condenser 7 excellent wine outlet is connected with water scrubber 4 charging aperture, feeds condenser 7 light wine
Outlet is connected with the preposition recycling can 12 installed before recovery tower 6；
Topping still 2 bottom is provided with topping still reboiler 9, and top is connected with pumped vacuum systems, topping still reboiler 9 and essence
The gas outlet evaporating tower (3) top is connected；
Rectifying column 3 bottom is provided with rectifying column reboiler 10, and total number of plates is 95-100 layer, and middle part is provided with fusel oil export
d1, top is provided with and is respectively equipped with the excellent wine of rectifying column 3, the outlet of rectifying column 3 light wine, rectifying column reboiler 10 and rectifying column 3 top
Gas outlet is connected, and is provided with primary steam Z air inlet, and the outlet of rectifying column 3 excellent wine is located above the outlet of rectifying column 3 light wine, rectification
The outlet of tower 3 excellent wine is connected with eparating methanol tower 5, and the outlet of rectifying column 3 light wine is connected with the preposition recycling can 12 installed before recovery tower 6；
Water scrubber 4 top is provided with impurity discharging port and light wine outlet, and bottom is provided with water scrubber reboiler 15, water scrubber 4 impurities removal
Mouth is located above light wine outlet, is provided with impurity condenser 14, the outlet of water scrubber 4 light wine and recovery tower 6 after water scrubber 4 impurity discharging port
The preposition recycling can 12 of front installation is connected, and water scrubber reboiler 15 is connected with rectifying column 3 top gas outlet, water scrubber 4 discharging opening
It is connected with rectifying column 3 charging aperture；
Eparating methanol tower 5 bottom is provided with eparating methanol tower reboiler 11, and bottom is provided with and takes wine mouth a, and middle part is provided with light wine outlet,
Top is provided with impurity discharging port e, and top is connected with pumped vacuum systems, and the impurity discharging port e of eparating methanol tower 5 goes out positioned at the light wine of eparating methanol tower 5
Above mouthful, light wine outlet takes above wine mouth a positioned at eparating methanol tower 5, installs before the light wine outlet of eparating methanol tower 5 and recovery tower 6
Preposition recycling can 12 is connected, and eparating methanol tower reboiler 11 is connected with water scrubber 4 and eparating methanol tower 5 top gas outlet respectively；
Preposition recycling can 12 is installed before recovery tower 6 charging aperture, middle part is provided with fusel oil export d2, bottom is provided with back
Receive tower reboiler 13, recovery tower reboiler 13 is connected with recovery tower 6 top gas outlet.
The work process of five column distillation devices：
As shown in figure 1, five column distillation work process are：Fermenting-ripening wine with dregs is preheated through feed exchanger 8, after preheating
Enter prefractionation device 1 and carry out vacuum distillation, the fume that prefractionation device 1 still-process produces is back to feed exchanger 8 and maturation
Wine with dregs carries out heat exchange maturation wine with dregs, and then fume carries out condensation and obtains liquid alcohol through charging condenser 7, and wine degree is less than 50%
(v/v) it is referred to as light wine, wine degree is that 50%-60% (v/v) is referred to as excellent wine, and condensed light wine flows into the preposition recovery of recovery tower 6
Tank 12, excellent wine enters water scrubber 4；The part that can not evaporate in prefractionation device 1 is referred to as distiller grains, and distiller grains further flow into topping still 2
Carry out vacuum distillation；While the fume that topping still 2 produces enters prefractionation device 1 as heating gas, it is incorporated to prefractionation generation
Fume carries out heat exchange with ripe wine with dregs in feed exchanger 8, and the distiller grains that topping still 2 produces enter discharge of wastewater system through bottom discharge
System, the thermal source of topping still 2 derives from topping still reboiler 9, and the steam of topping still reboiler 9 is derived from the secondary of rectifying column 3 tower top
Steam；The excellent wine of the generation of charging condenser 7 enters water scrubber 4 and is washed, and impurity is cold through impurity condenser 14 from tower top
