CN108823262A - A kind of novel process for cassava production alcohol - Google Patents
A kind of novel process for cassava production alcohol Download PDFInfo
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- CN108823262A CN108823262A CN201810751858.XA CN201810751858A CN108823262A CN 108823262 A CN108823262 A CN 108823262A CN 201810751858 A CN201810751858 A CN 201810751858A CN 108823262 A CN108823262 A CN 108823262A
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- 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
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- 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
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- 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
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/02—Stirrer or mobile mixing elements
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses a kind of novel process for cassava production alcohol, using two mash heat exchangers, add α-amylase, the liquefaction of two steps twice in the liquefied pot of front and back respectively, the heat exchange of two step mash, material repeatedly heat up and cool down in preceding liquefied pot, after-ripening device, rear liquefied pot and saccharifying tank equal segments；This saccharification system is not in the case where utilizing other processes thermal energy, thinning process steam in Alcohol Production（8Kg/cm2Saturated vapor）Consumption is within 200Kg；Can meet the needs of alcohol thick mash fermentation, solve the transportation problem of high concentration mash under the premise of taking into account energy consumption, mash concentration is up to 25Bx。More than, end of a period alcohol content of fermenting is up to 14%（V/V）More than.
Description
Technical field
The invention belongs to heat exchange equipment technologies, in particular to the saccharification system for cassava production alcohol.
Background technique
With in the technique of starchy material production edible alcohol, thinning workshop section is very crucial process, direct shadow
Ring the energy consumption and starch utilization ratio to production.There are two types of prior arts：One is the coolings of liquefied fermented glutinous rice vacuum cooled, and one is spirals
The cooling of one step of sheet heat exchanger.The shortcomings that vacuum cooled falling temperature method is：Temperature of charge control can not be adjusted well in technique institute
The range needed, that is, temperature of charge control are unstable；The shortcomings that spiral-plate heat exchanger falling temperature method is：In High Concentration Situation
Under, mash viscosity is big, difficulty of transportation, while heat exchanger is easy blocking, and cooling effect is poor, and thermal loss is big.
Chinese patent Shen application number：201610858721.5 the applying date：2016-09-27 discloses a kind of using manioc waste
Add the processing method of cassava production alcohol, which is characterized in that the processing method includes the following steps：(1) it pre-processes：Fresh cassava
It desilts, remove the peel by cleaning machine cleaning；(2) it crushes：Water is added in step (1) pretreated fresh cassava and carries out wet pulverizing
Slurry is obtained, the content of starch of slurry is 20%-25%；(3) manioc waste is added：It is added to extract into the slurry of step (2) and form sediment
Manioc waste after powder obtains slag charge slurry, and manioc waste content of starch is 7%-9%, slurry：The weight ratio of manioc waste is 2-4:1；
(4) boiling：The thermostable α-amylase that 10u/g-15u/g is added into the slag charge slurry of step (3) is precooked, temperature of precooking
It is 50 DEG C -60 DEG C, the time of precooking is 20min-30min, and 95-105 DEG C is heated to after the completion of precooking and maintains 90min- through after-ripening device
120min obtains liquefied fermented glutinous rice；(5) it is saccharified：Liquefied fermented glutinous rice enters brew kettle and is saccharified to obtain converted mash, and saccharifying carbohydrase adds
Dosage is 200u/g-250u/g, and saccharification temperature is 50 DEG C -65 DEG C, saccharificatinn period 20min-30min；(6) it ferments：Using even
Continuous fermentation method is fermented to obtain mature wine with dregs, and wine part concentration of mature wine with dregs is more than or equal to 12% (v/v)；(7) it distills：By mature wine with dregs
It is distilled, distillation mode selects five column distillation systems, obtains alcohol after distillation.The energy of its saccharification step is without sufficiently benefit
With.
