CN110452092A - A kind of method that the coupling of tower film carries out material and is thermally integrated purification alcohol fuel - Google Patents
A kind of method that the coupling of tower film carries out material and is thermally integrated purification alcohol fuel Download PDFInfo
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- CN110452092A CN110452092A CN201910722750.2A CN201910722750A CN110452092A CN 110452092 A CN110452092 A CN 110452092A CN 201910722750 A CN201910722750 A CN 201910722750A CN 110452092 A CN110452092 A CN 110452092A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a kind of tower films to couple the method for carrying out material and being thermally integrated purification alcohol fuel, this method is the three-tower rectification section formed with a pressurization essence gold-plating tower of connecting again after the thick gold-plating tower of a decompression pressurized raw gold-plating tower in parallel, rectifying-purifying technique system of the rectifying section composition constituted with a membrane separation device, pass through the material and heat system matched to rectifying section and rectifying section, to reduce unit product steam consumption, it is combined by Steam soak UF membrane, while reducing the requirement of feed ethanol concentration, it reduces the number of plates of pressurized raw tower and reduces reflux ratio, to carry out rectification and purification to biomass ferment mash to prepare the process for the high straight alcohol for meeting alcohol fuel requirement, and reach the production purpose of environment protection energy-saving efficient.The method of the present invention, which has, greatlys save many advantages such as steam consumption, primary discharging quality is high, system automation degree is high, installation area is small, plant maintenance is convenient, film consumption product material is reliability and durability, resource utilization is high.
Description
Technical field
The present invention relates to a kind of tower films to couple the method for carrying out material and being thermally integrated purification alcohol fuel.
Technical background
The development and utilization of fossil energy are faced with serious environmental pollution and resource exhaustion problem.There is carbon when ethanol combustion
Oxygen composition is moderate, octane number is high, nonoverload greenhouse gases and the advantages that pollutant after burning, and being used as gasoline additive makes
It is huge with, market.What on September 15th, 2017 national ministries and commissions' joints were put into effect " makes about the production of bio-fuel ethyl alcohol and popularization is expanded
With the embodiment of vehicle-use alcohol gasoline " in, it is desirable that vehicle ethanol all standing is realized substantially in the year two thousand twenty the whole country.Fuel
Ethyl alcohol is the dehydrated alcohol that volumetric concentration reaches 99.5% or more, has oxygen enriching burning-aid when using as fuel oil improver, reaches
Energy-saving and environment-friendly purpose.Meanwhile bio-fuel ethyl alcohol has reproducibility, therefore biochemical routes prepare the technique quilt of alcohol fuel
Domestic and international ethyl alcohol industry is widely used.In the case where national energy conservation and emission reduction requires to improve and alcohol fuel subsidizes reduced background, for up to
The purpose of this profit is dropped to enterprise, and a main approach is by continuing to optimize the technique of bio-fuel ethyl alcohol purification come real
It is existing.Ethyl alcohol volumetric concentration is 2~20% in the biomass ferments mash such as starch, fructosyl polysaccharide, cellulose family, raw with starch
When fermentation of materials, ethyl alcohol volumetric concentration can reach 8~20%.Rectifying needs during mentioning alcohol fuel by extractive distillation with salt
Or molecular sieve adsorbing and dewatering is realized.For this process route, optimization process is concentrated mainly on the heat recovery and utilization work of rectifying section
In skill design [1: Li Penghui alcohol fuel three-tower differential pressure distillation technique simulative optimization of document and the Xi'an tower technological design [D]:
Northwest University, 2017；Document 2:Shelfer JR, Bennett H, Shelfer Grant T, et al.Process and
apparatus for commercially producing motor fuel-grade ethanol:WO2008024109A1
[P] .2008-02-28.], or the more energy-efficient new technology of rectifying section use in alcohol fuel preparation process.
Vapor permeable membrane purification technique have separative efficiency height, high degree of automation, it is easy to operate, to equipment use
Condition is of less demanding, do not introduce third component, not environment easy to pollute the advantages that, have in organic solvent subtractive process obvious excellent
Gesture.Using vapor permeable membrane process for separating and purifying, whole system steam mono-consumption can save steam compared with traditional technique and reach
30%~50% or more [document 3, Gu Xuehong, Xiangli powder Juan, Yu Congli, wait a kind of biomass dehydrated alcohol of production method and
Device: CN104262090B [P] .2016-06-29.].