Solidifying discharge, water scrubber 4 produces, in still-process, the excellent wine entrance rectifying column 3 that wine degree is 60%-70% (v/v) and carries out rectification, water
Wash the light wine preposition recycling can 12 of entrance that tower 4 generation wine degree is less than 60% (v/v) to be reclaimed, the thermal source of water scrubber 4 derives from
Reboiler 15, the steam of water scrubber reboiler 15 is derived from the indirect steam of rectifying column 3 tower top；From water scrubber 4 excellent wine in essence
Evaporate tower 3 to be distilled, still-process produces the 72-80 layer column plate in rectifying column 3 for the excellent wine that wine degree is 95%-96% (v/v)
Collect, produce the 62-70 layer column plate collection in rectifying column 3 for the light wine that wine degree is less than 95% (v/v), enter preposition recycling can 12
Reclaimed, Alcohols,fusel passes through fusel oil export d1Collect, the thermal source of rectifying column 3 heats from rectifying column reboiler 10, essence
The steam part evaporating tower 10 is come from primary steam, and a part is from the indirect steam of rectifying column 3 tower top；Rectifying column 3 is collected
Excellent wine enter eparating methanol tower 5 and carry out vacuum distillation separating methanol, wherein, methanol passes through impurity removal port e to be collected and removes, and finished wine is proficient in
Cross and take wine mouth a to collect, the thermal source of eparating methanol tower 5 derives from eparating methanol tower reboiler 11, and the steam of eparating methanol tower reboiler 11 comes
Come from water scrubber 4 tower top and the indirect steam of eparating methanol tower 5；The light wine that above-mentioned preposition recycling can 12 reclaims enters through recovery tower 6
Row distillation concentration, the ethanol after distillation concentration sequentially enter water scrubber 4, rectifying column 3 and eparating methanol tower 5 carry out washing, rectification,
Separating methanol, obtains finished product ethanol.
Embodiment 1：
Carry out spice by extracting the Distillers' grains centrifugation clear liquid that the Semen Maydiss slurry after partial starch is with topping still discharge, obtain
The slurry being 15% to corn starch concentration；The thermostable α-amylase of 10u/g is added to be precooked in slurry, temperature of precooking
For 50 DEG C, the time of precooking is 20min, is heated to 95 DEG C and maintains 90min to obtain liquefied fermented glutinous rice through after-ripening device after the completion of precooking；To liquefy
Wine with dregs pumps into brew kettle to carry out saccharifying and obtains converted mash, and saccharifying saccharifying enzyme addition is 50 DEG C for 200u/g saccharification temperature, sugar
The change time is 20min, carries out continuous fermentation using 5 fermentation tanks and obtains ripe wine with dregs, fermentation process is：Sugar to the first fermentation tank
Change in wine with dregs and add the active dry yeast after activation according to mass concentration for 40mg/g, after fermentation 12h, be partitioned into from the first fermentation tank
Then first, second fermentation tank is filled it up with material by about 1/3 mash to the second fermentation tank again；Second fermentation tank normal fermentation 12-
Separate about 1/3 mash after 16h again to the 3rd fermentation tank, then fill it up with material, fermentation, thus along passing, the activation method of yeast is：Will
Active dry yeast is according to dry yeast：Technique water weight ratio is 1:15 ratio is thrown in and is activated in activated yeast tank, rehydration temperature
Spend for 30 DEG C, soak time is 20min, pumps into, after the completion of activation, the tank that spreads cultivation, and add liquefied fermented glutinous rice, activated yeast in the tank that spreads cultivation
With the weight of liquefied fermented glutinous rice than for 1:10, incubation time is 6h, delivers to fermentation tank, and 7d changes and plants once, when the wine of the ripe wine with dregs of fermentation
Part concentration is when 12% (v/v) to be distilled ripe wine with dregs from above-mentioned five column distillation devices, obtains finished product ethanol.
Recycle after distiller grains：The Distillers' grains that still-process topping still is discharged are centrifuged, by 50% after separating
The slurry of liquid and crush maize please carry out spice, 50% clear liquid is carried out vacuum evaporation, after concentration by concentrated solution with
The distiller grains dregs of rice carry out combination drying, pelletize obtains graininess high protein feed.
