CN104341268B - Continuous dehydration method for fuel ethanol - Google Patents
Continuous dehydration method for fuel ethanol Download PDFInfo
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- CN104341268B CN104341268B CN201310345199.7A CN201310345199A CN104341268B CN 104341268 B CN104341268 B CN 104341268B CN 201310345199 A CN201310345199 A CN 201310345199A CN 104341268 B CN104341268 B CN 104341268B
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 149
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000018044 dehydration Effects 0.000 title claims abstract description 14
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 14
- 239000000446 fuel Substances 0.000 title claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 30
- 239000012528 membrane Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 11
- 239000012465 retentate Substances 0.000 claims abstract description 10
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000002131 composite material Substances 0.000 claims abstract description 3
- 229960004756 ethanol Drugs 0.000 claims description 50
- 239000012466 permeate Substances 0.000 claims description 11
- 229960000935 dehydrated alcohol Drugs 0.000 claims description 9
- 238000005204 segregation Methods 0.000 claims description 2
- 230000000740 bleeding effect Effects 0.000 claims 1
- 150000002085 enols Chemical class 0.000 claims 1
- 238000010992 reflux Methods 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000004372 Polyvinyl alcohol Substances 0.000 abstract description 2
- 229920002451 polyvinyl alcohol Polymers 0.000 abstract description 2
- 235000019441 ethanol Nutrition 0.000 abstract 6
- 238000000605 extraction Methods 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 239000000047 product Substances 0.000 description 8
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 6
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 238000010533 azeotropic distillation Methods 0.000 description 3
- 239000001110 calcium chloride Substances 0.000 description 3
- 229910001628 calcium chloride Inorganic materials 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- 235000012255 calcium oxide Nutrition 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 230000001476 alcoholic effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000002595 Solanum tuberosum Nutrition 0.000 description 1
- 244000061456 Solanum tuberosum Species 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- XKJCHHZQLQNZHY-UHFFFAOYSA-N phthalimide Chemical compound C1=CC=C2C(=O)NC(=O)C2=C1 XKJCHHZQLQNZHY-UHFFFAOYSA-N 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- CVHZOJJKTDOEJC-UHFFFAOYSA-N saccharin Chemical compound C1=CC=C2C(=O)NS(=O)(=O)C2=C1 CVHZOJJKTDOEJC-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- 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
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a continuous dehydration method of fuel ethanol; the membrane separation device adopts a polyvinyl alcohol composite membrane, ethanol water solution with the mass fraction of 35-55% is continuously fed into an ethanol rectification tower, the liquid level of a tower kettle is 60%, a tower top condensing system is opened, the temperature of the tower kettle is raised, when reflux occurs, the total reflux lasts for 30min, and after the system is stabilized, a vacuum pump is started, so that the absolute pressure of the permeation side of the membrane separation device is controlled to be less than or equal to 10 KPa; the gaseous material at the top of the ethanol rectification tower enters a gas-liquid separation tank, and enters from an inlet at the retentate side of a membrane separation device after gas-liquid separation, and absolute ethanol is obtained at an outlet at the retentate side; gas at the permeation side enters an ethanol rectifying tower after passing through a vacuum pump; materials at the bottom of the ethanol rectification tower enter from a jacket inlet of the membrane separation device and are discharged from an outlet; the method can obtain the absolute ethyl alcohol with the ethyl alcohol content of 99.5-99.9% (V), and has the advantages of short flow, convenient operation, low energy consumption and no pollution.
Description
Technical field:
The present invention relates to fuel alcohol dewatering technology, couple even with water vapour penetration particularly to a kind of rectification
Continuous separating alcohol and the technique of water.
Background technology
In recent years, in global range, face serious energy crisis, find novel fungible energy source
Become the key of various countries' future source of energy strategy.Among these, alcohol fuel have renewable, efficient,
The features such as low cost, safety, can be directly used as liquid fuel or be used in mixed way with gasoline, reduce
Dependence to non-renewable energy resources oil, thus ensure the safety of domestically produced energy.By to paddy
Thing, potato class and the fermentation of saccharine material, distillation can produce ethanol continuously.But steamed by simple
Evaporate the concentration of alcohol of generation less than 96%(V/V), and as gasoline, the combustion of the effective additive of diesel oil
Ethanol content in material ethanol must be not less than 99.5%(W/W), the method for ethanol dehydration substantially has following
4 kinds:
(1) quick lime method: by quick lime and the alcoholic solution heat altogether of 95%, reflux for a long time, so
Rear distillation.Quick lime and calcium chloride have strong water absorption, generate calcium hydroxide and band knot after water suction
Calcium chloride (the CaCl of brilliant water2·H2O).Moisture in absorbent lime ethanol solution, calcium chloride is inhaled
Receive the moisture in vapour phase, thus reach to remove the effect of moisture in ethanol.Can prepare containing second by this method
Alcohol is up to the ethanol of 99.5%～99.8%.But the yield of dehydrated alcohol is only the 75% of theoretical value,
Labor intensity is big simultaneously, and poor product quality is the most superseded.
