CN109704920A - From the energy-saving process method and device of low concentration fermentation liquid production alcohol fuel - Google Patents
From the energy-saving process method and device of low concentration fermentation liquid production alcohol fuel Download PDFInfo
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- CN109704920A CN109704920A CN201910137368.5A CN201910137368A CN109704920A CN 109704920 A CN109704920 A CN 109704920A CN 201910137368 A CN201910137368 A CN 201910137368A CN 109704920 A CN109704920 A CN 109704920A
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 172
- 238000000034 method Methods 0.000 title claims abstract description 156
- 230000008569 process Effects 0.000 title claims abstract description 101
- 238000000855 fermentation Methods 0.000 title claims abstract description 56
- 230000004151 fermentation Effects 0.000 title claims abstract description 56
- 239000007788 liquid Substances 0.000 title claims abstract description 55
- 239000000446 fuel Substances 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 238000004821 distillation Methods 0.000 claims abstract description 329
- 108010025037 T140 peptide Proteins 0.000 claims description 122
- 239000007789 gas Substances 0.000 claims description 76
- 239000012071 phase Substances 0.000 claims description 64
- 239000007791 liquid phase Substances 0.000 claims description 59
- 239000007792 gaseous phase Substances 0.000 claims description 53
- 238000007599 discharging Methods 0.000 claims description 35
- 238000000605 extraction Methods 0.000 claims description 28
- 229960000935 dehydrated alcohol Drugs 0.000 claims description 22
- 239000004235 Orange GGN Substances 0.000 claims description 20
- 239000001760 fusel oil Substances 0.000 claims description 19
- 230000008676 import Effects 0.000 claims description 18
- 230000018044 dehydration Effects 0.000 claims description 17
- 238000006297 dehydration reaction Methods 0.000 claims description 17
- 239000004121 copper complexes of chlorophylls and chlorophyllins Substances 0.000 claims description 16
- 239000004214 Fast Green FCF Substances 0.000 claims description 15
- 239000004179 indigotine Substances 0.000 claims description 15
- 235000012738 indigotine Nutrition 0.000 claims description 15
- 230000000694 effects Effects 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000004161 brilliant blue FCF Substances 0.000 claims description 13
- 235000012745 brilliant blue FCF Nutrition 0.000 claims description 13
- 239000002808 molecular sieve Substances 0.000 claims description 13
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical group [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 13
- 239000004176 azorubin Substances 0.000 claims description 12
- 239000001679 citrus red 2 Substances 0.000 claims description 12
- 239000004120 green S Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 12
- 239000002351 wastewater Substances 0.000 claims description 11
- 239000004177 patent blue V Substances 0.000 claims description 10
- 238000010992 reflux Methods 0.000 claims description 9
- 239000008346 aqueous phase Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 230000008016 vaporization Effects 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 238000009834 vaporization Methods 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims description 2
- 230000008595 infiltration Effects 0.000 claims 1
- 238000001764 infiltration Methods 0.000 claims 1
- 238000010025 steaming Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 31
- 230000008901 benefit Effects 0.000 abstract description 16
- 239000000203 mixture Substances 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000005457 optimization Methods 0.000 abstract description 2
- 235000019441 ethanol Nutrition 0.000 description 109
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 24
- 235000011941 Tilia x europaea Nutrition 0.000 description 24
- 239000004571 lime Substances 0.000 description 24
- 239000000047 product Substances 0.000 description 22
- 230000004069 differentiation Effects 0.000 description 14
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 229960004756 ethanol Drugs 0.000 description 11
- 239000012528 membrane Substances 0.000 description 10
- 235000013339 cereals Nutrition 0.000 description 6
- 239000004178 amaranth Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 241000196324 Embryophyta Species 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 3
- 239000004410 anthocyanin Substances 0.000 description 3
- 239000001654 beetroot red Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 240000003183 Manihot esculenta Species 0.000 description 1
- 235000016735 Manihot esculenta subsp esculenta Nutrition 0.000 description 1
- 241001560086 Pachyrhizus Species 0.000 description 1
- 240000006394 Sorghum bicolor Species 0.000 description 1
- 235000011684 Sorghum saccharatum Nutrition 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- LLPOLZWFYMWNKH-CMKMFDCUSA-N hydrocodone Chemical compound C([C@H]1[C@H](N(CC[C@@]112)C)C3)CC(=O)[C@@H]1OC1=C2C3=CC=C1OC LLPOLZWFYMWNKH-CMKMFDCUSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 150000004702 methyl esters Chemical class 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of energy-saving process methods from low concentration fermentation liquid production alcohol fuel and device more particularly to a kind of energy-saving process method and device for producing alcohol fuel by distillation process from industrial tail gas fermentation liquid.Entire ethanol refinery system includes at least four towers and the dewatering units such as first rectifying column, Second distillation column, third distillation column, the 4th rectifying column and other corollary equipments composition.It is thermally integrated between first rectifying column, four tower of Second distillation column, third distillation column and the 4th rectifying column, in addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.The heat-exchange system of optimization makes dewatering unit organically be unified with distillation system, improves the stability and flexibility of entire distillation system.The shortcomings that the present invention overcomes prior arts, the more currently advanced alcohol fuel rectification technique of operation energy consumption reduce by 30% or more, have significant practicability and economic benefit, have a extensive future.
Description
Technical field
The present invention relates to a kind of energy-saving process methods and device from low concentration fermentation liquid production alcohol fuel, more particularly to
A kind of energy-saving process method and device producing alcohol fuel by distillation process from industrial tail gas fermentation liquid.
Background technique
The problems such as with the in short supply of the energy resources such as petroleum, coal, environmental pollution, greenhouse effects, gets worse, fuel
Ethyl alcohol is as a kind of renewable energy, increasingly by the attention of various aspects.Traditional alcohol fuel mainly with cereal crops such as
Sorghum, corn, pachyrhizus, cassava etc. are raw material, are obtained by biofermentation approach.It is that alcohol fuel is made in raw material with grain, no
It is only expensive, there is also " strive grain with people, with grain strive ground " the phenomenon that.
Using industrial tail gas microbial fermentation technology, alcohol fuel, while the high egg of by-product are converted by steel and iron industry tail gas
White feed and compressed natural gas have the characteristics that raw material is sufficient, concentration degree is high, are easy to collect, be produced into traditional fuel ethyl alcohol
Originally it compares, overall cost is low, energy utilization rate is high, added value of product is high, it can be achieved that the resource for generating pollution to environment carries out
Higher value application, remarkable in economical benefits.
Since industrial tail gas fermentation belongs to gaseous fermentation process, very low (general ethanol content is only for concentration of alcohol in fermentation liquid
It is 2~4%.Unless otherwise specified, mass percent is referred both in the application text), it is far below traditional grain crop fermentation liquid second
Determining alcohol (10~16%).At present from the process of fermentation liquid production alcohol fuel, three column distillation methods, this method are mostly used
There are the higher disadvantages of production energy consumption.If industrial tail gas fermentation preparing fuel ethanol distillation process still uses common process method, must
So cause distillation process energy consumption very high, by the serious economy for restricting industrial tail gas producing fuel ethyl alcohol by ferment technique.
Chinese patent CN200410094085.0 discloses a kind of " production of alcohol fuel ", and its essence is using single wine with dregs
Tower, Dan Jingta add the original process method of molecular sieve, although process flow is simple, operation energy consumption is very high.
CN200710057523.X discloses a kind of " process of ethyl alcohol rectifying is carried out using three-tower heat integration device ":
Entire ethyl alcohol distillation system includes three towers such as topping still, low pressure azeotropy rectification column, high pressure azeotropy rectification column, and topping still, low pressure are total
It is thermally integrated between boiling rectifying column, three tower of high pressure azeotropy rectification column, topping still side line gas phase provides part for low pressure azeotropy rectification column
Energy, high pressure azeotropy rectification column top gaseous phase provide energy for topping still tower reactor, and alcohol product is by low pressure azeotropy rectification column and height
Pressure azeotropy rectification column produces respectively, and essence is still the double-effect rectification technique of single prefractionator, double smart towers, and operation energy consumption is high.
CN200710058736.4 discloses a kind of " fuel ethanol production equipment and method ", and its essence is using double prefractionators
The tri-columns rectification process method of (thick tower, rectifying column lower part), double smart towers (rectifier, recovery tower top) plus molecular sieve, slightly
It is thermally integrated operation between three tower, rectifying column and recovery tower towers, realizes triple effect technique, operation energy consumption is lower.
CN201010545523.6 disclose " the distillation dehydration device of a kind of alcohol fuel and general grade edible alcohol coproduction and
Technique ", the process that similar CN200710058736.4 is provided, topping still, combined column are thermally integrated between three towers of rectifying column
Operation, realizes triple effect technique, improvement part is: combined column top gaseous phase is divided into three after the boosting of ethanol vapor gas compressor
Stock, one go topping still reboiler, one go methanol tower reboiler, another stock that adsorbing tower with molecular sieve is gone to be dehydrated, dewatered nothing
Water-ethanol gas returns to rectification cell and heats to topping still tower reactor reboiler, the technique side that opposite CN200710058736.4 is provided
Method further reduced operation energy consumption.The methanol column being arranged in CN201010545523.6 belongs to the general grade edible ethanol of coproduction
Required equipment, but redundant equipment is belonged to for fuel alcohol plant.Methanol concentration is well below concentration of alcohol, rectifying in fermentation liquid
Resulting azeotropic alcohol can meet GB 18350-2013 " fuel ethanol " standard without methanol removal after being dehydrated.Pressure
The setting of contracting machine considerably increases CN201010545523.6 and provides the power consumption of process, and increases the (compression of dynamic equipment
Machine) investment and maintenance cost.