Chinese patent application Publication No. 105841525A, a kind of entitled broad passage plate heat exchanger, Yi Zhongkuan
Channel plate heat exchanger, including support, shell, heat exchange core body, heat exchange medium import and export and heat exchange mash import and export, institute
It states heat exchange medium import and export and heat exchange mash import and export is located on the shell and is connected to heat exchange core body, the heat exchange
Core includes heat exchange medium circulation passage and heat exchange medium circulation passage, and multiple nest shapes are arranged in heat exchange medium circulation passage
Turbulence chamber, the shell are fabricated structure.In order to avoid have heat exchange mash pressure it is larger when heat exchange plate generate flexible deformation
Caused by heat exchange medium stop, present embodiment is arranged in pairs arc in each neck of heat exchange medium circulation passage
Supporting element, neither influences the expansion of heat exchange medium circulation passage, while guaranteeing the minimum in heat exchange medium circulation passage section
Size, and then guarantee the proper flow of heat exchange medium.
How to combine solution heat exchange medium mash slow in circulation road flow velocity, cooling effect is poor, and thermal loss is big, is production
Technical problem to be solved in the technique of edible alcohol.
Summary of the invention
The present invention is that technical problem to be solved by the invention is to provide a kind of cassavas that lifting temp effect is good, energy saving
Produce the novel process of alcohol.
The technical proposal of the invention is realized in this way：
A kind of novel process for cassava production alcohol, including saccharification step, saccharification step include the following steps：
1. water is added through screw feeder after crushed in raw material cassava, into desanding before tank, cassava slurry is obtained after mixing evenly, through desanding
Pump squeezes into the silt being mingled in desander removal raw material, into mixing tank；
2. thermostable α-amylase is added by 6 units/gram raw materials in mixing tank, beats through spice pump to 2# mash and change after stirring evenly
Hot device exchanges heat with the liquefied fermented glutinous rice of liquefied pot after 2#, and temperature rises to 55 ~ 60 DEG C, and liquefied fermented glutinous rice is cooled to 55 ~ 60 by 75 ~ 80 DEG C simultaneously
DEG C, 55 ~ 60 DEG C of slurries after heat exchange enter liquefied pot before 1#；
3. liquefied pot is warming up to 65 ~ 70 DEG C with steam before 1#, reach the gelatinization point of cassava；
It is changed 4. material liquefied pot before 1# is beaten through 1# mash ring heat pump to 1# mash heat exchanger with the boiling wine with dregs come out from after-ripening device
Heat, temperature rise to 80 ~ 85 DEG C and enter liquefied pot before 2#, while boiling wine with dregs is cooled to 75 ~ 80 DEG C by 90 ~ 95 DEG C, into 1# after liquid
Change tank；
5. the control of liquefied pot temperature is α-amylase the best use temperature at 80 ~ 85 DEG C before 2#, 3#；
6. material enters after-ripening device, after-ripening device temperature control through boiling feed pump after Jet liquefier and the uniform Hybrid Heating of steam
System is at 90 ~ 95 DEG C；
7. material from after-ripening device come out after through 1# mash heat exchanger cooling after enter 1# after liquefied pot, while after 1# liquefied pot press 4
Thermostable α-amylase is added in units/gram raw material；
8. material liquefied pot after 2# liquefies after, pump, which is beaten to 2# mash heat exchanger, is cooled to 55 ~ 60 DEG C, into saccharifying tank, saccharification
Carbohydrase is added in tank.
Preferably, above-mentioned 1# mash heat exchanger and 2# mash heat exchanger are broad passage plate mash heat exchanger.
Preferably, above-mentioned broad passage plate mash heat exchanger, including to include mash heat exchanger shell, heat exchange medium circulation logical
Road, heat exchange medium circulation passage, heat exchange core body, the import of heat exchange mash, the outlet of heat exchange mash and heat exchange medium import, heat exchange
Media outlet, the heat exchange medium import, heat exchange medium exit and heat exchange mash import, the outlet of heat exchange mash are located at mash
It is connected on heat exchanger shell and respectively with the heat exchange medium circulation passage of the heat exchange core body, heat exchange medium circulation passage；Institute
It states to be fixedly connected between each plate of heat exchange medium circulation passage and plate by point type spacing column and is changed to the fixed company of square steel type wire type
It connects.
Preferably, the height of above-mentioned board-like mash heat exchanger channel is 16mm, width 100mm.
Preferably, above-mentioned steps 1. in spice Cassava crushing granularity：∅1.6~1.8mm ；Spice temperature：35~40℃；
Spice water addition ratio：1：2.3 ~ 2. spice concentration：25~26BX°.