(2) molecular sieve dehydration: after being passed through by the ethanol of 96% with 3A type molecular sieve, molecular sieve can be
Water adsorption in ethanol, so that the purity of ethanol is improved.Molecular sieve has extremely strong suction
Attached ability and the adsorptive selectivity of height, good mechanical performance simultaneously, Heat stability is good, but pass
The molecular sieve dehydration technique of system also exists that price is high, regeneration temperature high, energy consumption is relatively big and energy regenerating
The problem that utilization rate is relatively low.
(3) azeotropic distillation: azeotropic distillation is one of conventional chemical separating method, is usually used in perseverance
Boiling thing or the separation of nearly azeotrope.In the case of dehydrated alcohol cannot being produced at ambient pressure, use to
It adds entrainer and carries out rectification, and conventional entrainer has benzene, hexamethylene, pentane, ether etc..
Now entrainer and the ethanol in alcoholic solution, water form new ternary azeotrope, and at this moment ternary is permanent
Boiling-point difference between boiling thing and pure component ethanol or water is relatively big, thus is obtained by rectification relatively easily
The ethanol that purity is the highest.Azeotropic distillation has mechanization degree height, production is stablized, yield is big,
Technology maturation, product purity advantages of higher, be the main method of Industrial Production of Anhydrous Alcohol, but
It is that energy consumption is relatively big, and entrainer can cause environmental pollution the most at that time in production operation.
(4) extracting rectifying: conventional extractant has glycerol, ethylene glycol etc..Second in extractive distillation column
Alcohol vapour ramps up, and solvent is taken away the moisture in ethanol vapor to the counter-current extraction declined, solvent,
Dehydrated alcohol exits at tower top, and discharge at the bottom of tower is the solvent with moisture, can answer after solvent reclamation
With.But solvent reclamation energy consumption is more.
Patent CN201020286456.6 discloses a kind of vapor permeable membrane for producing dehydrated alcohol
Device and ethanol dehydration system, membrane module use poly-phthalimide filter membrane, in its application example by
It is connected with vacuum pump and rectifying column respectively in fluid reservoir, owing to rectifying column is positive pressure operation, it is impossible to real
, there is the shortcoming that ethanol recovery is low in the normal charging to rectifying column of the existing liquid storage pot liquid simultaneously.
Summary of the invention
It is an object of the invention to provide a kind of low energy consumption, free of contamination alcohol fuel continuous dehydration method.
This method uses membrane separation device, has that flow process is short, energy consumption is low, low equipment investment, alcohol production
Low cost and other advantages.
A kind of alcohol fuel continuous dehydration method of the present invention, it is characterised in that membrane separation device
Use composite membrane of polyvinyl alcohol, specifically comprise the following steps that
(1) by mass fraction be 35～55% ethanol water be continuously introduced in Ethanol rectification column, make
Tower reactor liquid level, 60%, opens overhead condenser, heats up tower reactor, when there being backflow, and infinite reflux
30min, after system stability, opens vacuum pump, makes membrane separation device per-meate side absolute pressure control
≤10KPa；
(2) Ethanol rectification column top Gaseous materials enters knockout drum, after gas-liquid separation, by film
Segregation apparatus retentate side entrance enters, and obtains dehydrated alcohol in retentate side outlet；Per-meate side gas warp
After vacuum pump, enter Ethanol rectification column；
(3) Ethanol rectification column bottoms material is entered by the JI of membrane separation device, outlet arrange
Go out；
Described Ethanol rectification column theoretical cam curve is 35～45, tower top operation pressure be 110～
125KPa。
Described vacuum pump uses oil-free dry vacuum pump, this pumping outlet pressure≤10KPa, aerofluxus
Mouth pressure >=125KPa.
Described membrane separation device per-meate side and retentate side are equipped with water-bath chuck.
Beneficial effects of the present invention:
The present invention provides a kind of and utilizes rectification and water vapour penetration coupling continuously separating ethanol and the work of water
Skill, through rectification and membrane separation device, available ethanol content is 99.5%～99.9%(V) nothing
Water-ethanol, Appropriate application system thermal of the present invention, reduce the production cost of alcohol fuel, permissible
Realize steady in a long-term operation, have that flow process is short, easy to operate, energy consumption is low, free of contamination advantage.
Accompanying drawing illustrates:
Fig. 1 is the process chart of the present invention.
