CN101525272B - Ethanol distillation dehydration energy saving technique and device - Google Patents
Ethanol distillation dehydration energy saving technique and device Download PDFInfo
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- CN101525272B CN101525272B CN2009100683977A CN200910068397A CN101525272B CN 101525272 B CN101525272 B CN 101525272B CN 2009100683977 A CN2009100683977 A CN 2009100683977A CN 200910068397 A CN200910068397 A CN 200910068397A CN 101525272 B CN101525272 B CN 101525272B
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Abstract
The invention relates to an ethanol distillation dehydration energy saving technique and a device thereof, the technical proposal of which is that (a) part of gas phase at the tower top of an ethanol rectifying tower is condensed; (b) part of condensed gas phase enters into a compressor to be pressured; (c) the compressed gas phase directly enters into an adsorption unit. Overhead gas phase obtained after ethanol raw material passes through the ethanol rectifying tower enters into a partial condenser, the obtained mixing material enters into a reflux storage tank; wherein, liquid phase material as circulating liquor returns to the ethanol rectifying tower, the gas phase material enters into the compressor, and then enters into the adsorption unit after being pressured, after absorption, the needed high concentration ethanoal product is obtained. The invention can effectively reduce heat exhaustion in the production course of high concentration ethanol and the condensation loading of the tower top of the rectifying tower, reduces the manufacturing cost of the ethanol and has good application prospect.
Description
Technical field
The present invention relates to ethanol distillation dehydration energy saving technique and equipment, the high concentration ethanol of production can be used as industrial chemicals, anhydrous solvent or be used for producing alcohol fuel etc.
Background technology
Ethanol can be divided into fermenting alcohol and synthesizing alcohol by the mode of production, world's ethanol production 93% by fermentative Production.Its raw material sources very extensively mainly comprise cereal materials (corn, wheat, Chinese sorghum, paddy rice), potato raw material (sweet potato, cassava, yam), saccharine material (sugarcane, beet, molasses) and cellulosic material.Biomass obtain ethanol volume(tric)fraction content and are 5%～30% fermentation liquid after fermentation, can obtain the absolute ethyl alcohol product after fermentation liquid rectifying and the dehydration.
Absolute ethyl alcohol is widely used in Chemical Manufacture raw material, organic solvent and railroad fuel etc., wherein claims alcohol fuel again as the absolute ethyl alcohol of railroad fuel.The external interdependency of China's energy constantly increases at present, and the energy security problem becomes increasingly conspicuous; The problem of environmental pollution of China has seriously restricted fast development of national economy; China's agriculture, rural areas and farmers problem is outstanding.It is significant to addressing the above problem to greatly develop the fuel ethanol production technology.
Alcohol fuel is divided into two kinds, and the one, add volume(tric)fraction in the absolute ethyl alcohol and be about 5% denaturing agent (being generally white gasoline or other unleaded hydro carbons) and obtain alcohol fuel, can directly replace fossil oil to become railroad fuel; The 2nd, the absolute ethyl alcohol that in gasoline or diesel oil, adds certain proportion (5%～20%) is processed gasohol or Diesel alcohol.Because the alcoholic acid ignition properties is relatively poor, the ethanol water-content must not be higher than 0.5% (and various ester classes, aldehydes and fusel wet goods foreign matter content are not had particular requirement) when being used for fuel, so must use the absolute ethyl alcohol after the processed to produce alcohol fuel.
In traditional high concentration ethanol technological process of production, the ethanol dehydration process is what to separate with the ethanol rectifying, and concrete technical process is as shown in Figure 1.The cat head gas phase 5 that obtains behind the ethanol raw material 1 process ethanol rectifying tower 2 gets into condensing surfaces 15; The liquid phase material that condensation obtains gets into backflow storage tank 7; The center divides liquid phase material to return ethanol rectifying tower 2 as phegma 8; Remaining liquid phase 13 gets into revaporizer 14, and gas phase 16 backs get into absorbing unit 11 behind the revaporization, obtain the high concentration ethanol product 12 that needs after the absorption.In this flow process after rectifying; Condensation obtains volume ratio is formed (the ethanol volume ratio is 97.6%) near the ethanol-water azeotropic thing liquid aqueous ethanol; This liquid aqueous ethanol is before getting into absorbing unit; Need flash to gaseous state and forced feed once more, this can cause the waste of great amount of heat energy undoubtedly.
Energy-saving and cost-reducing is the effective way that high concentration ethanol manufacturing enterprise reduces product cost, and the exploitation of the energy-saving high concentration ethanol technological process of production receives increasing concern.The present invention has just proposed a kind of ethanol distillation, dewatering process and equipment from energy-saving and cost-reducing angle.