[document 4, Han Fei, Ding Weijun, Lin Changjun wait tri- tower triple-effect differential pressure of to be thermally integrated and produce altogether patent CN102126920B
Boiling the method for ethyl alcohol: CN102126920B [P] .2013-09-25.] three tower triple-effect differential pressures of description are thermally integrated the work of rectifying ethyl alcohol
Two more traditional tower rectification and purification techniques of skill (document 5, Zhang Minhua, Dong Xiuqin, Lv Huisheng wait production of alcohol fuel:
CN1298859C [P] .2007-02-07.]) there are apparent power savings advantages.Rectifying section uses thick gold-plating tower, rectifying column I, rectifying column
II 3 tower integrating device rectifying ethyl alcohol, rectifying section use molecular sieve adsorbing and dewatering.In heat main flow, extraneous primary steam is first given
II reboiler of rectifying column provides heat source, and overhead vapours is heated to I tower reactor of rectifying column.Thick gold-plating tower is with there are two reboiler, heat sources one
Aspect derives from I overhead stream of rectifying column, on the other hand derives from the dehydrated alcohol product steam of molecular sieve absorbing unit.Material
In main flow, fermentation liquid enters thick gold-plating tower top after two sections of preheatings, slightly evaporates the thick fume of rear tower top through the rear portion that exchanges heat
It forms thick wine lime set and feeds rectifying column I.Tower top azeotropic ethanol gas a part is back to I top of rectifying column after rectifying, a part
Into molecular sieve absorbing unit.Kettle material enters the further rectifying in II lower part of rectifying column after rectifying, and distillate a part flows back,
Other enter rectifying column I.This technical process only optimizes description to rectifying section, practical to be equipped with molecular sieve absorbing process process
In, exist into molecular sieve ethanol solution requirement concentration height (ethyl alcohol volumetric concentration >=93.5% or so), and then to I column plate of rectifying column
The more demanding problem of number.Molecular sieve absorption process can generate about 25% low-concentration ethanol solution, if this part is not returned
It is on the contrary to will cause additional steam consumption again with the utilization rate that can reduce raw material.In addition, distillation process uses multiple flash tanks,
Increase equipment investment.
Patent CN104262090B [document 3] describes a kind of method of bio-fuel ethyl alcohol process for refining, is driven using heat
The technology that the dynamic way of distillation is combined with UF membrane.Rectifying section uses three tower parallel connection integrating devices, respectively pressurization, normal pressure, decompression
Condition, rectifying section have used infiltration evaporation membrane process.In heat unit, I overhead vapours of compression rectification tower is atmospheric distillation tower II
Tower reactor reboiler heating, II overhead vapours of atmospheric distillation tower are the heating of III tower reactor reboiler of vacuum rectification tower, steam needed for system
It is accessed by I reboiler of compression rectification tower, the product steam that infiltrating and vaporizing membrane generates provides preheating for fermentation liquid.Material unit
In, each the top of the distillation column discharging is directly accessed infiltration evaporation film device after mixed heat transfer.This technique is due to using three towers simultaneously
Connection design, therefore, the discharging temperature difference is relatively large, and compression rectification tower and the vacuum rectification tower temperature difference generate in such cases up to 50 DEG C
Heat utilization ratio it is low, however it remains the excessively high problem of energy consumption.
In conclusion currently, although the technique for bio-fuel ethyl alcohol has optimization to mention from rectifying section and rectifying section
Rise improvement, but Steam soak membrane technology to input concentration require it is low, separative efficiency is high, without reflux etc. operating features, with
Agreeing with for rectifying section is still significantly improved space during combination, in conjunction with the rectification process and UF membrane feature of alcohol fuel,
It can further achieve the purpose that reduce integrated artistic energy consumption by idetified separation.
Summary of the invention
The technical problems to be solved by the present invention are: bioanalysis prepare alcohol fuel technique rectifying exists in the prior art
Section and rectifying section material and heat compatible degree be not high, and technique entirety energy consumption has the problem of optimization is further greatly lowered, and provides
A method of the new rectifying of combination rectifying column and UF membrane is integrated to strengthen purification alcohol fuel, and this method has reasonable distribution object
Stream amount, the advantage for making full use of material heat, can further reduce between rectifying column and rectifying column and membrane separation device it
Between temperature difference, reach and improve rectifying section and rectifying section material and heat compatible degree, further decrease the advantages of system energy consumption.