Embodiment 2：
Carry out spice by extracting the Distillers' grains centrifugation clear liquid that the Semen Maydiss slurry after partial starch is with topping still discharge, obtain
The slurry being 20% to corn starch concentration；The thermostable α-amylase of 15u/g is added to be precooked in slurry, temperature of precooking
For 60 DEG C, the time of precooking is 30min, is heated to 105 DEG C and maintains 120min to obtain liquefied fermented glutinous rice through after-ripening device after the completion of precooking；By liquid
Change wine with dregs and pump into brew kettle and carry out saccharifying and obtain converted mash, saccharifying saccharifying enzyme addition is that 250u/g saccharification temperature is 65 DEG C,
Saccharificatinn period is 30min, carries out continuous fermentation using 10 fermentation tanks and obtains ripe wine with dregs, fermentation process is：To the first fermentation tank
Converted mash according to mass concentration be 60mg/g add activation after active dry yeast, fermentation 16h after, divide from the first fermentation tank
Cut out about 1/3 mash to the second fermentation tank, then first, second fermentation tank is filled it up with material again；Second fermentation tank normal fermentation
Separate about 1/3 mash after 16h again to the 3rd fermentation tank, then fill it up with material, fermentation, thus along passing, the activation method of yeast is：Will
Active dry yeast is according to dry yeast：Technique water weight ratio is 1:25 ratio is thrown in and is activated in activated yeast tank, rehydration temperature
Spend for 35 DEG C, soak time is 30min, pumps into, after the completion of activation, the tank that spreads cultivation, and add liquefied fermented glutinous rice, activated yeast in the tank that spreads cultivation
With the weight of liquefied fermented glutinous rice than for 1:20, incubation time is 8h, delivers to fermentation tank, and 10d changes and plants once, when the wine of the ripe wine with dregs of fermentation
Part concentration is when 15% (v/v) to be distilled ripe wine with dregs from above-mentioned five column distillation devices, obtains finished product ethanol.
Recycle after distiller grains：The Distillers' grains that still-process topping still is discharged are centrifuged, by 60% after separating
The slurry of liquid and crush maize please carry out spice, 40% clear liquid is carried out vacuum evaporation, after concentration by concentrated solution with
The distiller grains dregs of rice carry out combination drying, pelletize obtains graininess high protein feed.
Embodiment 3：
Carry out spice by extracting the Distillers' grains centrifugation clear liquid that the Semen Maydiss slurry after partial starch is with topping still discharge, obtain
The slurry being 17% to corn starch concentration；The thermostable α-amylase of 13u/g is added to be precooked in slurry, temperature of precooking
For 55 DEG C, the time of precooking is 25min, is heated to 100 DEG C and maintains 110min to obtain liquefied fermented glutinous rice through after-ripening device after the completion of precooking；By liquid
Change wine with dregs and pump into brew kettle and carry out saccharifying and obtain converted mash, saccharifying saccharifying enzyme addition is that 220u/g saccharification temperature is 60 DEG C,
Saccharificatinn period is 25min, carries out continuous fermentation using 8 fermentation tanks and obtains ripe wine with dregs, fermentation process is：To the first fermentation tank
Add the active dry yeast after activation according to mass concentration for 50mg/g in converted mash, after fermentation 14h, split from the first fermentation tank
Go out about 1/3 mash to the second fermentation tank, then first, second fermentation tank is filled it up with material again；Second fermentation tank normal fermentation 14h
Separate about 1/3 mash afterwards again to the 3rd fermentation tank, then fill it up with material, fermentation, thus along passing, the activation method of yeast is：To live
Property dry yeast is according to dry yeast：Technique water weight ratio is 1:20 ratio is thrown in and is activated in activated yeast tank, rehydration temperature
For 32 DEG C, soak time be 25min, pump into, after the completion of activation, the tank that spreads cultivation, and in the tank that spreads cultivation add liquefied fermented glutinous rice, activated yeast with
The weight of liquefied fermented glutinous rice is than for 1:15, incubation time is 7h, delivers to fermentation tank, and 8d changes and plants once, when wine part of the ripe wine with dregs of fermentation
Concentration is when 13% (v/v) to be distilled ripe wine with dregs from above-mentioned five column distillation devices, obtains finished product ethanol.