Summary of the invention
The present invention has provided a novel ethanol distillation dehydration production technique and an equipment, can effectively reduce the process energy consumption, practices thrift the high concentration ethanol production cost, has huge economic benefit and social benefit.
A kind of ethanol distillation dehydration production technique of the present invention, technical scheme is:
A) ethanol rectifying tower cat head gas phase adopts partial condensation;
B) gas phase after the partial condensation gets into compressor and realizes pressurization;
C) gas phase after the compression directly gets into absorbing unit.
Can adopt the plurality of devices design to realize process method of the present invention with being connected.
The present invention provides a kind of equipment of realizing the ethanol distillation dehydration production technique, comprises ethanol rectifying tower, fractional distillating tube, backflow storage tank, reboiler, compressor and absorbing unit; Wherein: rectifying tower overhead gas phase materials pipe coupling is to the fractional distillating tube inlet, and fractional distillating tube outlet material pipe coupling is to the storage tank import, and the materail tube of storage tank gaseous phase outlet is connected to compressor inlet, and compressor outlet is connected to the absorbing unit import; Backflow storage tank liquid phase material returns the ethanol rectifying tower as phegma.
As shown in Figure 2; The cat head gas phase 5 entering part condensing surfaces 6 that obtain behind the ethanol raw material 1 process ethanol rectifying tower 2; The mixture that obtains gets into backflow storage tank 7, and liquid phase material wherein returns ethanol rectifying tower 2 as phegma 8, and gaseous phase materials 9 gets into compressor 10; Get into absorbing unit 11 through the pressurization back, obtain the high concentration ethanol product 12 that needs after the absorption.
Distinctive feature of the present invention is: ethanol cat head gas phase is only carried out partial condensation after getting into condensing surface, and the gas phase after the partial condensation gets into the molecular sieve adsorption unit after compressor compresses, and liquid phase is returned rectifying tower as phegma.So just avoided evaporating the thermal waste of being brought after the condensation of aqueous ethanol steam elder generation in the traditional technology,, therefore also reduced the condensation load of rectifying tower overhead condenser simultaneously because the rectifying tower overhead vapours only carries out partial condensation.
In the described technology, the effect of compressor is the condensed gas phase of compression section, and its pressure is raise, and satisfies the gaseous phase materials conditional request that gets into the absorbing unit needs, and it is 100～700kPa that the processing condition of compressor outlet reach absolute pressure.
The present invention can effectively reduce heat energy consumption and the condensation load of rectifying tower cat head in the high concentration ethanol production process, reduces the alcoholic acid production cost, has a good application prospect.
Description of drawings
Fig. 1 is conventional ethanol distillation dehydration process flow diagram;
Fig. 2 is the ethanol distillation dehydration energy saving technique schematic flow sheet;
Among the figure, 1. raw material, 2. ethanol rectifying tower, 3. reboiler, 4. discharging at the bottom of the tower, 5. cat head gas phase; 6. fractional distillating tube, 7. backflow storage tank, 8. phegma, 9. gas phase, 10. compressor, 11. absorbing units; 12. high concentration ethanol, 13. liquid phases, 14. revaporizers, 15. condensing surfaces, gas phase behind 16. revaporization.
Embodiment
Below in conjunction with accompanying drawing technology and equipment provided by the present invention is further explained.
The present invention realizes through following technical scheme:
As shown in Figure 2; The cat head gas phase 5 entering part condensing surfaces 6 that obtain behind the ethanol raw material 1 process ethanol rectifying tower 2; The mixture that obtains gets into backflow storage tank 7, and liquid phase material wherein returns ethanol rectifying tower 2 as phegma 8, and gaseous phase materials 9 gets into compressor 10; Get into absorbing unit 11 through the pressurization back, obtain the high concentration ethanol product 12 that needs after the absorption.
Technology and equipment of the present invention can be applicable to the high concentration ethanol production process, in order to explain that better the present invention in the advantage aspect saving energy and reduce the cost, chooses an application example and explains, but therefore do not limit the scope of application of present technique and equipment.
With ethanol content is that 5～50% liquid stock gets into the ethanol rectifying tower; Tower top pressure 130kPa; Temperature is 98.2 ℃, and rectifying tower cat head vapour phase is for forming the aqueous ethanol steam of (the ethanol volume ratio is 97.6%) near the ethanol-water azeotropic thing, and this steam is after condensing surface 2 carries out partial condensation; Liquid phase is returned rectifying tower as phegma, and gas phase gets into compressor.
Aqueous ethanol steam is after compressor compresses, and pressure is brought up to 200kPa, and temperature is 150 ℃, gets into the molecular sieve adsorption unit afterwards, is the absolute ethyl alcohol more than 99.5% through obtaining the ethanol volume ratio behind the adsorption dewatering.