CN201710542687.5 discloses " a kind of alcohol fuel energy-saving clean production method ", alcohol fuel rectifying
Cheng Shizhi is consistent with CN200710058736.4, is all to use double prefractionators (thick tower, rectifying column lower part), double smart towers (on rectifying column
Portion, recovery tower top) add the tri-columns rectification process method of molecular sieve, the difference is that being used for using dewatered dehydrated alcohol gas
Fermentation liquid is preheated, this technique is identical as CN201010545523.6.CN201710542687.5 with
CN201010545523.6 is the difference lies in that in the process that CN201710542687.5 is provided, " the of rectifying and dewatering unit
The heating steam of one smart tower reboiler is live steam, and the steam condensation water of discharge send to the first smart tower tower reactor after collecting and directly heats
Tower bottoms ", by this process, the first smart tower tower reactor reboiler can be omitted completely, directly introduce steam into the first smart tower tower
Kettle can reach same effect using direct steam heating.The process that CN201710542687.5 is provided is opposite
CN201010545523.6 without substantive breakthrough, and steam condensate be directly mixed in the first smart tower tower reactor waste water belong to it is very uneconomical
Method.
Summary of the invention
The purpose of the present invention is to provide a kind of energy-saving process methods and dress from low concentration fermentation liquid production alcohol fuel
It sets, produces the energy-saving process method and device of alcohol fuel by distillation process especially from industrial tail gas fermentation liquid, it can be with
The shortcomings that overcoming prior art.The present invention adopts breakthroughly on the Process ba- sis of currently used three towers ethanol refinery system
It is thermally integrated process with four tower rectifying, quadruple effect, greatly reduces operation energy consumption.Process provided by the invention has significant
Practicability and economic benefit.
It is provided by the invention from low concentration fermentation liquid production alcohol fuel energy-saving process method include:
1) first rectifying column, Second distillation column, third distillation column and the 4th rectifying column are included at least；
2) first rectifying column described in is combination tower, and first rectifying column top is the first rectifying section, and middle part is to take off light section, under
Portion is the first thick tower；
3) Second distillation column described in is stripper, and the following are the second thick towers for charging；
4) third distillation column described in is stripper, and the following are the thick towers of third for charging；
5) the 4th rectifying column described in is combination tower, and the 4th rectifier is the second rectifying section, and middle part is adopted for fusel oil
Section out, lower part are dewatering period；
6) first rectifying column, Second distillation column, third distillation column described in and between the 4th rectifying column to be thermally integrated, the 4th
Rectifying tower top gaseous phase provides institute's calorific requirement as third distillation column tower reactor heat source, for third distillation column；Third distillation column
Top gaseous phase provides institute's calorific requirement as Second distillation column tower reactor heat source, for Second distillation column；Second distillation column tower overhead gas
It is mutually used as first rectifying column tower reactor heat source, provides institute's calorific requirement for first rectifying column；
7) it goes dewatering unit gas phase first choice from the 4th rectifying tower top gaseous phase, is also possible to the evaporation of azeotropic alcohol liquid phase
Gas phase is also possible to other rectifying tower top gaseous phases in distillation system；
8) the dehydrated alcohol gas phase first choice of dewatering unit output is used as third distillation column tower reactor heat source, it is also possible to do
Two tower bottom of rectifying tower heat sources, it is also possible to do first rectifying column tower reactor heat source, it can also be used to fermentation liquid is preheated, it can also
For preheating first rectifying column charging, it can also be used to preheat Second distillation column charging, it can also be used to third distillation column charging is preheated,
It can also be used for preheating the 4th rectifying column charging；Aforementioned dehydrated alcohol vapor condensation object be process of alcohol products (or alcohol produce
Product).
By process provided by the invention, dewatering unit is molecular sieve water separation tower or infiltrating and vaporizing membrane.The dehydration
The light wine first choice of unit discharge enters first rectifying column, or is fed into the 4th rectifying column, Second distillation column or third distillation column.
By process provided by the invention, when being not necessarily to produce alcohol fuel, the dewatering unit can be deactivated, by
First rectifying column top or side take-off partially azeotropic alcohol, are total to by the 4th the top of the distillation column or upper aqueous phase side take-off part
Boil alcohol；Or first rectifying column extraction azeotropic alcohol enter the 4th rectifier column reflux tank or tower top, alcohol product all by
4th the top of the distillation column or upper aqueous phase side take-off；Or the 4th rectifying column extraction azeotropic alcohol enter first rectifying column return
Tank or tower top are flowed, alcohol product is all by first rectifying column tower top or upper aqueous phase side take-off.Realize alcohol fuel and azeotropic
The coproduction of alcohol product operates.
By process provided by the invention, fermentation liquid first choice is introduced into the first rectifying column；Second distillation column
Charging feed following liquid phase lateral line discharging from first rectifying column；The charging of third distillation column from first rectifying column feed with
Lower liquid phase lateral line discharging feeds following liquid phase lateral line discharging from Second distillation column；Fermentation liquid can also be divided into three strands, point
First rectifying column, Second distillation column and third distillation column are not gone；Fermentation liquid can also be introduced into Second distillation column, the first rectifying
The charging of tower feeds following liquid phase lateral line discharging from Second distillation column, and the charging of third distillation column is fed from first rectifying column
Following liquid phase lateral line discharging feeds following liquid phase lateral line discharging from Second distillation column；Fermentation liquid can also be introduced into third
The charging of rectifying column, Second distillation column feeds following liquid phase lateral line discharging from third distillation column, and the charging of first rectifying column comes
Following liquid phase lateral line discharging is fed from third distillation column or feeds following liquid phase lateral line discharging from Second distillation column；4th rectifying
The charging of tower is to feed the above liquid phase lateral line discharging, Second distillation column top distillate or its charging from first rectifying column with upper liquid
Phase lateral line discharging, third distillation column overhead or its mixed material for feeding the above liquid phase lateral line discharging.By preceding method,
It can be by Second distillation column top distillate or its above liquid phase lateral line discharging of charging, third distillation column overhead or its charging
The above liquid phase lateral line discharging introduces first rectifying column respectively or all and feeds the above position.
By process provided by the invention, there are three sections containing wine with dregs in entire rectifier unit system --- first rectifying column
Lower part, the lower part of Second distillation column and third distillation column lower part；First rectifying column, Second distillation column and third distillation column tower reactor
Waste water containing wine with dregs is discharged respectively；The discharge of 4th tower bottom of rectifying tower is free of wine with dregs waste water；The first rectifying column can be stripper, nothing
Top fractionation stage；Second distillation column can be combination tower, and rectifying section is arranged in top；Third distillation column can be combination tower, top
Rectifying section is set.
By process provided by the invention, the third distillation column can be deactivated, and the 4th rectifying tower top gaseous phase is made
For Second distillation column tower reactor heat source, institute's calorific requirement is provided for Second distillation column.
By process provided by the invention, one can also be increased between the third distillation column and the 4th rectifying column
The 5th rectifying column of platform, the 5th rectifying column and the first rectifying column, Second distillation column, third distillation column and the 4th rectifying are tower-shaped
Cheng Wuxiao is thermally integrated operation, further decreases operation energy consumption.4th rectifying tower top gaseous phase is heated as the 5th tower bottom of rectifying tower
Heat source provides institute's calorific requirement for the 5th rectifying column；5th rectifying tower top gaseous phase is as third distillation column tower reactor heat source
Third distillation column provides institute's calorific requirement；Third distillation column top gaseous phase is the second essence as Second distillation column tower reactor heat source
It evaporates tower and institute's calorific requirement is provided；Second distillation column top gaseous phase is mentioned as first rectifying column tower reactor heat source for first rectifying column
For institute's calorific requirement.The dehydrated alcohol gas phase first choice of dewatering unit output is used as the 5th tower bottom of rectifying tower heat source, it is also possible to do
Third distillation column tower reactor heat source, it is also possible to do Second distillation column tower reactor heat source, it is also possible to do first rectifying column tower reactor
Heat source.It, can be by Second distillation column top distillate or its above liquid phase lateral line discharging of charging, third rectifying by preceding method
Column overhead distillate or its above liquid phase lateral line discharging of charging, the 5th the top of the distillation column distillate or its above liquid phase side line of charging
Discharging introduces first rectifying column respectively or all and feeds the above position.
By process provided by the invention, azeotropic alcohol product first choice by the top of first rectifying column or upper part side line,
And the 4th at the top of rectifying column or upper part side line obtains respectively；Fusel oil is by liquid phase side take-off in the middle part of the 4th rectifying column；Institute
First rectifying column, Second distillation column, third distillation column, the 5th rectifying column and the 4th rectifying column stated all be compound tower structure, each
Rectifying section is all arranged in tower top.