Recycle after distiller grains：The Distillers' grains that still-process topping still is discharged are centrifuged, by 55% after separating
The slurry of liquid and crush maize please carry out spice, 45% clear liquid is carried out vacuum evaporation, after concentration by concentrated solution with
The distiller grains dregs of rice carry out combination drying, pelletize obtains graininess high protein feed.
Matched group：
Carry out Alcohol Production with five conventional column distillation methods, that is, production process saccharifying, fermentation plus sulphuric acid are antibacterial, from not
Five column distillation equipment before improvement, rectifying column does not carry out increasing improvement.
1st, embodiment interpretation of result：
Method according to embodiment 1-3 is produced molasses-spirit and is contrasted with matched group, according to GB10343-2008《Edible
Ethanol》Standard measure, and calculate a ton wine steam consumption and draw and the results are shown in Table 1 as follows:
Ton wine steam consumption (t/t)：Calculate and produce 1t ethanol needs how much steam, that is,：
Ton wine steam consumption (t/t)=steam total flow/alcohol output
Table 1 interpretation table
From the interpretation of result of upper table, the corn alcohol production method steam consumption announced from the present invention is than matched group
Steam consumption will low it was demonstrated that the ethanol being produced using the equipment of the present invention is more energy efficient, the ethanol being produced with the production method of the present invention
Oxidization time is longer than matched group, and methanol content is less than matched group, and the ethanol that explanation is produced with the present invention produces than conventional method
Ethanol more excellent.
2nd, value of the product analysis：
Embodiment 1-3 is compared with matched group, etc. quality Semen Maydiss through embodiment 1-3 the starch that carries, produce ethanol,
After production albumen feedstuff, production edible oil processing, the product price of the production of average 1t Semen Maydiss is only given birth to Semen Maydiss than matched group
The product price producing ethanol will exceed 1000-1500 unit, and economic benefit is and its significantly.
In sum, prolongation corn processed can be reached using the process that the production method of the present invention produces corn alcohol to produce
The industrial chain of ethanol, improves added value of product, energy-saving, the purpose that reduces cost is increased economic efficiency
Embodiment described above only have expressed the several embodiments of the present invention, and its description is more concrete and detailed, but simultaneously
Therefore limitation of the scope of the invention can not be interpreted as.It should be pointed out that for the person of ordinary skill of the art,
Without departing from the inventive concept of the premise, some deformation can also be made and improve, these broadly fall into the protection model of the present invention
Enclose.Therefore, protection scope of the present invention should be defined by claims.
Claims (8)
1. a kind of utilization distiller's grains liquor add Maize Production ethanol processing method it is characterised in that methods described procedure of processing such as
Under：
(1) pretreatment：The Distillers' grains centrifugation clear liquid that the Semen Maydiss slurry extracted after partial starch is discharged with topping still is carried out
Spice, obtains the pretreatment slurry that corn starch concentration is 15%-20%；
(2) steaming and decocting：The thermostable α-amylase of 10u/g-15u/g is added to be precooked in the slurry of step (1), temperature of precooking
For 50 DEG C -60 DEG C, the time of precooking is 20min-30min, is heated to 95-105 DEG C and maintains 90min- through after-ripening device after the completion of precooking
120min obtains liquefied fermented glutinous rice；
(3) saccharifying：Liquefied fermented glutinous rice entrance brew kettle carries out saccharifying and obtains converted mash, and saccharifying saccharifying enzyme addition is 200u/g-
250u/g saccharification temperature is 50 DEG C -65 DEG C, and saccharificatinn period is 20min-30min；
(4) ferment：Fermentation is carried out using continuous fermentation method and obtains ripe wine with dregs, wine part concentration of ripe wine with dregs is 12%-15% (v/v)
Shi Jinhang distills；
(5) distill：Ripe wine with dregs is distilled, distillation mode selects five column distillations, obtains ethanol after distillation；
(6) recycle after distiller grains：The Distillers' grains that still-process topping still is discharged are centrifuged, by 50%- after separating
60% clear liquid return to step (1) carries out spice, and the clear liquid of 40%-50% is carried out vacuum evaporation, will concentrate after concentration
Albumen feedstuff, with the distiller grains dregs of rice carry out combination drying, pelletize obtains graininess high protein feed, also can be extracted by liquid further,
Carry out refine and produce edible corn oil.