Preferably, it liquefies before above-mentioned 1# the tank temperature residence time：30~40min；The liquefied pot residence time before 2#, 3#：60~
90min。
Preferably, above-mentioned Jet liquefier temperature：90~95℃；The after-ripening device residence time：40~60min.
Preferably, the above-mentioned rear liquefied pot residence time：60~90min.
Preferably, above-mentioned saccharifying tank carbohydrase additive amount：150 ~ 200 units/gram raw materials；Saccharifying tank temperature：55~60℃；
The saccharifying tank residence time：40~60min.
This system using α-amylase is added twice, and the liquefaction of two steps, the heat exchange of two step wine with dregs wine with dregs, material segmentation repeatedly heats up and cooling：
1, the temperature of liquefied pot controls before 1# and the residence time is the key point of technique, and temperature control is just liquid at 65 ~ 70 degree
Change enzyme to start to play the temperature of viscosity reduction effect, residence time control made α-amylase have sufficient action time at 30 ~ 40 minutes；
2, broad passage plate heat exchanger is welded entirely using modified instead of spiral-plate heat exchanger, and plate heat exchanger channel is by being highly
16mm, width 100mm are changed to square steel type wire type by the fixation of spacing column point type between plate and plate and fix, solve the big resistance of viscosity
Blockage problem caused by power is big and material impurity is more.
Detailed description of the invention
Fig. 1 and Fig. 2 is the structural schematic diagram for the system that cassava of the present invention produces edible alcohol；
Fig. 3 is the structural schematic diagram of mash heat exchanger of the invention；
Tank before 1- desanding；2- removes sand pump；3- desander；4- mixing tank；5- spice pump；Liquefied pot before 6-1#；The heat exchange of 7-1# mash
Pump；8-1# mash heat exchanger；Liquefied pot before 9-2#；Liquefied pot before 10-3#；11- boiling feed pump；12- sprays liquefier；After 13-
Ripe device；14- boiling wine with dregs pump；Water of 15- is from pipe network；Liquefied pot after 16-1#；161-1# mash heat exchanger exit；After 17-2#
Liquefied pot；Liquefy pump after 18-；19-2# mash heat exchanger；20- concentrated sulfuric acid tank；21-1# saccharifying tank；22- carbohydrase tank；23-2#
Saccharifying tank；24- saccharification discharging pump.
81- mash heat exchanger shell；82- heat exchange medium circulation passage；83- heat exchange mash circulation passage；84- heat exchange core
Body；85- heat exchange medium import；86 heat exchange mash outlets；87- heat exchange mash import；88- square steel linear columns；89- heat exchange is situated between
Matter outlet；84-1- heat exchange plate.
Specific embodiment
Below in conjunction with attached drawing, specific embodiments of the present invention will be described in further detail：
Mash：Fermentation method produces in edible alcohol, the mixture of material and water.
Referring to Fig. 1 and Fig. 2, a kind of saccharification system for cassava production alcohol, including tank 1 before desanding, except sand pump 2, remove
Liquefied pot 6 before sand device 3, mixing tank 4, spice pump 5,1#；1# mash heat exchange pump 7；1# mash heat exchanger 8, boiling feed pump 11,
Spray liquefier 12, after-ripening device 13, boiling wine with dregs pump 14, rear liquefied pot, rear liquefaction pump 18,2# mash heat exchanger 18, concentrated sulfuric acid tank 20,
1# saccharifying tank 21, carbohydrase tank 22,2# saccharifying tank 23；Be saccharified discharging pump 24；
Wherein 1 outlet of tank removes sand pump 2 before desanding；
Except the outlet desander 3 of sand pump 2；The outlet of desander 3 connects mixing tank 4；It is set between desander 3 and mixing tank 4
Have except sand launder；
The outlet connection spice pump 5 of mixing tank 4；
The heat exchange mash circulation passage import of spice pump 5 and 2# mash heat exchanger 19；The heat exchange mash stream of 2# mash heat exchanger 19
Circulation passage outlet and the import of liquefied pot 6 before 1# communicate；The outlet of liquefied pot 6 is connected with the import of 1# mash heat exchange pump 7 before 1#
It is logical；The outlet of 1# mash heat exchange pump 7 is connected with the heat exchange mash import of 1# mash heat exchanger 8；
The outlet of the heat exchange mash of 1# mash heat exchanger 8 is connected with other preceding liquefied pot imports；
Above-mentioned other preceding liquefied pots refer to the preceding liquefied pot other than liquefied pot 6 before 1#, 9 He of liquefied pot before this attached drawing middle finger 2#
Liquefied pot 10 before 3#, liquefied pot 10 is connected before liquefied pot 9 and 3# before 2#.