For the advantage of explanation the present invention aspect energy-conservation, flow process according to the invention and existing single tower separation process are compared, mainly energy expenditure is seen table 1.
Energy consumption relatively in table 1 technology
In the ethanol dehydration process, to remove outside reboiler energy consumes, main energy consumption concentrates on phlegma once more in the evaporative process, can see from calculation result, and embodiment needs only is that the power consumption of compressor is 0.1523 * 10
6KJ/hr, it is 3.5432 * 10 that Comparative Examples then needs heat exhaustion
6KJ/h, the embodiment total energy consumption of comparing with Comparative Examples has reduced by 14.94%, cuts down the consumption of general facilities in the alcohol production operating process significantly, has really realized energy saving purposes.
Ethanol distillation dehydration energy saving technique and equipment that the present invention proposes; Be described through preferred embodiment; Person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to structure as herein described with technological method is changed or suitably change and combination, realize the present invention's technology.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as and are included in spirit of the present invention, scope and the content.
Claims (1)
1. ethanol distillation dehydration production technique is characterized in that: ethanol cat head gas phase is only carried out partial condensation after getting into condensing surface, and the gas phase after the partial condensation gets into the molecular sieve adsorption unit after compressor compresses, and liquid phase is returned rectifying tower as phegma; The absolute pressure of compressor outlet is 100～700kPa.
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| CN2009100683977A CN101525272B (en) | 2009-04-07 | 2009-04-07 | Ethanol distillation dehydration energy saving technique and device |
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| CN2009100683977A CN101525272B (en) | 2009-04-07 | 2009-04-07 | Ethanol distillation dehydration energy saving technique and device |
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| CN101525272B true CN101525272B (en) | 2012-05-30 |
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| US8541633B2 (en) | 2010-02-02 | 2013-09-24 | Celanese International Corporation | Processes for producing anhydrous ethanol compositions |
| CN103566613A (en) * | 2012-08-06 | 2014-02-12 | 南通醋酸纤维有限公司 | Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump |
| US8653308B2 (en) | 2010-02-02 | 2014-02-18 | Celanese International Corporation | Process for utilizing a water stream in a hydrolysis reaction to form ethanol |
| US8680342B2 (en) | 2010-05-07 | 2014-03-25 | Celanese International Corporation | Process for recovering alcohol produced by hydrogenating an acetic acid feed stream comprising water |
| US8704012B2 (en) | 2011-06-16 | 2014-04-22 | Celanese International Corporation | Distillation of crude alcohol product using entrainer |
| US8748675B2 (en) | 2011-06-16 | 2014-06-10 | Celanese International Corporation | Extractive distillation of crude alcohol product |
| US8747492B2 (en) | 2010-02-02 | 2014-06-10 | Celanese International Corporation | Ethanol/fuel blends for use as motor fuels |
| US8747493B2 (en) | 2010-02-02 | 2014-06-10 | Celanese International Corporation | Ethanol compositions |
| US8748673B2 (en) | 2011-11-18 | 2014-06-10 | Celanese International Corporation | Process of recovery of ethanol from hydrogenolysis process |
| US8802901B2 (en) | 2011-11-18 | 2014-08-12 | Celanese International Corporation | Continuous ethyl acetate production and hydrogenolysis thereof |
| US8829251B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Liquid esterification method to produce ester feed for hydrogenolysis |
| US8829249B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Integrated esterification and hydrogenolysis process for producing ethanol |
| US8853470B2 (en) | 2011-11-22 | 2014-10-07 | Celanese International Corporation | Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis |
| US8853468B2 (en) | 2011-11-18 | 2014-10-07 | Celanese International Corporation | Vapor esterification method to produce ester feed for hydrogenolysis |
| US8859827B2 (en) | 2011-11-18 | 2014-10-14 | Celanese International Corporation | Esterifying acetic acid to produce ester feed for hydrogenolysis |
| US8865609B2 (en) | 2012-01-06 | 2014-10-21 | Celanese International Corporation | Hydrogenation catalysts |
| US8907142B2 (en) | 2011-12-29 | 2014-12-09 | Celanese International Corporation | Process for promoting catalyst activity for ethyl acetate conversion |
| US8926718B2 (en) | 2013-03-15 | 2015-01-06 | Celanese International Corporation | Thermochemically produced ethanol compositions |
| US8975451B2 (en) | 2013-03-15 | 2015-03-10 | Celanese International Corporation | Single phase ester feed for hydrogenolysis |