By process provided by the invention, (charging above and below) is if setting near the 4th rectifying column feed entrance point
Dry fusel oil produces mouth, according to the operating conditions of input concentration and the 4th rectifying column, suitable fusel oil is selected to produce mouth discharge
Fusel oil.
By process provided by the invention, the process of alcohol products (or alcohol product or steam condensate) can be with
To first rectifying column produce azeotropic alcohol preheating, can to dewatering unit be discharged light wine preheating, can to fermentation liquid it is pre-
Heat, can to first rectifying column feeding preheating, can to Second distillation column feeding preheating, can be fed to third distillation column it is pre-
Heat can give the 4th rectifying column feeding preheating, recycle wherein heat, reduce cooling-water consumption.
By process provided by the invention, heat exchange is thermally integrated between the 4th rectifying column and third distillation column
The heat collection being thermally integrated between heat exchanger, third distillation column and Second distillation column between device, the 4th rectifying column and the 5th rectifying column
At the dehydrated alcohol gas phase for being thermally integrated heat exchanger, dewatering unit output between heat exchanger, Second distillation column and first rectifying column
Condenser can be using falling-film reboiler, pump forced circulation heat exchanger, the steam generator of indirect heat exchange, plate heat exchanger, heat
Hydrocone type reboiler.By process provided by the invention, in fermentation liquid rectifier unit, the 4th tower bottom of rectifying tower only described is again
Boiling device need to introduce external heat source heating, other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement.Described
The heat medium of 4th tower bottom of rectifying tower reboiler can be steam, conduction oil either heating furnace.It is thermally integrated the type of heat exchanger
Formula, be only using which kind of heat medium process provided by the invention implementation detail, do not constitute and spirit of that invention appointed
What is limited, and is that can be freely combined completely or realize this skill using the heat exchanger of other patterns for a person skilled in the art
Art.
Process provided by the invention be it is a kind of from low concentration fermentation liquid production alcohol fuel energy-saving process method and
Device, especially a kind of energy-saving process method and dress for producing alcohol fuel by distillation process from industrial tail gas fermentation liquid
It sets, can be also used for the rectifying and dehydration of the aqueous solution that other can form low-boiling azeotrope with water.The energy and water
Forming the typical substance of low-boiling azeotrope includes but is not limited to isopropanol, normal propyl alcohol, sec-butyl alcohol, the tert-butyl alcohol, tetrahydrofuran, second
Sour methyl esters, ethyl acetate, pyridine, acetonitrile etc..
By process provided by the invention, each tower typical operation conditions are as follows:
First rectifying column tower top operating pressure range is 8~90kpa；
Second distillation column tower top operating pressure range is 20~280kpa；
Third distillation column tower top operating pressure range is 70~500kpa；
4th the top of the distillation column operating pressure range is 100~1280kpa；
Dewatering unit operating pressure range is 100~1280kpa.
Unless otherwise specified, all pressure refer both to absolute pressure in the present invention.
By process provided by the invention, each tower preferred operations condition are as follows:
First rectifying column tower top operating pressure be 30kpa, 50 DEG C of tower top, 78 DEG C of tower reactor；
Second distillation column tower top operating pressure be 100kpa, 97 DEG C of tower top, 103 DEG C of tower reactor；
Third distillation column tower top operating pressure be 180kpa, 114 DEG C of tower top, 119 DEG C of tower reactor；
4th rectifying tower tower top operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；
Dewatering unit (gas-phase dehydration membrane module) operating pressure is 590kpa.
Industrial tail gas fermentation belongs to gaseous fermentation process, and concentration of alcohol is very low in fermentation liquid (being typically only 2~4%), such as
The energy consumption control of this low-concentration industrial tail gas fermentation liquid distillation process belongs to typical mash alcohol stripping control separation process.
Double prefractionators of CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve to be current cereal crops hair
This rectification technique is such as used for industrial tail gas fermentation by the rectification technique that ferment production alcohol fuel industry generallys use
Liquid distillation process, operation energy consumption are very high.By taking industrial tail gas fermentation liquid concentration of alcohol 3% as an example, mentioned by CN201710542687.5
The tri-columns rectification process method of confession, the steam consumption of alcohol fuel per ton are up to 3.0 tons of steam.
By process provided by the invention, the first thick tower of the first rectifying column lower part, Second distillation column lower part
The second thick tower, third distillation column lower part the thick tower of third form the triple effect of low concentration fermentation liquid, be thermally integrated stripping operation；Institute
The thick tower of the first of the first rectifying column lower part stated, the second thick tower of Second distillation column lower part, the third of third distillation column lower part are thick
Tower, the 5th rectifying column lower part the 5th thick tower form the quadruple effect of low concentration fermentation liquid, be thermally integrated stripping operation；Effectively overcome
The defect of the prior art (double prefractionators, mash economic benefits and social benefits stripping operation) significantly reduces industrial tail gas fermentation liquid production fuel second
The operation energy consumption of alcohol.
Using process provided by the invention, as shown in 1~attached drawing of attached drawing 6, by conventional double prefractionators (double prefractionators, wine with dregs
Liquid economic benefits and social benefits stripping operation) three prefractionators are improved to, it realizes the triple effect of mash, be thermally integrated stripping operation, operation energy consumption is only 2.0 tons
Steam/ton process of alcohol products, operation energy consumption substantially reduce.
Using process provided by the invention, as shown in Fig. 8, by conventional double prefractionators (double prefractionators, mash economic benefits and social benefits vapour
Propose operation) four prefractionators are improved to, it realizes the quadruple effect of mash, be thermally integrated stripping operation, operation energy consumption is only 1.8 tons of steam/tons
Process of alcohol products, operation energy consumption greatly reduce.
The present invention relates to a kind of energy-saving process methods and device from low concentration fermentation liquid production alcohol fuel, more particularly to
A kind of energy-saving process method and device producing alcohol fuel by distillation process from industrial tail gas fermentation liquid.Entire alcohol essence
Evaporate system including at least four towers and the dewatering unit such as first rectifying column, Second distillation column, third distillation column, the 4th rectifying column and
Other corollary equipments composition.It is thermally integrated between first rectifying column, four tower of Second distillation column, third distillation column and the 4th rectifying column,
In addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.The heat-exchange system of optimization keeps dehydration single
Member is organically unified with distillation system, improves the stability and flexibility of entire distillation system.The present invention overcomes
The shortcomings that prior art, the more currently advanced alcohol fuel rectification technique of operation energy consumption reduce by 30% or more, have extremely
Significant practicability and economic benefit, have a extensive future.
Detailed description of the invention
Fig. 1 is provided by the invention a kind of typically from the energy-saving process method stream of low concentration fermentation liquid production alcohol fuel
Cheng Tu；Dewatering unit uses gas-phase dehydration membrane module.
Fig. 2 is a kind of differentiation process of Fig. 1, and the 4th the top of the distillation column shown in FIG. 1 does not produce azeotropic alcohol gas phase
Remove dewatering unit；The liquid phase azeotropic alcohol of the liquid phase azeotropic alcohol of first rectifying column overhead extraction and the extraction of the 4th the top of the distillation column
Together into evaporator E144, the alcohol gas phase after vaporization removes dewatering unit.
Fig. 3 is a kind of differentiation process of Fig. 2, a part of liquid of first rectifying column tower shown in Fig. 2 top side take-off
Phase azeotropic alcohol goes to the 4th the top of the distillation column, and final whole azeotropic alcohol is from the 4th rectifier liquid phase side take-off, then
Into evaporator E144, the alcohol gas phase after vaporization removes dewatering unit.
Fig. 4 is a kind of differentiation process of Fig. 1, the dehydrated alcohol gas phase of dewatering unit output shown in FIG. 1 be changed to
Second distillation column the second reboiler E123 heating；Dewatering unit adsorbs/regenerates handover operation dehydration using molecular sieve.
Fig. 5 is a kind of differentiation process of Fig. 1, when switching produces azeotropic alcohol, deactivates dewatering unit, the first rectifying
Column overhead produces liquid phase and the 4th the top of the distillation column extraction liquid phase together as azeotropic alcohol product.
Fig. 6 is a kind of differentiation process of Fig. 5, when switching produces azeotropic alcohol, first rectifying column tower top side line
It produces a part of azeotropic alcohol and goes to the 4th the top of the distillation column, final whole azeotropic alcohol is adopted from the 4th rectifier liquid phase side line
Out.
Fig. 7 is a kind of differentiation process of Fig. 1, is simplified to the process of Fig. 1, third rectifying is omitted
Tower, the 4th rectifying tower top gaseous phase a part are heated to Second distillation column reboiler E122, and another part removes dewatering unit.Through de-
The dewatered dehydrated alcohol gas phase of water unit is heated to Second distillation column the second reboiler E123.
Fig. 8 is a kind of differentiation process of Fig. 1, further energy saving optimizing has been carried out to the process of Fig. 1, in third
The 5th rectifying column is increased between rectifying column and the 4th rectifying column.4th rectifying tower top gaseous phase a part gives the 5th rectifying column again
Device E162 heating is boiled, another part removes dewatering unit；Through the dewatered dehydrated alcohol gas phase of dewatering unit to the 5th rectifying column the
Two reboiler E163 heating；5th rectifying tower top gaseous phase is heated to third distillation column reboiler E132.