2. a kind of utilization distiller's grains liquor according to claim 1 add Maize Production ethanol processing method it is characterised in that
The fermentation tank of described step (4) continuous fermentation has 5-10, and continuous ferment process is, in the converted mash of the first fermentation tank according to
Mass concentration adds the active dry yeast after activation for 40mg/g-60mg/g, after fermentation 12-16h, is partitioned into from the first fermentation tank
Then first, second fermentation tank is filled it up with material by about 1/3 mash to the second fermentation tank again；Second fermentation tank normal fermentation 12-
Separate about 1/3 mash after 16h again to the 3rd fermentation tank, then fill it up with material, fermentation, thus along passing down.
3. a kind of utilization distiller's grains liquor according to claim 2 add Maize Production ethanol processing method it is characterised in that
Described activated yeast method is：By active dry yeast according to dry yeast：Technique water weight ratio is 1:The ratio of 15-25 is thrown in ferment
Female activation pot is activated, and rehydration temperature is 30 DEG C -35 DEG C, and soak time is 20min-30min, pumps into and spread cultivation after the completion of activation
Tank, and add liquefied fermented glutinous rice in the tank that spreads cultivation, the weight of activated yeast and liquefied fermented glutinous rice ratio is for 1:10-20, incubation time is 6h-8h,
Deliver to fermentation tank, 7-10d changes and plants once.
4. a kind of utilization distiller's grains liquor according to claim 1 add Maize Production ethanol processing method it is characterised in that
Described step (6) five column distillation includes prefractionation device (1), topping still (2), rectifying column (3), water scrubber (4), eparating methanol tower (5)
With recovery tower (6), feed exchanger (8) and charging condenser (7) are installed before described prefractionation device (1), prefractionation device (1) pushes up
Portion is connected with pumped vacuum systems, and described feed exchanger (8) discharging opening is connected with prefractionation device (1) charging aperture, feed exchanger
(8) air inlet is connected with prefractionation device (1) top gas outlet, feed exchanger (8) gas outlet with charging condenser (7) charging aperture
It is connected, described prefractionation device (1) discharging opening is connected with topping still (2) charging aperture, prefractionation device (1) air inlet and topping still (2)
Top gas outlet is connected, and described charging condenser (7) is provided with two discharging openings and is respectively excellent wine outlet and light wine outlet, and charging is cold
The outlet of condenser (7) excellent wine is connected with water scrubber (4) charging aperture, installs before charging condenser (7) light wine outlet and recovery tower (6)
Preposition recycling can (12) is connected；
Described topping still (2) bottom is provided with topping still reboiler (9), and top is connected with pumped vacuum systems, and described topping still is again
Boiling device (9) is connected with the gas outlet at rectifying column (3) top；
Described rectifying column (3) bottom is provided with rectifying column reboiler (10), and total number of plates is 95-100 layer, and middle part is provided with Alcohols,fusel
Outlet (d1), top is provided with and is respectively equipped with the excellent wine of rectifying column (3), the outlet of rectifying column (3) light wine, described rectifying column reboiler (10)
It is connected with the gas outlet at rectifying column (3) top, and is provided with primary steam Z air inlet, the excellent wine outlet of described rectifying column (3) is located at essence