Other preceding liquefied pot outlets are connected with the import of boiling feed pump 11；The outlet of boiling feed pump 11 and it is multiple after
The import of ripe device 13 is connected；Spray liquefier 12 is equipped between the boiling charging pump discharge and the import of after-ripening device；
Jet chimney is connected with liquefied pot before whole and spray liquefier 12 respectively；
Multiple outlets of after-ripening device 13 are connected through boiling wine with dregs pump 14 with the heat exchange medium import of 1# mash heat exchanger 8；It steams at this time
Boiling wine with dregs is 90 ~ 95 DEG C；
The heat exchange medium exit of 1# mash heat exchanger 8 is connected with the import of liquefied pot 16 after 1#；Wherein liquefied pot 16 after 1#
It connects with liquefied pot 17 after 2#；
The outlet of liquefied pot liquefaction pump 18 after is connected with the heat exchange medium import of 2# mash heat exchanger 19 afterwards；
The heat exchange medium exit of 2# mash heat exchanger 19 is connected with 1# saccharifying tank import；Wherein 1# saccharifying tank 21 and 2# saccharification
Tank 23 connects and is connected with primary steam pipeline；It is respectively equipped with the carbohydrase tank 22 that carbohydrase is added on 1# saccharifying tank 21 and adds
Enter the concentrated sulfuric acid tank 20 of sulfuric acid；
Mash is sent out through saccharification discharging pump 24 in the outlet of 2# saccharifying tank 23 to ferment.
By taking cassava is raw material production edible alcohol as an example：
One, brief description of the process：
1, process water is added through screw feeder after crushed in raw material cassava, into desanding before tank, obtain cassava slurry after mixing evenly, pass through
Except sand pump squeezes into the silt being mingled in desander removal raw material, into mixing tank.
2, thermostable α-amylase is added by 6 units/gram raw materials in mixing tank（Hereinafter referred to as α-amylase）, after mixing evenly
It beats through spice pump to 2# mash heat exchanger, exchanges heat with the liquefied fermented glutinous rice of liquefied pot after 2#, temperature rises to 55 ~ 60 DEG C, and liquefied fermented glutinous rice is simultaneously
55 ~ 60 DEG C are cooled to by 75 ~ 80 DEG C, 55 ~ 60 after heat exchange DEG C slurry enters liquefied pot before 1#.
3, liquefied pot with steam is warming up to 65 ~ 70 DEG C before 1#, reaches the gelatinization point of cassava, α-amylase starts to act as at this time
With phosphoric acid significantly reduces, and conveying is no longer difficult.
4, material liquefied pot before 1# is beaten through 1# mash ring heat pump to 1# mash heat exchanger and the boiling from after-ripening device out
Wine with dregs heat exchange, temperature rises to 80 ~ 85 DEG C and enters liquefied pot before 2#, while boiling wine with dregs is cooled to 75 ~ 80 DEG C by 90 ~ 95 DEG C, into 1#
Liquefied pot afterwards.
5, the control of liquefied pot temperature is α-amylase the best use temperature at 80 ~ 85 DEG C before 2#, 3#.
6, material enters after-ripening device, after-ripening device temperature through boiling feed pump after Jet liquefier and the uniform Hybrid Heating of steam
Degree control is at 90 ~ 95 DEG C.
7, material enters after the cooling of 1# mash heat exchanger liquefied pot after 1#, while liquefied pot after 1# after coming out from after-ripening device
α-amylase is added by 4 units/gram raw materials.
8, material liquefied pot after 2# pump that liquefies after is beaten to 2# mash heat exchanger and is cooled to 55 ~ 60 DEG C, into saccharifying tank,
Carbohydrase is added in saccharifying tank.