Specific embodiment
Specific embodiments of the present invention be explained in detail with reference to the accompanying drawings it is as follows, but for illustrative purposes only rather than limitation the present invention.
Unless otherwise specified, composition, the structure of the process equipments such as specifically used tower part, material are not specified in embodiment
(connecting pipeline etc. for being connected between each tower part), reagent etc., are commercially available or the ordinary skill of this field
Personnel are obtained with well known method.Related specific experiment method, operating condition, usually according to common process condition and hand
Condition described in volume, or according to the normal condition proposed by manufacturer.
As Figure 1-Figure 8, the present invention provides a kind of energy savers from low concentration fermentation liquid production alcohol fuel:
Including at least first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140
Four towers and connecting pipeline.
The feeding line is connect with the condenser E111 tube-side inlet of first rectifying column T110, E111 tube side outlet with
The feed preheater E113 cold side import of first rectifying column T110 connects, and E113 cold side outlet port is connected to first rectifying column T110's
Middle part.The top gaseous phase outlet of first rectifying column T110 and the condenser E111 shell side gas phase entrance of first rectifying column T110 connect
It connects, the condenser E111 shell side gaseous phase outlet of first rectifying column T110 and the tail cooler E112 shell side gas phase of first rectifying column T110
Entrance connection, the tail cooler E112 shell side gaseous phase outlet of first rectifying column T110 are connected to vacuum system.First rectifying column T110
Condenser E111 and the condensate outlet pipeline of tail cooler E112 of first rectifying column T110 be divided into two, one is connected to first
The overhead reflux mouth of rectifying column T110, another be connected to the 4th rectifying column T140 overhead reflux mouth.E112 condensate outlet pipeline
It is additionally coupled to industrial alcohol extraction pipeline.The tower reactor of first rectifying column T110 respectively with the reboiler E114 of first rectifying column T110
Tube-side inlet is connected with the feed preheater E113 hot side import of first rectifying column T110.The feeding preheating of first rectifying column T110
Device E113 hot side outlet is connected with useless wine with dregs discharge pipe.The reboiler tube side outlet of first rectifying column T110 is connected to the first rectifying
The tower reactor of tower T110.
First rectifying column T110 feeds the above liquid phase side line outlet and is connected to the 4th the first feed preheater of rectifying column T140
E141 cold side input port, first rectifying column T110 feed following liquid phase side line outlet and are connected to Second distillation column T120 feed preheater
E121 cold side input port.
Second distillation column T120 feed preheater cold side outlet port is divided into two, and one is connected to Second distillation column T120 charging
Mouthful, another is connected to third distillation column T130 feed preheater E131 cold side input port.Second distillation column T120 top gaseous phase goes out
Mouth is connect with first rectifying column T110 reboiler E114 shell side gas phase entrance, first rectifying column T110 reboiler E114 shell side lime set
Outlet is connected to the 4th rectifying column T140 the first feed preheater E141 cold side input port.Second distillation column T120 tower reactor is respectively with
Two rectifying column T120 reboiler E122 tube-side inlets are connected with Second distillation column T120 feed preheater E121 hot side import.Second
Rectifying column T120 feed preheater hot side outlet is connected to first rectifying column T110 feed preheater E113 hot side import.Second essence
It evaporates the outlet of tower T120 reboiler tube side and is connected to Second distillation column T120 tower reactor.
Third distillation column T130 feed preheater E131 cold side outlet port is connected to third distillation column T130 feed inlet.Third essence
It evaporates the outlet of tower T130 top gaseous phase to connect with Second distillation column T120 reboiler E122 shell side gas phase entrance, Second distillation column T120
Reboiler E122 shell side condensate outlet is connected to the 4th rectifying column T140 the first feed preheater E141 cold side input port.Third rectifying
Tower T130 tower reactor respectively with third distillation column T130 the first reboiler E132 tube-side inlet, the second reboiler of third distillation column T130
E133 tube-side inlet is connected with third distillation column T130 feed preheater E131 hot side import.Third distillation column T130 feeding preheating
Device hot side outlet is connected to Second distillation column T120 feed preheater E121 hot side import.The first reboiler of third distillation column T130
The outlet of E132 tube side and the outlet of the second reboiler of third distillation column T130 E133 tube side are connected to third distillation column T130 tower reactor.
4th rectifying column T140 the first feed preheater E141 cold side outlet port and the 4th the second feeding preheating of rectifying column T140
Device E142 cold side input port is connected, the 4th rectifying column T140 the second feed preheater E142 cold side outlet port and the 4th rectifying column T140 into
Material mouth is connected.4th rectifying column T140 top gaseous phase outlet respectively with third distillation column T130 the first reboiler E132 shell side gas phase
Entrance, dewatering unit gas phase import are connected.Third distillation column T130 the first reboiler E132 shell side condensate outlet pipeline is connected to
4th rectifying column T140 overhead reflux mouth.
The dehydrated alcohol vapor delivery line of dewatering unit output is connected to third distillation column T130 the second reboiler E133 shell side
Gas phase entrance, the second reboiler of third distillation column T130 E133 shell side condensate outlet are connected with process of alcohol products extraction pipeline.
The light wine pipeline of dewatering unit discharge is connected to first rectifying column T110 and feeds the above light wine feed inlet.
Several fusel oil extraction mouths are respectively set in 4th rectifying column T140 feed entrance point above and below, and fusel oil produces mouth
It is connect respectively with fusel oil extraction pipeline.
4th rectifying column T140 tower reactor respectively with the 4th rectifying tower reboiler E143 tube-side inlet and the 4th rectifying column T140
First feed preheater E141 hot side import is connected.4th rectifying column T140 the first feed preheater E141 hot side outlet and waste water
Discharge pipe connection.The outlet of 4th rectifying column T140 reboiler E143 tube side is connected to the 4th tower bottom of rectifying tower.Heat steam pipe
Line is connected to the 4th rectifying column T140 reboiler E143 shell side gas phase entrance, the 4th rectifying column T140 reboiler E143 shell side lime set
Outlet is connected to the 4th rectifying column T140 the second feed preheater E142 hot side import.4th the second feeding preheating of rectifying column T140
Device E142 hot side outlet is connected with heating vapour-condensing liquid discharge pipe.
A kind of energy-saving process method from low concentration fermentation liquid production alcohol fuel provided by the invention includes the following steps:
1) first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column are included at least
T140；
2) the first rectifying column T110 described in is combination tower, and first rectifying column top is the first rectifying section S1101, and middle part is
Take off light section S1102), lower part is the first thick tower S1103；
3) the Second distillation column T120 described in is stripper, and the following are the second thick tower S1203 for charging；
4) the third distillation column T130 described in) it is stripper, the following are the thick tower S1303 of third for charging；
5) the 4th rectifying column T140 described in is combination tower, and the 4th rectifier is the second rectifying section S1401, and middle part is
Fusel oil produces section S1402, and lower part is dewatering period S1403；
6) first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140 described in
Between to be thermally integrated, the 4th rectifying column T140 top gaseous phase is used as third distillation column T130 tower reactor heat source, for third rectifying
Tower T130 provides institute's calorific requirement；Third distillation column T130 top gaseous phase is the as Second distillation column T120 tower reactor heat source
Two rectifying column T120 provide institute's calorific requirement；Second distillation column T120 top gaseous phase heats heat as first rectifying column T110 tower reactor
Source provides institute's calorific requirement for first rectifying column T110；
7) there are three sections containing wine with dregs in entire rectifier unit system --- under first rectifying column lower part S1103, Second distillation column
Portion S1203 and third distillation column lower part S1303；First rectifying column T110, Second distillation column T120 and third distillation column T130 tower
Kettle discharges waste water containing wine with dregs respectively；The discharge of 4th rectifying column T140 tower reactor is free of wine with dregs waste water.
8) azeotropic alcohol product is by the top first rectifying column T110 or upper part side line and the 4th rectifying T140 top of tower
Or upper part side line obtains respectively；Fusel oil is by liquid phase side take-off in the middle part of the 4th rectifying column T140；
9) the evaporation gas phase of the 4th rectifying column T140 top gaseous phase or azeotropic alcohol liquid phase removes dewatering unit；
10) the dehydrated alcohol gas phase first choice of dewatering unit output is used as third distillation column T130 tower reactor heat source, can also
It is used as Second distillation column T120 tower reactor heat source, it is also possible to do first rectifying column T110 tower reactor heat source, it can also be used to pre-
Hot fermentation mash, it can also be used to preheat first rectifying column T110 charging, it can also be used to Second distillation column T120 charging is preheated, it can also
For preheating third distillation column T130 charging, it can also be used to preheat the 4th rectifying column T140 charging.
Aforementioned dehydrated alcohol vapor condensation object is process of alcohol products.