1. inlet valve；2. Ethanol rectification column；3 condensers；4. knockout drum；5. overhead extraction valve；
6. membrane separation device；7. vacuum meter；8. heat exchanger；9. ethanol collecting tank；10. product extraction valve；
11. thermometeies；12. reflux inlets；13. vacuum pump outlet valves；14 vacuum pumps；15 vacuum pump imports
Valve；Extraction valve at the bottom of 16. towers；17. tower top pressure tables；18 reboilers；
Detailed description of the invention
Embodiment 1
Open inlet valve 1, the ethanol water that mass fraction is 35% sent in Ethanol rectification column 2,
When tower reactor liquid level reaches 60%, close inlet valve 1, stop charging；Open Ethanol rectification column 2 tower
Top condenser 3, reflux inlet 12, open tower reactor and add thermocurrent, make tower reactor steadily heat up, work as tower top
When producing backflow, infinite reflux 30min, after tower top, bottom temperature, back-flow velocity are stablized, tower top
In backflow, ethanol content is 90.4%, now bottom temperature and pressure be respectively 103.2 DEG C and
125KPa, the temperature of tower top and pressure are respectively 78.5 DEG C and 120KPa；Open vacuum pump outlet valve
13 and vacuum pump inlet valve 15, start vacuum pump 14, start evacuation, stable after, membrance separation fills
Putting 6 per-meate side pressure is 8KPa, and per-meate side gas is entered Ethanol rectification column by top after vacuum pump.
Opening overhead extraction valve 5 and inlet valve 1, inlet amount is 2kg/h, by regulation tower top condensation flow
Amount makes tower top pressure stable at 110Kpa, Ethanol rectification column substrate material after membrane separation device chuck by
Outlet is discharged, and extraction valve 16 at the bottom of adjusting tower makes tower reactor Liquid level 60%, and stable rear membrance separation fills
Putting jacket temperature is 85.2 DEG C, Ethanol rectification column tower top temperature and pressure be respectively 80.1 DEG C and
110KPa, bottom temperature and pressure are respectively 102.5 DEG C and 112Kpa, Ethanol rectification column top gas state
Material enters knockout drum 4, after gas-liquid separation, membrane separation device retentate side entrance enters,
Dehydrated alcohol is obtained in retentate side outlet.Dehydrated alcohol enters ethanol by heat exchanger 8 shell side and collects
Tank 9, dehydrated alcohol is plucked out of by being arranged on the product extraction valve 10 at ethanol collecting tank 9 end.Second
Alcohol rectifying tower top is provided with tower top pressure table 17, is provided with reboiler 18 at the bottom of tower, the chuck of membrane separation device
Being provided with thermometer 11, between vacuum pump inlet valve and membrane separation device per-meate side, pipeline is provided with very
Empty table 7, tower reactor extraction flow is 1.3kg/h, and in tower bottoms, ethanol content is 2.6%, product extraction
Flow is 0.65kg/h, and product is 99.5%(V containing ethanol), ethanol recovery is 94.5%.
Embodiment 2
Open inlet valve 1, the ethanol water that mass fraction is 55% sent in Ethanol rectification column 2,
When tower reactor liquid level reaches 60%, close inlet valve 1, stop charging；Open Ethanol rectification column tower top
Condenser system, opens tower reactor and adds thermocurrent, makes tower reactor steadily heat up, when tower top produces backflow,
Infinite reflux 30min, after tower top, bottom temperature, back-flow velocity are stablized, ethanol in overhead reflux liquid
Content is 92.8%, and now temperature and the pressure of tower reactor is respectively 102.6 DEG C and 124KPa, tower top
Temperature and pressure are respectively 78.9 DEG C and 122KPa；Open valve 13 and 15 before and after vacuum pump, start
Vacuum pump 14 starts evacuation, and after stablizing, membrane separation device per-meate side pressure is 8KPa, per-meate side
Gas is entered Ethanol rectification column by top after vacuum pump.Open overhead extraction valve 5 and charging simultaneously
Valve 1, inlet amount is 2kg/h, and regulation tower top condensate flow makes tower top pressure stable at 112Kpa
Left and right, Ethanol rectification column substrate material is discharged by outlet after membrane separation device chuck, adopts at the bottom of adjusting tower
Going out valve 16 makes tower reactor liquid level about 60%, and stable rear membrane separation device jacket temperature is 87.2 DEG C,
Ethanol rectification column tower top temperature and pressure are respectively 80.3 DEG C and 112Kpa, bottom temperature and pressure divide
Not being 102.8 DEG C and 115KPa, tower reactor extraction flow is 0.92kg/h, and in tower bottoms, ethanol content is
2.8%, product extraction flow is 0.98kg/h, and product is 99.8%(V containing ethanol), ethanol reclaims
Rate is 96.2%.