Two, every technology controlling and process index：
1, grinding particle size：1.6 ~ 1.8mm spice temperature： 35~40℃
Spice water addition ratio：1：2.3 ~ 2.5 spice concentration：25~26BX°
2, liquefied pot α-amylase additive amount before 1#：6 units/gram raw materials
Liquefied pot temperature before 1#：65~70℃
The liquefied pot residence time before 1#：30~40min
Liquefied pot temperature before 2#, 3#：80~85℃
The liquefied pot residence time before 2#, 3#：60~90min
3, Jet liquefier temperature：90~95℃
The after-ripening device residence time：40~60min
4, liquefied pot α-amylase additive amount after 1#：4 units/gram raw materials
Liquefied pot temperature afterwards：75~80℃
The liquefied pot residence time afterwards：60~90min
5, saccharifying tank carbohydrase additive amount：150 ~ 200 units/gram raw materials,
Saccharifying tank temperature：55~60℃
The saccharifying tank residence time：40~60min.
Mashing process of the invention solves the problems, such as follows：
1, the transportation problem of material under the conditions of thick mash is solved；
2, traditional thinning technique heat exchanger blockage problem is solved；
3, solve the problems, such as that thinning process heat sufficiently recycles；
4, the instability problem of traditional thinning process liquefaction extent control is solved.
This technique is not in the case where utilizing other processes thermal energy, thinning process steam in Alcohol Production（8Kg/cm2It is full
And steam）Consumption is within 200Kg.
This technique can meet the needs of alcohol thick mash fermentation, solve the defeated of high concentration mash under the premise of taking into account energy consumption
Problem is sent, mash concentration is up to 25Bx。More than, end of a period alcohol content of fermenting is up to 14%（V/V）More than.
Referring to Fig. 3, mash heat exchanger includes mash heat exchanger shell 81, heat exchange medium circulation passage 82, heat exchange mash
Circulation passage 83, heat exchange core body 84, heat exchange mash import 85, heat exchange mash outlet 89 and heat exchange mash import 87, heat exchange
Mash outlet 86, heat exchange medium import 85, heat exchange medium exit 89 and heat exchange mash import 13, heat exchange mash export 87
It is connected on mash heat exchanger shell and with heat exchange core body 84.
Mash heat exchanger shell 81 is fabricated structure, is bolted and is formed by 4 side plates in front and back up and down, both ends are set
End cap is set, the mash heat exchanger shell 81 that can be dismantled entirely is thus constituted, installs and repair and is very convenient.
Heat exchange medium import 85, heat exchange medium exit 89 and heat exchange mash import 87,86 difference of heat exchange mash outlet
Positioned at the two-end part of front and rear sides plate.
Relative to cassava mash heat exchanger of the invention, the number of plies and width of heat exchange plate 84-1 compares other common
Mash heat exchanger is much bigger, when being the prior art between heat exchange plate 84-1, heat exchange plate 84- when heat exchange mash pressure is larger
1 generates heat exchange medium cutout, plate and plate caused by flexible deformation（Piece）Between be fixedly connected for point type spacing column, work as cassava
Mash passes through, and since the concentration of cassava mash is big, and contains a large amount of fibers, is easy in direct use in spacing column（It is equivalent to back
The supporting element 25 of scape technology）Form obstruction.
Present embodiment is changed between each plate and plate of heat exchange medium circulation passage 82 by the fixation of point type spacing column
Square steel linear columns are fixedly connected, i.e., heat exchange core body 84 is used by several heat exchange plate 84-1 and two sides partition along mash forward direction
Steel formula wire type is constituted.
It was originally in that the heat exchange medium circulation passage 82 of a piece of laminar flow has been changed to one by one by improvement above
Individual channel.
Originally since spacing column is in point type, the impurity of cassava mash will hang on spacing column, will soon occur in channel
Blocking, clearance time frequency is high, seriously affects production efficiency.
And after the point type for changing spacing column is square steel linear columns, cassava mash has passed through channel just without hanging point.
In order to further overcome mash heat exchanger to be easy blocking, plate heat exchanger channel height is changed to 16mm by 12mm,
Width 60mm is changed to 100mm.
It does not influence the expansion of heat exchange medium circulation passage 82 in this way, while guaranteeing 82 section of heat exchange medium circulation passage
Cassava mash relative to optimum size, and then guarantee the proper flow of heat exchange medium.