By process provided by the invention, comprise the concrete steps that:
The advanced first rectifying column condenser E111 tube side of industrial tail gas fermentation liquid 101, by first rectifying column T110 tower top
Logistics 102 is into first rectifying column T110 feed preheater E113 cold side input port after gas phase 104 preheats, by first rectifying column T110 tower
Kettle is discharged the logistics 103 after useless mash 111 preheats and enters the top for taking off light section S1102 in the middle part of first rectifying column T110.First essence
It evaporates tower T110 top gaseous phase 104 and enters first rectifying column T110 condenser E111 shell side, E111 does not coagulate gas phase 105 into the first rectifying
Tower T110 tail cooler E112 shell side, E112 shell-side outlet fixed gas 106 go vacuum system.First rectifying column T110 condenser E111
It is two strands that shell side lime set and the mixed logistics 108 of first rectifying column T110 tail cooler E112 shell side lime set, which are divided to, one 109 reflux
To first rectifying column T110 tower top, another stock 110 enters the 4th rectifying column T140 tower top.First rectifying column T110 tail cooler E112
There are also one 107 conduct industrial alcohol to produce for shell side lime set.Useless mash 111 is discharged through the first rectifying in first rectifying column T110 tower reactor
Rectifier unit is discharged in logistics 112 after tower T110 feed preheater E113 and logistics 102 exchange heat.
First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102
Stream 113.First rectifying column T110 charging is following, takes off extraction liquid phase side-stream between the thick tower S1103 of light section S1102 and first
114.Logistics 114 is after the useless heat exchange of mash 205 is discharged in Second distillation column feed preheater E121 and Second distillation column T120 tower reactor
Logistics 115 to be divided to be two strands, first burst of logistics 201 enters Second distillation column T120；Second burst of logistics 202 through third distillation column into
T130 expects that preheater E131 and third distillation column T130 tower reactor are discharged useless mash 304 and exchange heat, and the logistics 301 after heat exchange enters third
Rectifying column T130.
Second distillation column T120 and first rectifying column T110 are thermally integrated operation, Second distillation column T120 top gaseous phase 203 into
First rectifying column T110 reboiler E114 shell side provides separation institute's calorific requirement for first rectifying column T110.
Third distillation column T130 and Second distillation column T120 are thermally integrated operation, third distillation column T130 top gaseous phase 302 into
Second distillation column reboiler E122 shell side provides separation institute's calorific requirement for Second distillation column T120.
4th rectifying column T140 and third distillation column T130 are thermally integrated operation, the 4th rectifying column T140 tower top one gas phase
404 provide separation required partial heat into third distillation column T130 the first reboiler E132 shell side, to third distillation column T130；The
Four another burst of gas phases of rectifying column T140 tower top, 405 air inlet phase dehydration membrane module M150, dewatered dehydrated alcohol gas phase 407 is into
Three rectifying column T130 the second reboiler E133 shell sides provide separation required another part heat for third distillation column T130.Heating
Steam 430 enters the 4th rectifying column T140 reboiler E143 shell side.
First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102
Stream 113, first rectifying column reboiler E114 shell side lime set 204 and Second distillation column T120 reboiler E122 shell side lime set 303 are mixed
It closes, logistics 401 is discharged useless through the 4th rectifying column T140 the first feed preheater E141 and the 4th rectifying column T140 tower reactor after mixing
Water 411 exchanges heat, and the logistics 402 after heat exchange is again into the 4th rectifying column T140 the second feed preheater E142, with the 4th rectifying column
T140 reboiler E143 shell side steam condensate 431 exchanges heat, and the logistics 403 after heat exchange enters the 4th lower part rectifying column T140 dewatering period
The top of S1403.
First rectifying column T110 condenser E111 shell side lime set and first rectifying column T110 tail cooler E112 shell side lime set are mixed
One lime set 110 and the mixed logistics 413 of the first reboiler of third distillation column T130 E132 shell side lime set 406 after conjunction enter
4th rectifying column T140 tower top.
Useless mash 304 is discharged after third distillation column T130 feed preheater E131 heat exchange in third distillation column T130 tower reactor
Logistics 305 enters Second distillation column T120 feed preheater E121 hot side, Second distillation column T120 feed preheater E121 hot side
Outlet streams 206 enter first rectifying column T110 feed preheater E113 hot side.
The light wine 409 that gas-phase dehydration membrane module M150 is generated enters the first rectifying section S1101 of first rectifying column T110
Third distillation column T130 the second reboiler E133 shell side lime set 408 is process of alcohol products.
Fusel oil extraction section S1402 produces fusel oil 410 in the middle part of 4th rectifying column T140.
The discharge of 4th rectifying column T140 the first feed preheater E141 hot side outlet is free of wine with dregs waste water 412.
4th rectifying column T140 the second feed preheater E142 hot side outlet discharges steam condensate 432.
By process provided by the invention, typical raw material composition are as follows:
Above-mentioned raw materials compositing range does not constitute any limitation of the invention, and the present invention can be used for the fuel second of various compositions
The separation of alcohol fermentation liquid.
Embodiment 1:
As shown in Figure 1, the advanced first rectifying column T110 condenser E111 tube side of industrial tail gas fermentation liquid 101,
Logistics 102 enters into the cold side first rectifying column T110 feed preheater E113 after being preheated by first rectifying column T110 top gaseous phase 104
Mouthful, the logistics 103 after the preheating of mash 111 of being given up by the discharge of first rectifying column T110 tower reactor, which enters in the middle part of first rectifying column T110, to be taken off gently
The top of section S1102.First rectifying column T110 top gaseous phase 104 enters first rectifying column T110 condenser E111 shell side, E111
For not solidifying gas phase 105 into first rectifying column T110 tail cooler E112 shell side, E112 shell-side outlet fixed gas 106 goes vacuum system.The
One rectifying column T110 condenser E111 shell side lime set and the mixed logistics of first rectifying column T110 tail cooler E112 shell side lime set
108 points are two strands, one 109 infinite reflux to first rectifying column T110 tower top, another stock 110 enters the 4th rectifying column T140 tower
Top.There are also one 107 conduct industrial alcohol to produce for first rectifying column T110 tail cooler E112 shell side lime set.First rectifying column T110
Tower reactor is discharged logistics 112 of the useless mash 111 after first rectifying column T110 feed preheater E113 and logistics 102 exchange heat and essence is discharged
Distillation unit.
First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102
Stream 113.First rectifying column T110 charging is following, takes off extraction liquid phase side-stream between the thick tower S1103 of light section S1102 and first
114.Logistics 114 is discharged useless mash 205 with Second distillation column T120 tower reactor through Second distillation column T120 feed preheater E121 and changes
It is two strands that logistics 115 after heat, which is divided to, and first burst of logistics 201 enters Second distillation column T120, and second burst of logistics 202 is through third rectifying
Tower T130 feed preheater E131 and third distillation column T130 tower reactor are discharged useless mash 304 and exchange heat, and the logistics 301 after heat exchange enters
Third distillation column T130.
Second distillation column T120 and first rectifying column T110 are thermally integrated operation, Second distillation column T120 top gaseous phase 203 into
First rectifying column T110 reboiler E114 shell side provides separation institute's calorific requirement for first rectifying column T110.
Third distillation column T130 and Second distillation column T120 are thermally integrated operation, third distillation column T130 top gaseous phase 302 into
Second distillation column T120 reboiler E122 shell side provides separation institute's calorific requirement for Second distillation column T12.
4th rectifying column T140 and third distillation column T130 are thermally integrated operation, the 4th rectifying column T140 tower top one gas phase
404 provide separation required partial heat into third distillation column T130 the first reboiler E132 shell side, to third distillation column T130；The
Four another burst of gas phases of rectifying column T140 tower top, 405 air inlet phase dehydration membrane module M150, dewatered dehydrated alcohol gas phase 407 is into
Three rectifying column T130 the second reboiler E133 shell sides provide separation required another part heat for third distillation column T130.Heating
Steam 430 enters the 4th rectifying column T140 reboiler E143 shell side.
First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102
Stream 113, first rectifying column T110 reboiler E114 shell side lime set 204 and Second distillation column reboiler E122 shell side lime set 303 are mixed
It closes, logistics 401 is discharged useless through the 4th rectifying column T140 the first feed preheater E141 and the 4th rectifying column T140 tower reactor after mixing
Water 411 exchanges heat, and the logistics 402 after heat exchange is again into the 4th rectifying column T140 the second feed preheater E142, with the 4th rectifying column
T140 reboiler E143 shell side steam condensate 431 exchanges heat, and the logistics 403 after heat exchange enters the 4th lower part rectifying column T140 dewatering period
The top of S1403.
First rectifying column T110 condenser E111 shell side lime set and first rectifying column T110 tail cooler E112 shell side lime set are mixed
One lime set 110 and the mixed logistics 413 of the first reboiler of third distillation column T130 E132 shell side lime set 406 after conjunction enter
4th rectifying column T140 tower top.
Useless mash 304 is discharged after third distillation column T130 feed preheater E131 heat exchange in third distillation column T130 tower reactor
Logistics 305 enters Second distillation column T120 feed preheater E121 hot side, Second distillation column T120 feed preheater E121 hot side
Outlet streams 206 enter first rectifying column T110 feed preheater E113 hot side.
The light wine 409 that gas-phase dehydration membrane module M150 is generated enters the first rectifying section S1101 of first rectifying column T110
Third distillation column T130 the second reboiler E133 shell side lime set 408 is process of alcohol products.
Fusel oil extraction section S1402 produces fusel oil 410 in the middle part of 4th rectifying column T140.