Evaporate above the outlet of tower (3) light wine, the excellent wine outlet of described rectifying column (3) is connected with eparating methanol tower (5), described rectifying column (3) light wine
Outlet is connected with the preposition recycling can (12) installed before recovery tower (6)；
Described water scrubber (4) top is provided with impurity discharging port and light wine outlet, and bottom is provided with water scrubber reboiler (15), described washing
Tower (4) impurity discharging port is located above light wine outlet, is provided with impurity condenser (14), water scrubber (4) is light after water scrubber (4) impurity discharging port
Wine outlet is connected with the preposition recycling can (12) installed before recovery tower (6), and described water scrubber reboiler (15) is pushed up with rectifying column (3)
Portion gas outlet is connected, and described water scrubber (4) discharging opening is connected with rectifying column (3) charging aperture；
Described eparating methanol tower (5) bottom is provided with eparating methanol tower reboiler (11), and bottom is provided with and takes wine mouth (a), and middle part is provided with light
Wine exports, and top is provided with impurity discharging port (e), and top is connected with pumped vacuum systems, and the impurity discharging port (e) of described eparating methanol tower (5) is located at
Above the light wine outlet of eparating methanol tower (5), light wine outlet takes above wine mouth (a) positioned at eparating methanol tower (5), described eparating methanol tower
(5) light wine outlet is connected with the preposition recycling can (12) installed before recovery tower (6), and described eparating methanol tower reboiler (11) is respectively
It is connected with water scrubber (4) and eparating methanol tower (5) top gas outlet；
Before described recovery tower (6) charging aperture, preposition recycling can (12) is installed, middle part is provided with fusel oil export (d2), bottom is pacified
Equipped with recovery tower reboiler (13), described recovery tower reboiler (13) is connected with recovery tower (6) top gas outlet.
5. a kind of utilization distiller's grains liquor according to claim 4 add Maize Production ethanol processing method it is characterised in that
Described rectifying column (3) and recovery tower (6) bottom are provided with slag-drip opening, are connected with waste water drainage system, and waste water drainage system produces
Indirect steam reclaimed through vapor-recovery system, indirect steam be passed through recovery tower reboiler (13) recovery tower is carried out plus
Heat.
6. a kind of utilization distiller's grains liquor according to claim 4 add Maize Production ethanol processing method it is characterised in that
Described prefractionation device (1), topping still (2) operating pressure are negative pressure, and rectifying column (3) operating pressure is malleation, described water scrubber (4)
Operating pressure is normal pressure, and eparating methanol tower (5) operating pressure is negative pressure, and recovery tower (6) operating pressure is normal pressure.
7. a kind of utilization distiller's grains liquor according to claim 6 add Maize Production ethanol processing method it is characterised in that
The bottom gauge pressure of described prefractionation device (1) is -40kPa～-30kPa, and top gauge pressure is -60kPa～-70kPa；Topping still tower reactor
Gauge pressure is -40kPa～-30kPa, and tower top gauge pressure is 0kPa～5kPa；Rectifying column (3) tower reactor gauge pressure is 90～200kPa, tower top
Gauge pressure is 70kPa～180kPa；Water scrubber (4) tower reactor gauge pressure is 25～60kPa, and tower top gauge pressure is 0kPa～20kPa；Separating methanol
Tower (5) tower reactor gauge pressure is -5kPa～10kPa, and tower top gauge pressure is -25kPa～-40kPa；Recovery tower (6) tower reactor gauge pressure is 25kPa
～30kPa, tower top gauge pressure is 0kPa～5kPa.