Claims (5)
1. an alcohol fuel continuous dehydration method, it is characterised in that: membrane separation device uses poly-second
Enol composite membrane, specifically comprises the following steps that
(1) by mass fraction be 35～55% ethanol water be continuously introduced in Ethanol rectification column, make
Tower reactor liquid level, 60%, opens overhead condenser, heats up tower reactor simultaneously, when there being backflow, entirely returns
Stream 30min；After system stability, open vacuum pump, make membrane separation device per-meate side absolute pressure control
At≤10KPa；
(2) Ethanol rectification column top Gaseous materials enters knockout drum, after gas-liquid separation, by film
Segregation apparatus retentate side entrance enters, and obtains dehydrated alcohol in retentate side outlet；Per-meate side gas warp
After vacuum pump, enter Ethanol rectification column；
(3) Ethanol rectification column bottoms material is entered by the JI of membrane separation device, outlet arrange
Go out.
A kind of alcohol fuel continuous dehydration method the most according to claim 1, it is characterised in that
The theoretical cam curve of Ethanol rectification column is 35～45, and tower top operation pressure is 110～125KPa.
A kind of alcohol fuel continuous dehydration method the most according to claim 1, it is characterised in that
Vacuum pump uses oil-free dry vacuum pump.
A kind of alcohol fuel continuous dehydration method the most according to claim 1, it is characterised in that
Membrane separation device per-meate side and retentate side are equipped with water-bath chuck.
A kind of alcohol fuel continuous dehydration method the most according to claim 1, it is characterised in that
Vacuum pump bleeding point pressure≤10KPa, exhaust port pressure >=125KPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310345199.7A CN104341268B (en) | 2013-08-09 | 2013-08-09 | Continuous dehydration method for fuel ethanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310345199.7A CN104341268B (en) | 2013-08-09 | 2013-08-09 | Continuous dehydration method for fuel ethanol |
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| Publication Number | Publication Date |
|---|---|
| CN104341268A CN104341268A (en) | 2015-02-11 |
| CN104341268B true CN104341268B (en) | 2016-08-10 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201310345199.7A Active CN104341268B (en) | 2013-08-09 | 2013-08-09 | Continuous dehydration method for fuel ethanol |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108083979B (en) * | 2017-12-19 | 2024-04-16 | 江苏九天高科技股份有限公司 | Ethanol production method and device |
| CN110483248B (en) * | 2019-08-06 | 2022-08-23 | 中海油天津化工研究设计院有限公司 | Method for refining fuel ethanol by coupling and strengthening three towers and two membranes |
| CN110511115B (en) * | 2019-08-06 | 2022-08-23 | 中海油天津化工研究设计院有限公司 | Method for coupling and strengthening separation of fuel ethanol by rectifying tower and membrane |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4405409A (en) * | 1980-10-06 | 1983-09-20 | Gunter Tusel | Method and apparatus for dehydrating mixtures of organic liquids and water |
| CN101820964A (en) * | 2007-10-12 | 2010-09-01 | Epcon能源处理控制股份公司 | Method for dewatering mixture of mostly ethanol and water |
| CN201744279U (en) * | 2010-08-05 | 2011-02-16 | 安徽丰原生物化学股份有限公司 | Vapour osmotic membrane device and ethanol dehydration system used for producing anhydrous ethyl alcohol |
| CN102180768A (en) * | 2011-03-21 | 2011-09-14 | 安徽丰原生物化学股份有限公司 | Method for preparing anhydrous alcohol |
| CN102260140A (en) * | 2011-04-30 | 2011-11-30 | 白银阳明银光化工有限公司 | New process for producing absolute ethanol by rectification and pervaporation method |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090117631A1 (en) * | 2007-11-02 | 2009-05-07 | Pierre Lucien Cote | Alcohol extraction process for biofuel production |
-
2013
- 2013-08-09 CN CN201310345199.7A patent/CN104341268B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4405409A (en) * | 1980-10-06 | 1983-09-20 | Gunter Tusel | Method and apparatus for dehydrating mixtures of organic liquids and water |
| CN101820964A (en) * | 2007-10-12 | 2010-09-01 | Epcon能源处理控制股份公司 | Method for dewatering mixture of mostly ethanol and water |
| CN201744279U (en) * | 2010-08-05 | 2011-02-16 | 安徽丰原生物化学股份有限公司 | Vapour osmotic membrane device and ethanol dehydration system used for producing anhydrous ethyl alcohol |
| CN102180768A (en) * | 2011-03-21 | 2011-09-14 | 安徽丰原生物化学股份有限公司 | Method for preparing anhydrous alcohol |
| CN102260140A (en) * | 2011-04-30 | 2011-11-30 | 白银阳明银光化工有限公司 | New process for producing absolute ethanol by rectification and pervaporation method |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
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| CN104341268A (en) | 2015-02-11 |
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