The discharge of 4th rectifying column T140 the first feed preheater E141 hot side outlet is free of wine with dregs waste water 412.
4th rectifying column T140 the second feed preheater E142 hot side outlet discharges steam condensate 432.
Following present a kind of typical operation conditions of each tower in embodiment 1, typical operation conditions and operation energy consumption are as follows:
First rectifying column T110 tower top operating pressure be 30kpa, 50 DEG C of tower top, 78 DEG C of tower reactor；
Second distillation column T120 tower top operating pressure be 100kpa, 97 DEG C of tower top, 103 DEG C of tower reactor；
Third distillation column T130 tower top operating pressure be 180kpa, 114 DEG C of tower top, 119 DEG C of tower reactor；
4th rectifying column T140 column overhead operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；
Dewatering unit (gas-phase dehydration membrane module) operating pressure is 590kpa.
By the process that Fig. 1 of the present invention is provided, conventional double prefractionators (double prefractionators, mash economic benefits and social benefits stripping operation) are improved
For three prefractionators --- the thick tower S1103 of the first of the lower part first rectifying column T110, the lower part Second distillation column T120 the second thick tower
S1203, the lower part third distillation column T130 the thick tower S1303 of third, realize the triple effect of mash, be thermally integrated stripping operation.Entire essence
It evaporates system first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140 and forms quadruple effect heat
Integrated operation, the 4th rectifying T140 column overhead gas phase as third distillation column T130 tower reactor the first reboiler E132 heat source,
A part of heat is provided for third distillation column T130, the dehydrated alcohol gas phase of dewatering unit output is as third distillation column T130 tower
Kettle the second reboiler E133 heat source, provides another part heat for third distillation column T130；Third distillation column T130 tower top
Gas phase provides institute's calorific requirement as Second distillation column T120 tower reactor heat source, for Second distillation column T120；Second distillation column
T120 top gaseous phase provides institute's calorific requirement as first rectifying column T110 tower reactor heat source, for first rectifying column T110.Entirely
Only the 4th rectifying column T140 tower bottom reboiler E143 needs middle pressure steam to heat to distillation system, operation energy consumption be only 2.0 tons of steam/
Ton process of alcohol products, operation energy consumption substantially reduce.
By 200,000 tons/year of fuel alcohol plants, 8000 hour/year of operation hour, middle pressure steam consumption is 50 ton/hours.
Other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement.
Add the tri-columns rectification process side of molecular sieve by double prefractionators of Chinese patent CN201710542687.5 offer, double smart towers
Method, distillation system operation energy consumption are 3.0 tons of steam/ton alcohol fuel.By 200,000 tons/year of fuel alcohol plants, operation hours
8000 hours/year, middle pressure steam consumption are 75 ton/hours.
(3.0-2.0)/3.0 ≈ 33%
Double prefractionators of opposite Chinese patent CN201710542687.5 offer, double smart towers add the tri-columns rectification process of molecular sieve
Method, the process energy consumption that Fig. 1 of the present invention is provided reduce about 33%.
75-50=25 ton/hours of steam can be saved per hour.
25 ton/hours × 8000 hour/year=200000 ton/year of middle pressure steam can be saved every year.
It is calculated by 150 yuan of steam per ton, steam expense can be saved every year:
200000 tons/year × 150 yuan/ton ten thousand yuan/year of ÷ 10000=3000.
A kind of energy-saving process method and device from low concentration fermentation liquid production alcohol fuel provided by the invention, has pole
Its significant economic benefit.
Embodiment 2:
As shown in Fig. 2, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
4th rectifying column T140 tower top shown in FIG. 1 does not produce azeotropic alcohol gas phase and removes dewatering unit.First rectifying column
After the liquid phase azeotropic alcohol 110 of T110 overhead extraction and the liquid phase azeotropic alcohol 414 of the 4th rectifying column T140 overhead extraction mix
Logistics 415 into evaporator E144, the alcohol gas phase 405 after vaporization removes dewatering unit.
Embodiment 3:
As shown in figure 3, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is such as
Under:
The top first rectifying column T110 shown in Fig. 2 a part of liquid phase azeotropic alcohol 110 of side take-off removes the 4th rectifying column
T140 tower top, final whole azeotropic alcohol is produced from the 4th rectifying column T140 upper aqueous phase side line 415, then into evaporator
E144, the alcohol gas phase 405 after vaporization remove dewatering unit.
Embodiment 4:
As shown in figure 4, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
Dewatering unit shown in FIG. 1 is changed to be adsorbed/regenerated handover operation dehydration, dewatering unit using molecular sieve T150A/B
The dehydrated alcohol gas phase 407 of output is changed to heat to Second distillation column T120 the second reboiler E123.Dewatering unit generates light
Wine 409 enters the first rectifying section S1101 of first rectifying column T110.Second distillation column T120 the second reboiler E123 shell side lime set
408 be process of alcohol products.
Embodiment 5:
As shown in figure 5, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
When switching produces azeotropic alcohol, dewatering unit, first rectifying column T110 overhead extraction liquid phase 110 and the 4th are deactivated
Rectifying column T140 overhead extraction liquid phase 414 is together as azeotropic alcohol product 415.
Embodiment 6:
As shown in fig. 6, it is a kind of differentiation process of Fig. 5, process difference relatively shown in fig. 5 is such as
Under:
When switching produces azeotropic alcohol, the top first rectifying column T110 a part of azeotropic alcohol 110 of side take-off goes the
Four rectifying column T140 tower tops, final whole azeotropic alcohol are produced from the 4th rectifying column T140 upper aqueous phase side line 415.
Embodiment 7:
As shown in fig. 7, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
The process of Fig. 1 is simplified, third distillation column T130, the 4th rectifying column T140 top gaseous phase is omitted
A part 404 is heated to Second distillation column T120 reboiler E122, and another part 405 removes dewatering unit M150.Through dewatering unit
Dewatered dehydrated alcohol gas phase 407 is heated to Second distillation column T120 the second reboiler E123.
Following present a kind of typical operation conditions of each tower in embodiment 7, typical operation conditions and operation energy consumption are as follows:
First rectifying column T110 tower top operating pressure be 30kpa, 50 DEG C of tower top, 78 DEG C of tower reactor；
Second distillation column T120 tower top operating pressure be 170kpa, 92 DEG C of tower top, 118 DEG C of tower reactor；
4th rectifying column T140 column overhead operating pressure be 570kpa, 129 DEG C of tower top, 158 DEG C of tower reactor；
Dewatering unit (gas-phase dehydration membrane module) operating pressure is 570kpa.
By the process that Fig. 7 of the present invention is provided, entire distillation system only the 4th rectifying column T140 tower bottom reboiler E143
Middle pressure steam is needed to heat, distillation system operation energy consumption is 2.7 tons of steam/ton alcohol fuel.
Embodiment 8:
As shown in figure 8, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
Further energy saving optimizing is carried out to the process of Fig. 1, in third distillation column T130 and the 4th rectifying column T140
Between increase the 5th rectifying column T160.4th rectifying column T140 top gaseous phase a part 404 is boiled again to the 5th rectifying column T160
Device E162 heating, another part 405 remove dewatering unit M150.The 5th is given through the dewatered dehydrated alcohol gas phase 407 of dewatering unit
Rectifying column T160 the second reboiler E163 heating.5th rectifying column T160 top gaseous phase 602 gives third distillation column T130 reboiler
E132 heating.Second distillation column T120 pushes up distillate that is, first rectifying column T110 reboiler E114 shell side lime set 204 goes first
Rectifying column T110 feeds the above position.The charging of 4th rectifying column T140 is to feed the above liquid side from first rectifying column T110
Line discharging 113, third distillation column T130 overhead 303, the 5th rectifying column T160 overhead 603 mixed material.
Following present a kind of typical operation conditions of each tower in embodiment 8, typical operation conditions and operation energy consumption are as follows:
First rectifying column T110 tower top operating pressure be 25kpa, 46 DEG C of tower top, 74 DEG C of tower reactor；
Second distillation column T120 tower top operating pressure be 70kpa, 87 DEG C of tower top, 93 DEG C of tower reactor；
Third distillation column T130 tower top operating pressure be 120kpa, 102 DEG C of tower top, 107 DEG C of tower reactor；
5th rectifying column T160 tower top operating pressure be 195kpa, 116 DEG C of tower top, 121 DEG C of tower reactor；
4th rectifying column T140 tower top operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；
Dewatering unit (gas-phase dehydration membrane module) operating pressure is 590kpa.