Mash heat exchanger of the invention will almost be overhauled for two, three weeks before no improvement, by only needing after improving
Being safeguarded at three months can work normally.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
In the technical scope disclosed by the present invention, any changes or substitutions that can be easily thought of by anyone skilled in the art,
It should be covered by the protection scope of the present invention.
Claims (9)
1. a kind of novel process for cassava production alcohol, including saccharification step, which is characterized in that the saccharification step packet
Include following steps：
1. water is added through screw feeder after crushed in raw material cassava, into desanding before tank, cassava slurry is obtained after mixing evenly, through desanding
Pump squeezes into the silt being mingled in desander removal raw material, into mixing tank；
2. thermostable α-amylase is added by 6 units/gram raw materials in mixing tank, beats through spice pump to 2# mash and change after stirring evenly
Hot device exchanges heat with the liquefied fermented glutinous rice of liquefied pot after 2#, and temperature rises to 55 ~ 60 DEG C, and liquefied fermented glutinous rice is cooled to 55 ~ 60 by 75 ~ 80 DEG C simultaneously
DEG C, 55 ~ 60 DEG C of slurries after heat exchange enter liquefied pot before 1#；
3. liquefied pot is warming up to 65 ~ 70 DEG C with steam before 1#, reach the gelatinization point of cassava；
It is changed 4. material liquefied pot before 1# is beaten through 1# mash ring heat pump to 1# mash heat exchanger with the boiling wine with dregs come out from after-ripening device
Heat, temperature rise to 80 ~ 85 DEG C and enter liquefied pot before 2#, while boiling wine with dregs is cooled to 75 ~ 80 DEG C by 90 ~ 95 DEG C, into 1# after liquid
Change tank；
5. the control of liquefied pot temperature is α-amylase the best use temperature at 80 ~ 85 DEG C before 2#, 3#；
6. material enters after-ripening device, after-ripening device temperature control through boiling feed pump after Jet liquefier and the uniform Hybrid Heating of steam
System is at 90 ~ 95 DEG C；
7. material from after-ripening device come out after through 1# mash heat exchanger cooling after enter 1# after liquefied pot, while after 1# liquefied pot press 4
Thermostable α-amylase is added in units/gram raw material；
8. material liquefied pot after 2# liquefies after, pump, which is beaten to 2# mash heat exchanger, is cooled to 55 ~ 60 DEG C, into saccharifying tank, saccharification
Carbohydrase is added in tank.
2. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that the 1# mash changes
Hot device and 2# mash heat exchanger are broad passage plate mash heat exchanger.
3. a kind of novel process for cassava production alcohol as claimed in claim 2, which is characterized in that the fat pipe plate
Formula mash heat exchanger, including include mash heat exchanger shell, heat exchange medium circulation passage, heat exchange medium circulation passage, heat exchange core
Body, the import of heat exchange mash, heat exchange mash outlet and heat exchange medium import, heat exchange media outlet, the heat exchange medium into
Mouthful, heat exchange medium exit and heat exchange mash import, heat exchange mash outlet be located at mash heat exchanger shell on and respectively with it is described
The heat exchange medium circulation passage of heat exchange core body, heat exchange medium circulation passage connection；The heat exchange medium circulation passage it is each
It is fixedly connected between a plate and plate by point type spacing column and is changed to square steel type wire type and is fixedly connected.
4. a kind of novel process for cassava production alcohol as claimed in claim 3, which is characterized in that the board-like mash
The height of heat exchanger channel is 16mm, width 100mm.
5. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that the step 1. in
The Cassava crushing granularity of spice：∅1.6~1.8mm ；Spice temperature：35~40℃；Spice water addition ratio：1：2.3 ~ 2. spice concentration：
25~26BX°。
6. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that liquid before the 1#
Change the tank residence time：30~40min；The liquefied pot residence time before 2#, 3#：60~90min.
7. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that the injection liquefaction
Device temperature：90~95℃；The after-ripening device residence time：40~60min.
8. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that liquefied pot after described
Residence time：60~90min.