| US9024086B2 (en) | 2012-01-06 | 2015-05-05 | Celanese International Corporation | Hydrogenation catalysts with acidic sites |
| US9024089B2 (en) | 2011-11-18 | 2015-05-05 | Celanese International Corporation | Esterification process using extractive separation to produce feed for hydrogenolysis |
| US9029614B2 (en) | 2011-12-14 | 2015-05-12 | Celanese International Corporation | Phasing reactor product from hydrogenating acetic acid into ethyl acetate feed to produce ethanol |
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| US8907139B2 (en) | 2011-12-28 | 2014-12-09 | Celanese International Corporation | Process for acetal removal in the purification of a crude ethanol product |
| CN103318859B (en) * | 2012-03-22 | 2015-05-13 | 中国石油化工集团公司 | Rectification dehydration tower and dehydration method for nitrogen dioxide |
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| US8541633B2 (en) | 2010-02-02 | 2013-09-24 | Celanese International Corporation | Processes for producing anhydrous ethanol compositions |
| US9447005B2 (en) | 2010-02-02 | 2016-09-20 | Celanese International Corporation | Processes for producing anhydrous ethanol compositions |
| US8653308B2 (en) | 2010-02-02 | 2014-02-18 | Celanese International Corporation | Process for utilizing a water stream in a hydrolysis reaction to form ethanol |
| US8747492B2 (en) | 2010-02-02 | 2014-06-10 | Celanese International Corporation | Ethanol/fuel blends for use as motor fuels |
| US8747493B2 (en) | 2010-02-02 | 2014-06-10 | Celanese International Corporation | Ethanol compositions |
| US8680342B2 (en) | 2010-05-07 | 2014-03-25 | Celanese International Corporation | Process for recovering alcohol produced by hydrogenating an acetic acid feed stream comprising water |
| US8704012B2 (en) | 2011-06-16 | 2014-04-22 | Celanese International Corporation | Distillation of crude alcohol product using entrainer |
| US8748675B2 (en) | 2011-06-16 | 2014-06-10 | Celanese International Corporation | Extractive distillation of crude alcohol product |
| US9000235B2 (en) | 2011-06-16 | 2015-04-07 | Celanese International Corporation | Extractive distillation of crude alcohol product |
| US8859827B2 (en) | 2011-11-18 | 2014-10-14 | Celanese International Corporation | Esterifying acetic acid to produce ester feed for hydrogenolysis |
| US9024089B2 (en) | 2011-11-18 | 2015-05-05 | Celanese International Corporation | Esterification process using extractive separation to produce feed for hydrogenolysis |
| US8829249B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Integrated esterification and hydrogenolysis process for producing ethanol |
| US8829251B2 (en) | 2011-11-18 | 2014-09-09 | Celanese International Corporation | Liquid esterification method to produce ester feed for hydrogenolysis |
| US8853468B2 (en) | 2011-11-18 | 2014-10-07 | Celanese International Corporation | Vapor esterification method to produce ester feed for hydrogenolysis |
| US8802901B2 (en) | 2011-11-18 | 2014-08-12 | Celanese International Corporation | Continuous ethyl acetate production and hydrogenolysis thereof |
| US8748673B2 (en) | 2011-11-18 | 2014-06-10 | Celanese International Corporation | Process of recovery of ethanol from hydrogenolysis process |
| US8853470B2 (en) | 2011-11-22 | 2014-10-07 | Celanese International Corporation | Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis |
| US9029614B2 (en) | 2011-12-14 | 2015-05-12 | Celanese International Corporation | Phasing reactor product from hydrogenating acetic acid into ethyl acetate feed to produce ethanol |
| US8907142B2 (en) | 2011-12-29 | 2014-12-09 | Celanese International Corporation | Process for promoting catalyst activity for ethyl acetate conversion |
| US8975200B2 (en) | 2012-01-06 | 2015-03-10 | Celanese International Corporation | Hydrogenation catalysts with cobalt-modified supports |
| US8865609B2 (en) | 2012-01-06 | 2014-10-21 | Celanese International Corporation | Hydrogenation catalysts |
| US9024086B2 (en) | 2012-01-06 | 2015-05-05 | Celanese International Corporation | Hydrogenation catalysts with acidic sites |
| US9308523B2 (en) | 2012-01-06 | 2016-04-12 | Celanese International Corporation | Hydrogenation catalysts with cobalt-modified supports |
| US9381500B2 (en) | 2012-01-06 | 2016-07-05 | Celanese International Corporation | Process for producing ethanol using hydrogenation catalysts |
| CN103566613B (en) * | 2012-08-06 | 2016-03-30 | 南通醋酸纤维有限公司 | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique |
| CN103566613A (en) * | 2012-08-06 | 2014-02-12 | 南通醋酸纤维有限公司 | Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump |
| US8926718B2 (en) | 2013-03-15 | 2015-01-06 | Celanese International Corporation | Thermochemically produced ethanol compositions |
| US8975451B2 (en) | 2013-03-15 | 2015-03-10 | Celanese International Corporation | Single phase ester feed for hydrogenolysis |
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