By the process that Fig. 8 of the present invention is provided, conventional double prefractionators (double prefractionators, mash economic benefits and social benefits stripping operation) are improved
For four prefractionators --- the thick tower S1103 of the first of the lower part first rectifying column T110, the lower part Second distillation column T120 the second thick tower
S1203, the thick tower S1303 of third of the lower part third distillation column T130, the 5th lower part rectifying column T160 the 5th thick tower S1603 formed
The quadruple effect of low concentration fermentation liquid is thermally integrated stripping operation.Entire distillation system first rectifying column T110, Second distillation column
T120, third distillation column T130, the 5th rectifying column T160 and the 4th rectifying column T140 form five effects and are thermally integrated operation, the 4th rectifying
Tower T140 top gaseous phase provides one as the 5th tower bottom of rectifying tower the first reboiler E162 heat source for the 5th rectifying column T160
The dehydrated alcohol gas phase of partial heat, dewatering unit output heats heat as the 5th rectifying column T160 tower reactor the second reboiler E163
Source provides another part heat for the 5th rectifying column T160；5th rectifying column T160 top gaseous phase is as third distillation column tower reactor
Heat source provides institute's calorific requirement for third distillation column T130；Third distillation column T130 top gaseous phase is as Second distillation column
T120 tower reactor heat source provides institute's calorific requirement for Second distillation column T120；Second distillation column T120 top gaseous phase is as first
Rectifying column T110 tower reactor heat source provides institute's calorific requirement for first rectifying column T110.Only the 4th rectifying column T140 tower bottom is boiled again
Device E143 needs middle pressure steam to heat, and operation energy consumption is only 1.8 tons of steam/ton process of alcohol products, and operation energy consumption substantially reduces.
By 200,000 tons/year of fuel alcohol plants, 8000 hour/year of operation hour, the technique side provided by Fig. 8 of the present invention
Method, middle pressure steam consumption are 45 ton/hours.Other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement.
Double prefractionators of comparison CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve,
Distillation system operation energy consumption is 3.0 tons of steam/ton alcohol fuel, and middle pressure steam consumption is 75 ton/hours:
(3.0-1.8)/3.0=40%
Double prefractionators of opposite CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve, this
The process energy consumption that invention figure 8 provides reduces about 40%.
75-45=30 ton/hours of steam can be saved per hour.
30 ton/hours × 8000 hour/year=240000 ton/year of middle pressure steam can be saved every year.
It is calculated by 150 yuan of steam per ton, steam expense can be saved every year:
240000 tons/year × 150 yuan/ton ten thousand yuan/year of ÷ 10000=3600.
A kind of energy-saving process method and device from low concentration fermentation liquid production alcohol fuel provided by the invention, has pole
Its significant economic benefit.
It is illustrated in conjunction with the embodiments, the method that the personnel of related fields can provide according to the present invention completely carries out
Appropriate change or changes and combinations, to realize the technology.It should be strongly noted that all these by provided by the invention
Process flow carries out similar change or changes and reconfigure, apparent to those skilled in the art, all
It is considered as in spirit of the invention, range and content.
Claims (10)
1. a kind of energy-saving process method from low concentration fermentation liquid production alcohol fuel, it is characterised in that:
1) first rectifying column (T110), Second distillation column (T120), third distillation column (T130) and the 4th rectifying column are included at least
(T140)；
2) first rectifying column (T110) is combination tower, and the first rectifying column top (T110) is the first rectifying section (S1101), and middle part is
It takes off light section (S1102), lower part is the first thick tower (S1103)；
3) Second distillation column (T120) is stripper, and the following are the second thick towers (S1203) for charging；
4) third distillation column (T130) is stripper, and the following are the thick towers of third (S1303) for charging；
5) the 4th rectifying column (T140) is combination tower, and the 4th rectifying column top (T140) is the second rectifying section (S1401), and middle part is
Fusel oil produces section (S1402), and lower part is dewatering period (S1403)；
6) first rectifying column (T110), Second distillation column (T120), third distillation column (T130) and the 4th rectifying column (T140) it
Between to be thermally integrated, the 4th rectifying column (T140) top gaseous phase is used as third distillation column (T130) tower reactor heat source, is that third is smart
It evaporates tower (T130) and institute's calorific requirement is provided；Third distillation column (T130) top gaseous phase heats heat as Second distillation column (T120) tower reactor
Source provides institute's calorific requirement for Second distillation column (T120)；Second distillation column (T120) top gaseous phase is as first rectifying column
(T110) tower reactor heat source provides institute's calorific requirement for first rectifying column (T110)；
7) it goes dewatering unit gas phase first choice from the 4th rectifying column (T140) top gaseous phase, is also possible to the steaming of azeotropic alcohol liquid phase
It gets angry phase, is also possible to other rectifying tower top gaseous phases in distillation system；
8) the dehydrated alcohol gas phase of dewatering unit output is used as third distillation column (T130) tower reactor heat source, is used as the second rectifying
Tower (T120) tower reactor heat source is used as first rectifying column (T110) tower reactor heat source, for preheating fermentation liquid, being used in advance
The charging of hot first rectifying column, for preheat Second distillation column (T120) charging, for preheat third distillation column (T130) charging or
For preheating the charging of the 4th rectifying column (T140)；
The dehydrated alcohol vapor condensation object is process of alcohol products.
2. process described in accordance with the claim 1, it is characterised in that the dewatering unit is molecular sieve water separation tower or infiltration
Vaporization film thoroughly；The light wine of the dewatering unit discharge enters first rectifying column (T110), or is fed into the 4th rectifying column
(T140), Second distillation column (T120) or third distillation column (T130).
3. process described in accordance with the claim 1, it is characterised in that: when being not necessarily to produce alcohol fuel, the dehydration
Unit deactivates, by first rectifying column (T110) top or side take-off partially azeotropic alcohol, by the 4th rectifying column (T140) tower top
Or upper aqueous phase side take-off partially azeotropic alcohol；Or the azeotropic alcohol of first rectifying column (T110) extraction enters the 4th rectifying
Tower (T140) return tank or tower top, alcohol product is all by the 4th rectifying column (T140) tower top or upper aqueous phase side take-off；Or
The azeotropic alcohol of the 4th rectifying column (T140) of person extraction enters first rectifying column (T110) return tank or tower top, and alcohol product is whole
By first rectifying column (T110) tower top or upper aqueous phase side take-off.
4. process described in accordance with the claim 1, it is characterised in that fermentation liquid mode of entrance is selected from:
1) enter first rectifying column (T110), the charging of Second distillation column (T120) is following from first rectifying column (T110) charging
Liquid phase lateral line discharging, the charging of third distillation column (T130) from first rectifying column (T110) feed following liquid phase lateral line discharging or
Following liquid phase lateral line discharging is fed from Second distillation column (T120)；
2) fermentation liquid is divided into three strands, goes first rectifying column (T110), Second distillation column (T120) and third distillation column respectively
(T130)；
3) fermentation liquid enters Second distillation column (T120), and the charging of first rectifying column (T110) comes from Second distillation column (T120)
Following liquid phase lateral line discharging is fed, the charging of third distillation column (T130) feeds following liquid side from first rectifying column (T110)
Line discharging feeds following liquid phase lateral line discharging from Second distillation column (T120)；
4) fermentation liquid enters third distillation column (T130), and the charging of Second distillation column (T120) comes from third distillation column (T130)
Following liquid phase lateral line discharging is fed, the charging of first rectifying column (T110) feeds following liquid side from third distillation column (T130)
Line discharging feeds following liquid phase lateral line discharging from Second distillation column (T120)；The charging of 4th rectifying column (T140) be from
First rectifying column (T110) feeds the above liquid phase lateral line discharging, Second distillation column (T120) top distillate or its charging with liquid phase
Lateral line discharging, third distillation column (T130) overhead or its mixed material for feeding the above liquid phase lateral line discharging；
By preceding method, by Second distillation column top (T120) distillate or its above liquid phase lateral line discharging of charging, third distillation column
(T130) overhead or its above liquid phase lateral line discharging of charging introduce first rectifying column (T110) charging or more respectively or all
Position.
5. process described in accordance with the claim 1, it is characterised in that the tower top of the first rectifying column (T110) operates
Pressure is 8~90kPa；The tower top operating pressure of Second distillation column (T120) is 20~280kPa；Third distillation column (T130)
Tower top operating pressure is 70~500kPa；The tower top operating pressure of 4th rectifying column (T140) is 100~1280kPa；Dehydration is single
Atom operation pressure limit is 100~1280kpa.
6. process described in accordance with the claim 1, it is characterised in that there are three contain wine with dregs in entire rectifier unit system
Section --- the lower part (S1103) first rectifying column (T110), the lower part (S1203) Second distillation column (T120) and third distillation column
(T130) lower part (S1303)；First rectifying column (T110), Second distillation column (T120) and third distillation column (T130) tower reactor difference
Discharge waste water containing wine with dregs；The discharge of 4th rectifying column (T140) tower reactor is free of wine with dregs waste water；
By preceding method, first rectifying column (T110) is stripper, without top fractionation stage；Second distillation column (T120) is compound
Rectifying section is arranged in tower, top；Third distillation column (T130) is combination tower, and rectifying section is arranged in top.