To achieve the above object, the technical scheme adopted by the invention is as follows:
A kind of tower film coupling of the present invention carries out material and is thermally integrated the method for refining alcohol fuel, this method comprises:
Fermentation liquid is divided into two-way mash: mash F1 and mash F2 after three-level preheats；Wherein mash F1 is directly fed
Depressurize topping still 1；The direct feed pressurization topping still 2 of mash F2, the decompression topping still 1 and pressurization topping still 2 are in material stream
It is connected in parallel upwards, mash F1, which enters decompression topping still 1, to carry out depressurizing the overhead ethanol steam a1 obtained after thick evaporate, to karusen
Enter compression rectification tower 3 after the heat exchange of liquid level-one and carries out compression rectification；The waste water that decompression 1 tower reactor of topping still obtains is to fermentation liquid three
Discharge system after grade heat exchange；
Mash F2 enter pressurization topping still 2 carry out pressurized raw evaporate after obtain overhead ethanol steam to decompression topping still 1 boil again
Device h11 heat exchange, a part of alcohol vapour b1 are back to pressurized raw and evaporate her tower 2, and a part of alcohol vapour b2 is pre- by extraneous steam
Enter vapor permeation membrane component 4 after heat, pressurization 2 tower reactor ethanol solution b3 of topping still enters compression rectification tower 3, tower after heat exchange
Discharge system after kettle waste water exchanges heat to fermentation liquid three-level；
After 3 overhead ethanol steam of compression rectification tower is to pressurization 2 reboiler h21 of topping still heat exchange, a part of alcohol vapour c1
Enter pressurized raw after reflux, a part of alcohol vapour c2 and pressurization 2 tower reactor ethanol solution b3 of topping still heat exchange and evaporates 2 pressurized raw of tower
It evaporates, discharge system after tower reactor waste water exchanges heat to fermentation liquid three-level；
It is pressurization 2 reboiler h22 of topping still and fermentation liquid that the purification of vapor permeation membrane component 4, which obtains product steam d1 successively,
Process of alcohol products, purified obtained outlet waste water discharge system after condensation are obtained after secondary heat exchange；
The whole system that this method is related to includes rectifying section and rectifying section, and wherein rectifying section includes that the decompression that is connected in parallel is thick
Evaporate tower 1, pressurization topping still 2, the compression rectification tower 3 linked with above-mentioned cascade towers and four reboilers h11, h21, h22 and
h31；Rectifying section includes vapor permeation membrane component 4, and wherein vapor permeation membrane component 4 is provided with a preheater and a condensation
Device；Rectifying section and rectifying section pass through the preheated device of tower top of pressurization topping still 2 and the entrance progress material of vapor permeation membrane component 4
Connection；4 products export of vapor permeation membrane component and pressurization 2 reboiler h22 of topping still carry out heat exchange connection；
Wherein pressurization topping still 2,3 overhead ethanol opposing steam flow ratio of compression rectification tower are all 0.5~3.5；Preheated entrance
The alcohol vapour volume concentration range of vapor permeation membrane component 4 is 55% or more；
In the above scheme, alcohol fuel rectifying section requires to will affect pressurization to the ethanol vapor concentration into film separation system
Number of plates parameter designing, operation temperature, pressure and reflux ratio of topping still 2 etc.；It is preferred that preheated enter vapor permeation membrane component 4
Alcohol vapour b2 volume concentration range be 75% or more.
In the above scheme, depressurize topping still 1, pressurization topping still 2, compression rectification tower 3 the number of plates be respectively >=35,
>=40, >=55, decompression 1 absolute pressure range of topping still be 25~55kPa, pressurization 2 absolute pressure range of topping still be 100~
500kPa, compression rectification tower 3 absolute pressure range are 400~600kPa, decompression topping still 1, pressurization topping still 2, compression rectification tower 3
Tower top temperature range is respectively 57~68 DEG C, 82~110 DEG C, 120~130 DEG C of decompression topping stills 1, pressurization topping still 2, pressurization essence
The bottom temperature range for evaporating tower 3 is respectively 72~86 DEG C, 100~130 DEG C, 125~135 DEG C.