9. a kind of novel process for cassava production alcohol as described in claim 1, which is characterized in that the saccharifying tank sugar
Change enzyme additive amount：150 ~ 200 units/gram raw materials；Saccharifying tank temperature：55~60℃；The saccharifying tank residence time：40~60min.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111484914A (en) * | 2020-05-25 | 2020-08-04 | 镇江丹和醋业有限公司 | Process for improving fermentation quality of fermented glutinous rice by using enzyme preparation |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101195836A (en) * | 2008-01-04 | 2008-06-11 | 广西明阳生化科技股份有限公司 | Novel technique for producing manioc waste ethanol |
| WO2009100042A2 (en) * | 2008-02-05 | 2009-08-13 | Syngenta Participations Ag | Systems and processes for producting biofuels from biomass |
| WO2010022045A1 (en) * | 2008-08-20 | 2010-02-25 | Novozymes A/S | Processes for producing fermentation products |
| CN102978244A (en) * | 2012-11-23 | 2013-03-20 | 吴江永祥酒精制造有限公司 | Process for producing alcohol by thick mash fermentation from cassava raw material |
| CN103014073A (en) * | 2012-11-23 | 2013-04-03 | 吴江永祥酒精制造有限公司 | Method for recycling waste heat of liquefied wine with dregs in stewing section of cassava alcohol |
| CN105368878A (en) * | 2014-08-12 | 2016-03-02 | 江苏花厅生物科技有限公司 | Method for producing alcohol by using manihot esculenta crantz as raw material |
| CN105841525A (en) * | 2016-05-27 | 2016-08-10 | 南阳天泰建设工程有限公司 | Wide-channel plate heat exchanger |
| CN106636223A (en) * | 2016-09-27 | 2017-05-10 | 广西罗城科潮基业科技发展有限公司 | Processing method for utilizing cassava residue and cassava to produce alcohol |
| CN107287261A (en) * | 2016-03-30 | 2017-10-24 | 郑州大学 | A kind of liquefying starchiness raw material saccharification waste heat reclaiming process |
-
2018
- 2018-07-10 CN CN201810751858.XA patent/CN108823262A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101195836A (en) * | 2008-01-04 | 2008-06-11 | 广西明阳生化科技股份有限公司 | Novel technique for producing manioc waste ethanol |
| WO2009100042A2 (en) * | 2008-02-05 | 2009-08-13 | Syngenta Participations Ag | Systems and processes for producting biofuels from biomass |
| WO2010022045A1 (en) * | 2008-08-20 | 2010-02-25 | Novozymes A/S | Processes for producing fermentation products |
| CN102978244A (en) * | 2012-11-23 | 2013-03-20 | 吴江永祥酒精制造有限公司 | Process for producing alcohol by thick mash fermentation from cassava raw material |
| CN103014073A (en) * | 2012-11-23 | 2013-04-03 | 吴江永祥酒精制造有限公司 | Method for recycling waste heat of liquefied wine with dregs in stewing section of cassava alcohol |
| CN105368878A (en) * | 2014-08-12 | 2016-03-02 | 江苏花厅生物科技有限公司 | Method for producing alcohol by using manihot esculenta crantz as raw material |
| CN107287261A (en) * | 2016-03-30 | 2017-10-24 | 郑州大学 | A kind of liquefying starchiness raw material saccharification waste heat reclaiming process |
| CN105841525A (en) * | 2016-05-27 | 2016-08-10 | 南阳天泰建设工程有限公司 | Wide-channel plate heat exchanger |
| CN106636223A (en) * | 2016-09-27 | 2017-05-10 | 广西罗城科潮基业科技发展有限公司 | Processing method for utilizing cassava residue and cassava to produce alcohol |
Non-Patent Citations (3)
| Title |
|---|
| 张树河等: "木薯淀粉制燃料酒精的技术研究", 《福建农业学报》 * |
| 陆婷婷等: "高浓度木薯粉浆糊化液化粘度的研究", 《食品工业科技》 * |
| 高义霞等: "响应面法优化α-淀粉酶酶解木薯淀粉的工艺及动力学模型研究", 《中国粮油学报》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111484914A (en) * | 2020-05-25 | 2020-08-04 | 镇江丹和醋业有限公司 | Process for improving fermentation quality of fermented glutinous rice by using enzyme preparation |
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