7. process described in accordance with the claim 1, it is characterised in that the third distillation column (T130) deactivates, the 4th essence
Tower (T140) top gaseous phase is evaporated as Second distillation column tower reactor heat source, provides institute's calorific requirement for Second distillation column (T120)；
Or increase the 5th rectifying column (T160), the 5th rectifying column between third distillation column (T130) and the 4th rectifying column (T140)
(T160) with first rectifying column (T110), Second distillation column (T120), third distillation column (T130) and the 4th rectifying column (T140)
Form five effects and be thermally integrated operation, the 4th rectifying column (T140) top gaseous phase as the 5th rectifying column (T160) tower reactor heat source,
Institute's calorific requirement is provided for the 5th rectifying column (T160)；5th rectifying column (T160) top gaseous phase is as third distillation column (T130) tower
Kettle heat source provides institute's calorific requirement for third distillation column (T130)；Third distillation column (T130) top gaseous phase is as the second essence
Tower (T120) tower reactor heat source is evaporated, provides institute's calorific requirement for Second distillation column (T120)；Second distillation column (T120) tower overhead gas
It is mutually used as first rectifying column (T110) tower reactor heat source, provides institute's calorific requirement for first rectifying column (T110)；Dewatering unit produces
Dehydrated alcohol gas phase out is used as the 5th tower bottom of rectifying tower heat source, is used as third distillation column tower reactor heat source, is used as
Two rectifying columns (T120) tower reactor heat source is used as first rectifying column (T110) tower reactor heat source；
By preceding method, Second distillation column (T120) is pushed up into distillate or it feeds the above liquid phase lateral line discharging, third distillation column
(T130) overhead or its feed above liquid phase lateral line discharging, the 5th rectifying column (T160) overhead or its charging with
Liquid phase lateral line discharging introduces first rectifying column (T110) respectively or all and feeds the above position.
8. according to process described in claim 1 or 7, it is characterised in that azeotropic alcohol product first choice is by first rectifying column
(T110) top or upper part side line and the 4th rectifying column (T140) top or upper part side line obtain respectively；Fusel oil by
Liquid phase side take-off in the middle part of 4th rectifying column (T140)；Described first rectifying column (T110), Second distillation column (T120), third
Rectifying column (T130), the 5th rectifying column (T160) and the 4th rectifying column (T140) are all that compound tower structure, each tower top are all arranged
Rectifying section.
9. process described in accordance with the claim 1, it is characterised in that the process of alcohol products is the preheating of following processes,
Include: first rectifying column (T110) extraction azeotropic alcohol preheating, dewatering unit discharge light wine preheating, fermentation liquid preheating,
First rectifying column (T110) feeding preheating, Second distillation column (T120) feeding preheating, third distillation column (T130) feeding preheating,
Four rectifying columns (T140) feeding preheating.
10. a kind of energy saver from low concentration fermentation liquid production alcohol fuel, it is characterised in that: include at least first rectifying column
(T110), Second distillation column (T120), third distillation column (T130) and the 4th rectifying column (T140) and connecting pipeline；
The feeding line is connect with condenser (E111) tube-side inlet of first rectifying column (T110), condenser (E111) pipe
Journey outlet is connect with first rectifying column feed preheater (E113) cold side import, and feed preheater (E113) cold side outlet port is connected to
In the middle part of first rectifying column (T110)；The condenser of the top gaseous phase outlet and first rectifying column (T110) of first rectifying column (T110)
(E111) shell side gas phase entrance connects, condenser (E111) the shell side gaseous phase outlet and first rectifying column of first rectifying column (T110)
(T110) tail cooler (E112) shell side gas phase entrance connection, tail cooler (E112) shell side gas phase of first rectifying column (T110) go out
Mouth is connected to vacuum system；The condenser (E111) of first rectifying column (T110) and the tail cooler of first rectifying column (T110)
(E112) condensate outlet pipeline is divided into two, and one is connected to the overhead reflux mouth of first rectifying column (T110), another company
It is connected to the 4th rectifying column (T140) overhead reflux mouth；Tail cooler (E112) condensate outlet pipeline is additionally coupled to industrial alcohol extraction pipe
Line；The tower reactor of first rectifying column (T110) is smart with reboiler (E114) tube-side inlet of first rectifying column (T110) and first respectively
Feed preheater (E113) hot side import for evaporating tower (T110) is connected；Feed preheater (E113) heat of first rectifying column (T110)
Side outlet is connected with useless wine with dregs discharge pipe；The reboiler tube side outlet of first rectifying column (T110) is connected to first rectifying column
(T110) tower reactor；
The first charging that the above liquid phase side line outlet of the charging of first rectifying column (T110) is connected to the 4th rectifying column (T140) is pre-
Hot device (E141) cold side input port, the following liquid phase side line outlet of the charging of first rectifying column (T110) are connected to Second distillation column
(T120) feed preheater (E121) cold side input port；
The feed preheater cold side outlet port of Second distillation column (T120) is divided into two, and one is connected to Second distillation column (T120)
Feed inlet, another is connected to feed preheater (E131) cold side input port of third distillation column (T130)；Second distillation column
(T120) top gaseous phase outlet is connect with first rectifying column reboiler (E114) shell side gas phase entrance, first rectifying column (T110)
Reboiler (E114) shell side condensate outlet be connected to the 4th the first feed preheater of rectifying column (E141) cold side input port；Second essence
Evaporate the tower reactor of tower (T120) respectively with reboiler (E122) tube-side inlet and Second distillation column of Second distillation column (T120)
(T120) feed preheater (E121) hot side import is connected；The feed preheater hot side outlet of Second distillation column (T120) connects
To feed preheater (E113) hot side import of first rectifying column (T110)；The reboiler tube side of Second distillation column (T120) exports
It is connected to the tower reactor of Second distillation column (T120)；
Feed preheater (E131) cold side outlet port of third distillation column (T130) is connected to the feed inlet of third distillation column (T130)；
The top gaseous phase outlet of third distillation column (T130) and reboiler (E122) the shell side gas phase entrance of Second distillation column (T120) connect
Connect, reboiler (E122) shell side condensate outlet of Second distillation column (T120) is connected to the 4th rectifying column T140) first charging
Preheater (E141) cold side input port；The tower reactor of third distillation column (T130) the first reboiler with third distillation column (T130) respectively
(E132) tower of tube-side inlet, the second reboiler (E133) tube-side inlet of third distillation column (T130) and third rectifying (T130)
Feed preheater (E131) hot side import is connected；The feed preheater hot side outlet of third distillation column (T130) is connected to the second essence
Evaporate feed preheater (E121) hot side import of tower (T120)；The first reboiler (E132) tube side of third distillation column (T130) goes out
The outlet of the second reboiler (E133) tube side of mouth and third distillation column (T130) is connected to the tower reactor of third distillation column (T130)；
The second of the first feed preheater (E141) cold side outlet port of 4th rectifying column (T140) and the 4th rectifying column (T140) into
Expect that preheater (E142) cold side input port is connected, the second feed preheater (E142) cold side outlet port of the 4th rectifying column (T140) and the
The feed inlet of four rectifying columns (T140) is connected；4th rectifying column (T140) top gaseous phase outlet respectively with third distillation column
(T130) the first reboiler (E132) shell side gas phase entrance, dewatering unit gas phase import are connected；Third distillation column (T130)
First reboiler (E132) shell side condensate outlet pipeline is connected to the overhead reflux mouth of the 4th rectifying column (T140)；
The dehydrated alcohol vapor delivery line of dewatering unit output is connected to the second reboiler (E133) shell of third distillation column (T130)
The second reboiler (E133) shell side condensate outlet and the process of alcohol products extraction of journey gas phase entrance, third distillation column (T130) are managed
Line is connected；The light wine pipeline of dewatering unit discharge is connected to the above light wine feed inlet of charging of first rectifying column (T110)；
Several fusel oil extraction mouths are respectively set in the feed entrance point above and below of 4th rectifying column (T140), and fusel oil produces mouth
It is connect respectively with fusel oil extraction pipeline；
The tower reactor of 4th rectifying column (T140) reboiler (E143) tube-side inlet and the 4th with the 4th rectifying column (T140) respectively
The first feed preheater (E141) hot side import of rectifying column (T140) is connected；First feeding preheating of the 4th rectifying column (T140)
Device (E141) hot side outlet is connect with wastewater discharge pipe line；Reboiler (E143) tube side of 4th rectifying column (T140) exports connection
To the tower reactor of the 4th rectifying column (T140)；Heating steam pipe line is connected to reboiler (E143) shell side of the 4th rectifying column (T140)
Gas phase entrance, reboiler (E143) shell side condensate outlet of the 4th rectifying column (T140) are connected to the of the 4th rectifying column (T140)
Two feed preheaters (E142) hot side import；The second feed preheater (E142) hot side outlet of 4th rectifying column (T140) with plus
Hot steam drip pipe line is connected.
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| CN110452092A (en) * | 2019-08-06 | 2019-11-15 | 中海油天津化工研究设计院有限公司 | A kind of method that the coupling of tower film carries out material and is thermally integrated purification alcohol fuel |
| CN115057760A (en) * | 2022-06-08 | 2022-09-16 | 天津市新天进科技开发有限公司 | Process method and device for producing fuel ethanol and high-grade edible alcohol by adopting five-tower heat integration |
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| CN108558602A (en) * | 2018-07-03 | 2018-09-21 | 肥城金塔机械科技有限公司 | Double thick double smart four tower quadruple effect energy-saving distillings production alcohol fuel systems and its application method |
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| CN110452092B (en) * | 2019-08-06 | 2022-11-15 | 中海油天津化工研究设计院有限公司 | Method for refining fuel ethanol by material and heat integration through tower-membrane coupling |
| CN115057760A (en) * | 2022-06-08 | 2022-09-16 | 天津市新天进科技开发有限公司 | Process method and device for producing fuel ethanol and high-grade edible alcohol by adopting five-tower heat integration |
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