In the above scheme, depressurize topping still 1, pressurization topping still 2, compression rectification tower 3 the number of plates be respectively 35~40
A, >=44,55~65, pressurization 2 absolute pressure range of topping still are 140~485KPa, the tower top temperature range for the topping still 2 that pressurizes
It is 85~100 DEG C, the bottom temperature range of pressurization topping still 2 is 110~130 DEG C.
Topping still 2,3 overhead ethanol opposing steam flow of compression rectification tower pressurize than being respectively 1.5~2.5,1.5~3.5.
In the above scheme, vapor permeable membrane is organic zeolite membrane or polyimide fiber film.
Biomass material source for this process feeds fermentation liquid includes cellulose, starch, corn, cassava, jerusalem artichoke
One of biomass such as rhizome, straw are a variety of, fermentation liquid ethyl alcohol volumetric concentration >=2%.
The innovative point of this method is, with rectifying section existing for bio-fuel ethyl alcohol prior art and rectifying section material and heat
It is not high to measure compatible degree, the high problem of entire process energy consumption influences rectifying section in conjunction with rectifying section process conditions, can further decrease
Rectifying section equipment requirement and steam usage amount is reduced, the characteristics of in conjunction with Steam soak UF membrane without low-concentration ethanol by-product, taken
Disappear rectifying section refluxing ethanol, can further decrease the steam usage amount of rectifying section.It proposes one and fuel second is prepared by biological mash
The low energy consumption variation route of alcohol.
The present invention has the following advantages:
(1) vapor permeable membrane purification technique have primary discharging quality height, high degree of automation, it is easy to operate, to equipment
The advantages such as use condition is of less demanding, do not introduce third component, environment not easy to pollute have bright in organic solvent subtractive process
Aobvious advantage；
(2) present invention is high with rectifying section and rectifying section material and heat matching degree, the equipment room temperature difference is moderate, heat exchange is filled
Point, the advantages such as heat utilization ratio height, system main heating source is only provided by the reboiler h31 of compression rectification tower 3 by extraneous, and is mentioned
The pure section of minimal amount of external heat source of warm needs entered before vapor permeable membrane；
(3) it is purified using vapor permeable membrane, the requirement to rectifying section rectifying tower plates number, operating condition etc. can be reduced, into
One step reduces rectifying section energy consumption；
(4) compared with traditional molecular sieve adsorbs purifying technique, in the product using the generation of vapor permeable membrane purification process
Raw material availability can be disposably improved without the rectifying again that flows back without low-concentration ethanol, reduces system energy consumption；
(5) compared with traditional rectifying mode, the rectifying of this combined column can save steam nearly 60% with barrier separation integral process；
Compared with traditional molecular sieve adsorbs purifying technique, the rectifying of this combined column and barrier separation integral process can save steam about 25%.
Whole system steam mono-consumption can be down to 1.1 tonsSteam/ tonAlcohol fuelLeft and right.
In short, the method for the present invention realizes the purpose for preparing alcohol fuel by biofermentation mash high-efficiency low energy consumption.With it is existing
Some rectifying, purifying technique are compared, and there is group technology provided by the present invention raw material availability height, product once to produce purity
High (the process of alcohol products volumetric concentration through vapor permeable membrane separating-purifying is up to 99.5% or more), product quality height, equipment
It is at low cost, system automation rate is high, easy to operate, unit consumption of product is low, environmental-friendly, reproducibility, rectifying and purifying technique
The advantages that material and heat matching degree are high, alcohol fuel Atom economy is high.
Detailed description of the invention
Fig. 1 is that a kind of tower film coupling of the present invention carries out material and the process flow for the method for being thermally integrated purification alcohol fuel is shown
It is intended to.
In Fig. 1,1 is decompression topping still, and 2 be the topping still that pressurizes, and 3 be compression rectification tower, and 4 be vapor permeation membrane component, h11
To depressurize 1 reboiler of topping still, h21, h22 are pressurization 2 reboiler of topping still, and h31 is 3 reboiler of compression rectification tower, and F1, F2 divide
The mash of decompression topping still 1, the topping still 2 that pressurizes Wei not entered, a1 is to be gone out by 1 tower top of decompression topping still and enter compression rectification tower
3 alcohol vapour, b1, b2 are respectively the pressurize reflux of topping still 2 and the alcohol vapour into vapor permeable membrane 4, and c1, c2 are respectively
The reflux of compression rectification tower 3 and the alcohol vapour for entering pressurization topping still 2, d1 are the product steam of vapor permeation membrane component 4.