8. a kind of utilization distiller's grains liquor according to claim 4 add Maize Production ethanol processing method it is characterised in that
Described five column distillation work process are：Fermenting-ripening wine with dregs is preheated through feed exchanger (8), enters prefractionation device after preheating
(1) carry out vacuum distillation, the fume that prefractionation device (1) still-process produces is back to feed exchanger (8) to be carried out with ripe wine with dregs
Heat exchange maturation wine with dregs, then fume carry out condensation and obtain liquid alcohol through charging condenser (7), wine degree is less than 50% (v/
V) it is referred to as light wine, wine degree is that 50%-60% (v/v) is referred to as excellent wine, and condensed light wine flows into the preposition recycling can of recovery tower (6)
(12), excellent wine enters water scrubber (4)；The part that can not evaporate in prefractionation device (1) is referred to as distiller grains, and distiller grains further flow into and slightly evaporate
Tower (2) carries out vacuum distillation；While the fume that topping still (2) produces enters prefractionation device (1) as heating gas, it is incorporated to pre- point
Evaporate the fume of generation and ripe wine with dregs carries out heat exchange in feed exchanger (8), the distiller grains that topping still (2) produces enter through bottom discharge
Enter waste water drainage system, the thermal source of topping still (2) derives from topping still reboiler (9), and the steam of topping still reboiler (9) is derived from
The indirect steam of rectifying column (3) tower top；The excellent wine of the generation of charging condenser (7) enters water scrubber (4) and is washed, impurity from
Tower top condenses through impurity condenser (14) and discharges, and it is 60%-70%'s (v/v) that water scrubber (4) produces wine degree in still-process
Excellent wine enters rectifying column (3) and carries out rectification, and water scrubber (4) produces the light wine preposition recycling can of entrance that wine degree is less than 60% (v/v)
(12) reclaimed, the thermal source of water scrubber (4) derives from reboiler (15), and the steam of water scrubber reboiler (15) is derived from rectifying column
(3) indirect steam of tower top；Excellent wine from water scrubber (4) is distilled in rectifying column (3), and still-process produces wine degree and is
The excellent wine of 95%-96% (v/v) is collected in the 72-80 layer column plate of rectifying column (3), produces wine degree and is less than the light of 95% (v/v)
Wine is collected in the 62-70 layer column plate of rectifying column (3), enters preposition recycling can (12) and is reclaimed, Alcohols,fusel passes through Alcohols,fusel
Outlet (d1) collect, the thermal source of rectifying column (3) derives from rectifying column reboiler (10) and heats, a steam part for rectifying column (10)
Come from primary steam, a part is from the indirect steam of rectifying column (3) tower top；The excellent wine that rectifying column (3) is collected enters piptonychia
Alcohol tower (5) carries out vacuum distillation separating methanol, and wherein, methanol passes through impurity removal port (e) to be collected and remove, and finished wine was proficient in and is taken wine mouth
A () collects, the thermal source of eparating methanol tower (5) derives from eparating methanol tower reboiler (11), and the steam of eparating methanol tower reboiler (11) comes
Come from water scrubber (4) tower top and the indirect steam of eparating methanol tower (5)；The light wine that above-mentioned preposition recycling can (12) is reclaimed is through reclaiming
Tower (6) carries out distilling concentration, and the ethanol after distillation concentration sequentially enters water scrubber (4), rectifying column (3) and eparating methanol tower (5) and enters
Row washing, rectification, separating methanol, obtain finished product ethanol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610858697.5A CN106399388B (en) | 2016-09-27 | 2016-09-27 | method for producing alcohol by using clear liquid of distiller's grains and corn |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610858697.5A CN106399388B (en) | 2016-09-27 | 2016-09-27 | method for producing alcohol by using clear liquid of distiller's grains and corn |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106399388A true CN106399388A (en) | 2017-02-15 |
| CN106399388B CN106399388B (en) | 2020-01-31 |
Family
ID=58015657
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610858697.5A Active CN106399388B (en) | 2016-09-27 | 2016-09-27 | method for producing alcohol by using clear liquid of distiller's grains and corn |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106399388B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107058403A (en) * | 2017-06-22 | 2017-08-18 | 广西中粮生物质能源有限公司 | A kind of distiller's grains liquor is used for the method that full amylofermentation prepares ethanol |