Specific embodiment
Below by specific embodiment, the present invention is described in detail, but these embodiments are not to the contents of the present invention
It is construed as limiting.When embodiment includes that the variation of charging mash concentration of alcohol, the three tower numbers of plates and reflux ratio change, system is to steam section
The about influence of degree.But it is not excluded for guarantee product second by other optimization of operating condition based on artwork, Lai Shixian
Determining alcohol meets as under alcohol fuel use premise, and acquirement further decreases the effect that unit product consumes steam consumption.
Such as Fig. 1, tower film coupling of the present invention carries out material and the method and process flow diagram for being thermally integrated purification alcohol fuel
Shown, the material flow and heat process of present invention process are specific as follows:
Material flow: fermentation liquid divides two-way mash F1, F2 after three-level preheats, and wherein mash F1 enters decompression topping still
1, mash F2 enter pressurization topping still 2.After depressurizing topping still 1, tower bottoms obtains waste water, tower after to the heat exchange of mash three-level
It pushes up after alcohol vapour a1 carries out level-one preheating to fermentation liquid and enters compression rectification tower 3.After mash F2 enters pressurization topping still 2,
Tower bottoms obtains waste water discharge system after to the heat exchange of mash three-level, and overhead ethanol steam divides after exchanging heat to 1 reboiler h11 of tower
For two parts, alcohol vapour b1 reflux, alcohol vapour b2 enters Steam soak membrane separation assemblies 4, and product is obtained after UF membrane and is steamed
Vapour d1 and waste water, product steam d1 successively give pressurization 2 reboiler h22 of topping still and charging fermentation liquid secondary heat exchange, are fired
Expect alcohol product.Alcohol vapour a1 is mixed before entering compression rectification tower 3 with pressurization 2 tower reactor ethanol solution b3 of topping still.Pressurization essence
It evaporates 3 overhead ethanol steam of tower and gives pressurization 2 reboiler h21 of topping still heat exchange rear portion alcohol vapour c1 reflux, a branch part second
Alcohol steam c2 is through evaporating tower 2 into pressurized raw with after pressurization 2 tower reactor ethanol solution of topping still heat exchange.3 tower bottoms of compression rectification tower warp
Discharge system after obtaining waste water is crossed after exchanging heat to mash three-level；
Heat process: by the primary steam from the external world to the 3 reboiler h31 heat supply of compression rectification tower.Topping still 2 pressurize again
Boil the origin of heat of device h21 in 3 overhead ethanol steam of compression rectification tower, reboiler h22 is by the fuel that purifies through vapor permeable membrane
Alcohol vapour d1 heat supply.The origin of heat of 1 reboiler h11 of topping still is depressurized in pressurization 2 overhead ethanol steam of topping still.Karusen
Liquid successively passes through 1 overhead vapours a1 of tower, alcohol vapour d1 and the heat exchange of 1,2,3 tower bottoms of tower, 4 separation process of vapor permeation membrane component
It is middle to need a small amount of steam, it is provided by the external world, but can ignore relative to the heat consumption of whole system；
It is as follows that further explanation of the technical solution of the present invention:
For the optimization foundation of rectifying section are as follows: (1) mash is sufficiently pre- into being carried out before each tower according to each tower operational temperature conditions
Heat；(2) mash follows the minimum principle of system heat losses into tower amount and reflux ratio distribution；(3) vapor permeable membrane is given full play to
The separation advantage of High Purity and low concentration charging；(4) feeding manner is matched with the selection of each Deethanizer design parameter, operating condition；(5)
Meet UF membrane requirement feature based on tower top fume concentration and temperature and match two groups of Steam soak membrane separation devices, avoids feed liquid temperature
It spends and carries additional consumption of calorie；
For the optimization foundation of rectifying section are as follows: about 1/4 can be generated in the advanced molecular sieve absorption purifying technique of industry at present
Low-concentration ethanol ingredient need to recycle again this part low-concentration ethanol to improve the utilization rate of biomass material
It utilizes, purification needs extra steam.And use vapor permeable membrane purifying technique to generate and flow back without low-concentration ethanol and recycle, it can
Substantially reduce steam consumption.
The method of the present invention effect is described further below by specific embodiment.
Embodiment 1
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and fixed pressurization 2 reflux ratio of topping still is 1.2, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 5.5%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 1 in table 1.
Embodiment 2
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and fixed pressurization 2 reflux ratio of topping still is 1.2, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 11.9%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 2 in table 1.
Embodiment 3
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and fixed pressurization 2 reflux ratio of topping still is 1.2, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 13.9%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 3 in table 1.
Embodiment 4
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and fixed pressurization 2 reflux ratio of topping still is 1.2, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 15.8%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 4 in table 1.
Experimental comparison results when 1. different feeds fermentation liquid concentration of alcohol of table
In summary, under this process flow operation, fermentation liquid input concentration increases, and the concentration of process of alcohol products
When close, steam consumption is reduced, and opposite traditional handicraft and relative combinations tower molecular sieve integrated technique save quantity of steam ten clearly
It is aobvious.In existing zymotechnique, when using corn and other starches biolobic material as fermenting raw materials, fermentation liquid ethyl alcohol volumetric concentration is 12%
Left and right, product design fully meets alcohol fuel requirement (concentration of alcohol >=99.5%), technique after feeding this process flow
It is obvious to save steaming effect.
Embodiment 5
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 48, and fixed pressurization 2 reflux ratio of topping still is 1.2, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 11.9%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 5 in table 2.
Embodiment 6
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and reducing pressurization 2 reflux ratio of topping still is 1.0, fixed pressurization
3 reflux ratio of rectifying column is 1.8.Fermentation liquid ethyl alcohol volumetric concentration is 11.9%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 6 in table 2.
Embodiment 7
Process flow chart be Fig. 1 described in, fermentation liquid raw material be corn, 29.9 DEG C of temperature.Fixed decompression topping still 1 and plus
3 number of plates of rectifying column is pressed, fixed pressurization 2 number of plates of topping still is 46, and fixed pressurization 2 reflux ratio of topping still is 1.2, reduces pressurization
3 reflux ratio of rectifying column is 1.5.Fermentation liquid ethyl alcohol volumetric concentration is 11.9%, after charging, the operation work of each tower in combined column
Condition, the quantity of steam of system unit alcohol fuel consumption, the Energy-saving Situation of opposite traditional handicraft and relative combinations tower molecular sieve are integrated
The Energy-saving Situation of technique is as shown in embodiment 7 in table 2.
Experimental comparison results when 2. reflux ratio of table changes
In summary, under this process flow operation, when pressurization 2 number of plates of topping still increases, product concentration of alcohol meets combustion
Expect ethyl alcohol requirement (concentration >=99.5%), steam consumption is slightly reduced.When reducing pressurization 2 reflux ratio of topping still, fuel second
Alcohol product design meets alcohol fuel requirement (concentration >=99.5%), and steam consumption increases.Compression rectification tower 3 is reduced to return
Stream than when, process of alcohol products concentration meets alcohol fuel requirement (concentration >=99.5%), steam consumption increase.With biography
It unites technique or compared with combined column molecular sieve integrated technique, three above embodiment steam consumption is saved obvious.
The present invention relates to the methods for realizing the preparation of bio-fuel ethyl alcohol with combined column rectifying and UF membrane integrating device.This hair
It is bright that advantageous feature is purified based on membrane process, by matched rectifying section and rectifying section material and thermal relationship, also have into one
Step reduces the advantages of System steam dosage, that is, has advantage efficiently good using resource, the feature of environmental protection.Film device is in efficiently purification second
The technical maturity of the organic compounds such as alcohol, also had using this process flow product separation degree is high, system automation degree is high,
The many advantages such as system footprint area is small, plant maintenance is convenient, film consumption product material is reliability and durability.Therefore, the invention has practical
Substitute the value of conventional rectification and purification group technology in existing bio-fuel ethyl alcohol production.
Claims (8)
1. a kind of tower film coupling carries out material and is thermally integrated the method for refining alcohol fuel characterized by comprising
Fermentation liquid is divided into two-way mash: mash (F1) and mash (F2) after three-level preheats；Wherein mash (F1) directly into
Material decompression topping still (1)；Mash (F2) directly feed pressurization topping still (2), the decompression topping still (1) and pressurization topping still
(2) it is connected in parallel on flow direction of material；
Mash (F1), which enters decompression topping still (1), to carry out depressurizing the overhead ethanol steam (a1) obtained after thick evaporate, to fermentation liquid
Enter compression rectification tower (3) after level-one heat exchange and carries out compression rectification；Obtained tower reactor waste water gives fermentation liquid three-level heat exchange heel row
System out；
Mash (F2), which enters pressurization topping still (2), to carry out obtaining overhead ethanol steam after pressurized raw evaporates to decompression topping still (1) again
Device (h11) heat exchange is boiled, a part of alcohol vapour (b1) is back to pressurization topping still (2), and a part of alcohol vapour (b2) is by outer
Enter vapor permeation membrane component (4) after boundary's steam preheating, pressurization topping still (2) tower reactor ethanol solution (b3) enters after heat exchange
Compression rectification tower (3), discharge system after tower reactor waste water exchanges heat to fermentation liquid three-level；
After compression rectification tower (3) overhead ethanol steam is to pressurization topping still (2) reboiler (h21) heat exchange, a part of alcohol vapour
(c1) it flows back, a part of alcohol vapour (c2) evaporates with after pressurization topping still (2) tower reactor ethanol solution (b3) heat exchange into pressurized raw
Tower (2) pressurized raw evaporates, discharge system after tower reactor waste water exchanges heat to fermentation liquid three-level；
It is pressurization topping still (2) reboiler (h22) and fermentation that vapor permeation membrane component (4) purification, which obtains product steam (d1) successively,
Process of alcohol products, purified obtained outlet waste water discharge system after condensation are obtained after mash secondary heat exchange；
The whole system that the method is related to includes rectifying section and rectifying section, and wherein rectifying section includes that the decompression that is connected in parallel is thick
Evaporate tower (1), pressurization topping still (2), the compression rectification tower (3) linked with above-mentioned cascade towers and four reboilers (h11),
(h21), (h22) and (h31)；Rectifying section includes vapor permeation membrane component (4), and wherein vapor permeation membrane component (4) is provided with one
A preheater and a condenser；The preheated device of tower top and Steam soak that rectifying section and rectifying section pass through pressurization topping still (2)
The entrance of membrane module (4) carries out material connection；Vapor permeation membrane component (4) products export and pressurization topping still (2) reboiler
(h22) heat exchange connection is carried out；
It wherein pressurizes topping still (2), compression rectification tower (3) overhead ethanol opposing steam flow ratio is all 0.5~3.5；Preheated entrance
The alcohol vapour volume concentration range of vapor permeation membrane component (4) is 55% or more.
2. according to the method described in claim 1, it is characterized by: the preheated ethyl alcohol for entering vapor permeation membrane component (4) steams
Vapour volume concentration range is 75% or more.
3. according to the method described in claim 1, it is characterized by: decompression topping still (1), pressurization topping still (2), compression rectification
The number of plates of tower (3) respectively >=35, >=40, >=55, decompression topping still (1) absolute pressure range is 25~55kPa, pressurization
Topping still (2) absolute pressure range is 100~500kPa, and compression rectification tower (3) absolute pressure range is 400~600kPa, depressurizes topping still
(1), pressurize topping still (2) and compression rectification tower (3) tower top temperature range be respectively 57~68 DEG C, 82~110 DEG C, 120~
130 DEG C, the bottom temperature range of decompression topping still (1), pressurization topping still (2) and compression rectification tower (3) is respectively 72~86 DEG C,
100~130 DEG C, 125~135 DEG C.
4. according to the method described in claim 3, it is characterized by: decompression topping still (1), pressurization topping still (2), compression rectification
The number of plates of tower (3) is respectively 35~40, >=44,55~65, and pressurization topping still (2) absolute pressure range is 140~485
KPa, pressurization topping still (2) tower top temperature range be 85~100 DEG C, pressurization topping still (2) bottom temperature range be 110~
130℃。
5. according to the method described in claim 1, it is characterized by: pressurization topping still (2), compression rectification tower (3) overhead ethanol
Opposing steam flow is than being respectively 1.5~2.5,1.5~3.5.
6. according to the method described in claim 1, it is characterized by: vapor permeable membrane is that organic zeolite membrane or polyimides are fine
Tie up film.
7. according to the method described in claim 1, it is characterized by: ethyl alcohol volumetric concentration >=2% of fermentation liquid.
8. according to the method described in claim 1, it is characterized by: the biomass material of fermentation liquid is cellulose, starch, jade
One of rice, cassava, jerusalem artichoke rhizome, plant straw biological matter are a variety of.
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