| CN108065026A (en) * | 2017-12-11 | 2018-05-25 | 广西中粮生物质能源有限公司 | A kind of preparation method of cereal feedstuff |
| CN110373305A (en) * | 2018-04-11 | 2019-10-25 | 北京百漾酒业科技股份有限公司 | The continuous distillation plant and method of white wine |
| CN113265310A (en) * | 2021-06-23 | 2021-08-17 | 安徽五河春生物科技有限公司 | Processing and production process of salvia miltiorrhiza wine |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736527A (en) * | 2005-06-30 | 2006-02-22 | 广东中科天元再生资源工程有限公司 | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof |
| CN104250581A (en) * | 2013-06-27 | 2014-12-31 | 安琪酵母股份有限公司 | Method for co-producing corn crude oil and DDG protein feed by using corn fermentation |
-
2016
- 2016-09-27 CN CN201610858697.5A patent/CN106399388B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736527A (en) * | 2005-06-30 | 2006-02-22 | 广东中科天元再生资源工程有限公司 | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof |
| CN104250581A (en) * | 2013-06-27 | 2014-12-31 | 安琪酵母股份有限公司 | Method for co-producing corn crude oil and DDG protein feed by using corn fermentation |
Non-Patent Citations (1)
| Title |
|---|
| 黄亚东 主编: "《酒精生产技术》", 28 February 2014, 中国轻工业出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107058403A (en) * | 2017-06-22 | 2017-08-18 | 广西中粮生物质能源有限公司 | A kind of distiller's grains liquor is used for the method that full amylofermentation prepares ethanol |
| CN108065026A (en) * | 2017-12-11 | 2018-05-25 | 广西中粮生物质能源有限公司 | A kind of preparation method of cereal feedstuff |
| CN110373305A (en) * | 2018-04-11 | 2019-10-25 | 北京百漾酒业科技股份有限公司 | The continuous distillation plant and method of white wine |
| CN113265310A (en) * | 2021-06-23 | 2021-08-17 | 安徽五河春生物科技有限公司 | Processing and production process of salvia miltiorrhiza wine |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106399388B (en) | 2020-01-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100525874C (en) | Six-column differential-pressure distillation device for extra edible alcohol and process therefor | |
| CN106399388A (en) | Ethyl alcohol processing method by clear solution of distiller grain and corn | |
| CN100453137C (en) | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof | |
| CN102286544B (en) | A kind of clean preparation method of starch base alcohol fuel | |
| CN204702730U (en) | A kind of Novel steam distillation unit for liquor production by liquid fermentation | |
| CN104130224B (en) | The tower continuous treater of furfural production six and furfural treatment technique thereof | |
| CN101191136A (en) | Clean producing technique for extracting saponin from turmeric and coproducing fuel ethanol | |
| CN204973118U (en) | High thermodynamic efficiency's alcohol distillation production system | |
| CN108531342A (en) | A kind of production method and equipment of the neutral edible product that brews alcohol | |
| CN103614278B (en) | The Apparatus and method for of waste liquid of molasses alcohol | |
| CN108728318A (en) | A kind of super clean superfine edible alcohol differential distillation process units and its production technology | |
| CN105503933B (en) | A kind of chemical industry monomer energy-saving rectifying device and method | |
| CN106434769B (en) | A kind of processing method adding alcohol produced from molasses using manioc waste | |
| CN110698325A (en) | Production device and process for co-producing fuel ethanol and special grade edible alcohol | |
| CN102517340A (en) | Process method for separating and drying lees produced in production process of ethanol with potatoes | |
| CN106636223A (en) | Processing method for utilizing cassava residue and cassava to produce alcohol | |
| CN101717802B (en) | Energy-saving production method of bio-ethanol | |
| CN214344493U (en) | Device for rectifying white spirit by liquid method | |
| CN106316792B (en) | The device and method of methanol and ethyl alcohol is recycled from stalk sugar hydrocrackates | |
| CN105733905A (en) | Method for preparing alcohol through slagless distillation | |
| CN209714332U (en) | A kind of acetonitrile rectifying column | |
| CN104232454B (en) | The method producing whiskey with waste yeast in beer production | |
| CN113667700A (en) | Method and system for producing ethanol by fermenting mixed raw materials | |
| CN113620804A (en) | Continuous esterification process and device for ethyl 2-methylbutyrate | |
| CN213232066U (en) | System for utilize fermented glutinous rice to prepare extra grade alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20200103 Address after: 317000 No. 5-100, Fengchuan Village, Shaojiadu Street, Linhai City, Taizhou City, Zhejiang Province Applicant after: Taizhou Zhongzhi Yingjian Machinery Automation Co., Ltd. Address before: The village of Tianhe town Hechi city the Guangxi Zhuang Autonomous Region Luocheng County 546400 Applicant before: GUANGXI LUOCHENG KECHAO FOUNDATION SCIENCE AND TECHNOLOGY DEVELOPMENT CO., LTD. |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |