CN105037094A - Energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation - Google Patents
Energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation Download PDFInfo
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- C07C67/00—Preparation of carboxylic acid esters
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- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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Abstract
Provided is an energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation. Rough alcohol prepared through an acetic acid ester hydrogenation process is adopted as a raw material, a methyl alcohol product and an ethyl alcohol product with high purity are obtained through rectification of a light component removal tower, a methyl alcohol tower and an ethyl alcohol tower and energy coupling, and meanwhile light components on the tower top of the light component removal tower can return to an acetic ester hydrogenation section to be subjected to a circular reaction to achieve the maximum light component utilization rate. According to energy coupling, under the operating conditions of normal pressure of the light component removal tower, positive pressure of the methyl alcohol tower and negative pressure or normal pressure of the ethyl alcohol tower, gas condensation heat on the tower top of the methyl alcohol tower is utilized for being supplied to tower bottoms of the light component removal tower and tower bottoms of the ethyl alcohol tower for reboiling, meanwhile, the number of adopted cooling media and heating media is reduced, and energy consumption of the device is greatly reduced.
Description
One, technical field
The present invention relates to the method for Energy harvesting in separating technology in a kind of chemical process and sepn process, is Specifically a kind of Energy Coupling rectificating method of acetic ester preparation of ethanol by hydrogenating.
Two, background technology
Ethanol, is commonly called as alcohol, is a kind of colourless and have the volatile liquid of peat-reek under room temperature.Ethanol is inflammable, is conventional fuel, solvent and sterilizing agent; As a kind of important basic chemical industry raw material, it is widely used in the numerous areas such as food, chemical industry, military project, medicine.
Industrial general amylo process or ethylene hydration method ethanol production.In recent years along with the rise of Coal Chemical Industry, coal ethanol enters into the visual field gradually.It is raw material through gasification for synthetic gas or (main component is CO and H with plant gas that coal ethanol refers to coal
2) be raw material, adopt different operational paths to produce the process of ethanol.At present, be that source produces the operational path of ethanol and mainly contains four with coal; See Fig. 2.
From reaction mechanism, direct method path is shorter, but due to its CO low conversion rate, selectivity and the raw material availability of ethanol are lower, are mainly in the experimental study stage at present, rarely have the report of industrial application.Although indirect method path is longer, the transformation efficiency of raw material and the selectivity of ethanol all reach higher level, and the research for catalyzer and reaction process has also reached the stage that large-scale commercial is promoted, and existing large-scale industry device is being built at present.
The advantage of acetic acid direct hydrogenation legal system ethanol is: path is relatively short; Return on investment (ROI) is higher.Inferior position is: mostly adopt noble metal catalyst, and cost is high; Acetic acid raw material reaction transformation efficiency does not reach 100%, requires higher to equipment material; Reaction has water to produce, and separating energy consumption is higher.
Acetic acid esterified hydrogenation legal system ethanolysis determined directed hydrogenation exist subject matter, its advantage is: adopt non-precious metal catalyst, cost is lower; Require lower to equipment material; React anhydrous generation, separating energy consumption is lower.Inferior position is: many step esterifications, reaction process is longer.
Ethanol can rough segmentation be the different stages such as dehydrated alcohol (ethanol massfraction >=99.5%), industrial alcohol (ethanol massfraction >=95%), alcohol fuel (ethanol massfraction >=92.1%), can adopt different separating technologies according to different specifications.
Thick alcohol of the present invention refers under Cu-series catalyst effect ritalin (under be called for short acetic ester) the thick alcohol product that preparation of ethanol by hydrogenating directly obtains, and in this mixture, each component is as follows:
| Material | Ethanol | Methyl alcohol | Acetic ester | All the other trace impurities |
| Massfraction/% | 30～70 | 30～70 | 0.1～10 | Propyl alcohol, water etc. |
Remarks: minor amount of water is bring water in raw material, the anhydrous generation of hydrogenation reaction itself.
Three, summary of the invention
The thick alcohol product that the object of the invention is to directly be obtained by rectification process Dichlorodiphenyl Acetate ester through hydrogenation ethanol is separated, and obtains product methyl alcohol, ethanol on the one hand, reclaims the recycle of light constituent acetic ester on the other hand.Technical problem to be solved is to reduce the energy consumption of device by Energy Coupling.
Rectifying of the present invention is that three tower apparatus be made up of lightness-removing column, methanol column and ethanol tower carry out three-tower rectification, and detailed process is as follows:
First thick alcohol enter lightness-removing column, and after lightness-removing column is separated, top gaseous phase is the mixing steam of acetic ester and methyl alcohol etc.; After condenser of light component removal column condensation, a part of phlegma returns lightness-removing column trim the top of column, and the light constituent of another part based on acetic ester returns upstream acetic ester hydrogenation workshop section, reclaims circulation hydrogenation and utilizes; Tower reactor is ethanol, methanol mixed solution containing minor amount of water, propyl alcohol etc., and pumping enters methanol column and is separated.
The working pressure of lightness-removing column (1) is normal pressure, tower top temperature 55-65 DEG C, bottom temperature 65-75 DEG C, reflux ratio 1-50.
After methanol column is separated, top gaseous phase is methyl alcohol; After methanol column condenser condenses, a part of phlegma returns methanol column trim the top of column, and another part removes product storage tank as methanol product (massfraction >=99.9%) extraction; Tower reactor is the ethanolic soln (massfraction >=98%) containing minor amount of water, propyl alcohol etc., and pumping enters ethanol tower and is separated further.
The working pressure of methanol column (2) is 0.2-0.8MPa, tower top temperature 80-130 DEG C, bottom temperature 100-150 DEG C, reflux ratio 1-30.
After ethanol tower is separated, top gaseous phase is the mixing steam of ethanol (massfraction >=99.5%) and water (massfraction≤0.5%); After ethanol tower condenser condenses, a part of phlegma returns ethanol tower trim the top of column, and another part removes product storage tank as alcohol product extraction; Tower reactor is the heavy constituent solution containing micro-propyl alcohol etc.
The working pressure of ethanol tower (3) is negative pressure or the normal pressure of 0.01-0.09MPa, tower top temperature 40-90 DEG C, bottom temperature 50-100 DEG C, reflux ratio 1-30.
Energy Coupling rectificating method alleged by the present invention is under lightness-removing column normal pressure, methanol column malleation, ethanol tower normal pressure or negative-pressure operation condition, methanol column overhead vapours heat of condensation is utilized to supply the boiling hot again of lightness-removing column and ethanol tower tower bottoms, to realize the Energy Coupling of rectification working process, reduce energy consumption.Concrete grammar is as follows:
Before lightness-removing column is arranged on methanol column, so first, second two reboilers need be arranged in lightness-removing column tower reactor, use the first reboiler during driving, steam heating; Use the second reboiler during normal running, by the heat supply of methanol column overhead gas gas phase, for this reason, the second reboiler forms a loop with between the tower top of methanol column and methanol column condenser.
Between lightness-removing column tower reactor and methanol column tower reactor, arrange interchanger, tower bottoms pumping after interchanger pre-heating temperature elevation of de-light device enters methanol column; Tower bottoms pumping after interchanger heat exchange of methanol column enters ethanol tower.
3rd reboiler is set in methanol column tower reactor, steam heating.
Arrange the 4th reboiler in ethanol tower reactor, the 4th reboiler forms a loop with between the tower top of methanol column and methanol column condenser, by the heat supply of methanol column overhead gas gas phase, realizes heating ethanol tower tower bottoms, thus omits steam heating.
Described reboiler is exactly heat exchanger, can be the heat exchanger that shell and tube or coil tube type etc. are conventional.
Present method adopts de-light, methanol column, ethanol tower three tower combine operations, takes into full account the recycle of light constituent, returns upstream hydrogenation workshop section after the unconverted acetic ester of one way is separated by lightness-removing column.Obtain methanol product (mass parts >=99%) and the alcohol product (mass parts >=99.2%) of higher degree simultaneously.
Present method takes into full account the comprehensive utilization of energy, well achieves the Energy Coupling of methanol column and lightness-removing column and ethanol tower; The recirculated water consumption of ton product ethanol saves at least 200 tons, and steam consumption saves at least 2.5 tons.
Four, accompanying drawing explanation
Fig. 1 is the schematic flow sheet of present method.
In figure: 1. lightness-removing column, 2. methanol column, 3. ethanol tower, 4. condenser of light component removal column, 5. the second reboiler, 6. the first reboiler, 7. methyl alcohol device condenser, 8. the 3rd reboiler, 9. ethanol tower condenser, 10. the 4th reboiler, 11. interchanger, 12. methanol column feeding pumps, 13. ethanol tower feeding pumps.
Fig. 2 is take coal as four process route charts that source produces ethanol.
Five. embodiment
1. three tower apparatus
Lightness-removing column tower top has condenser of light component removal column; Tower reactor is provided with first, second reboiler, the former steam heating, and the latter by the heat supply of methanol column top gas gas phase, and forms a loop with between the tower top of methanol column and methanol column condenser.
Methanol column tower top has methanol column condenser; Tower reactor is provided with the 3rd reboiler, steam heating.Interchanger is provided with between methanol column tower reactor and lightness-removing column tower reactor; Lightness-removing column tower bottoms enters methanol column through interchanger again after methanol column feeding pump, and methanol column tower bottoms enters ethanol tower through interchanger.
Ethanol tower tower top has ethanol tower condenser; Tower reactor is provided with the 4th reboiler, and this reboiler forms a loop with between the tower top of methanol column and methanol column condenser.
2. three-tower rectification
First thick alcohol from upstream acetic acid hydrogenation workshop section enter lightness-removing column, after lightness-removing column is separated, and top gaseous phase
(being mainly methyl alcohol and acetic ester), after condenser of light component removal column condensation, a part of phlegma returns lightness-removing column trim the top of column, and another part returns upstream acetic ester hydrogenation workshop section as light constituent; Tower reactor is coarse ethanol, methanol mixed solution pumping methanol column after interchanger pre-heating temperature elevation is separated.The working pressure of lightness-removing column (1) is normal pressure, tower top temperature 55-65 DEG C, bottom temperature 65-75 DEG C, reflux ratio 1-50.
After methanol column is separated, top gaseous phase is after methanol condenser condensation, and a part of phlegma returns methanol column trim the top of column, and another part removes product storage tank as methanol product extraction; Tower reactor is coarse ethanol solution, is pumped into ethanol tower and is separated further after interchanger heat exchange.
The working pressure of methanol column (2) is 0.2-0.8MPa, tower top temperature 80-130 DEG C, bottom temperature 100-150 DEG C, reflux ratio 1-30.
After ethanol tower is separated, top gaseous phase is after ethanol tower condenser condenses, part phlegma returns ethanol tower trim the top of column, another part removes product storage tank as alcohol product extraction: tower reactor obtains a small amount of heavy constituent solution, main component is propyl alcohol and 2-butanols, output is very little, is interrupted extraction as byproduct.
The working pressure of ethanol tower (3) is negative pressure or the normal pressure of 0.01-0.09MPa, tower top temperature 40-90 DEG C, bottom temperature 50-100 DEG C, reflux ratio 1-30.
3. Energy Coupling
Lightness-removing column arranges two reboilers, uses the first reboiler during driving, adopts steam heating, heats, use the second reboiler during normal running to tower bottoms, adopts the heat supply of methanol column overhead gas gas phase.
Methanol column tower reactor arranges the 3rd reboiler, steam heating, proceeds to heating to tower bottoms.Interchanger is set between methanol column tower reactor and lightness-removing column tower reactor, realizes the heat exchange of lightness-removing column tower bottoms and methanol column tower bottoms.
Ethanol tower tower reactor arranges the 4th reboiler, and forms loop with between the tower top of methanol column and methanol column condenser, adopts the heat supply of methanol column overhead gas gas phase.
Claims (1)
1. the Energy Coupling rectificating method of an acetic ester preparation of ethanol by hydrogenating, it is characterized in that: the thick alcohol prepared with acetic ester hydrogenation technique is for raw material, three towers be made up of lightness-removing column (1), methanol column (2) and ethanol tower (3) carry out three-tower rectification and Energy Coupling, and its concrete steps are as follows:
(1) three-tower rectification
A. first thick alcohol enter lightness-removing column (1) and be separated, and top gaseous phase is the mixing steam of acetic ester and methyl alcohol; After condenser of light component removal column (4) condensation, a part of phlegma backflow, another part returns upstream acetic ester hydrogenation workshop section; Tower bottoms pumping enters methanol column (2) and is separated;
The working pressure of lightness-removing column (1) is normal pressure, tower top temperature 55-65 DEG C, bottom temperature 65-75 DEG C, reflux ratio 1-50;
B., after methanol column (2) is separated, top gaseous phase is methyl alcohol; After methanol column condenser (7) condensation, a part of phlegma backflow, another part removes product storage tank as methanol product extraction; Tower bottoms is pumped into ethanol tower (3) and is separated further;
The working pressure of methanol column (2) is 0.2-0.8MPa, tower top temperature 80-130 DEG C, bottom temperature 100-150 DEG C, reflux ratio 1-30;
C., after ethanol tower (3) is separated, top gaseous phase is ethanol; After ethanol tower condenser (9) condensation, a part of phlegma backflow, another part removes product storage tank as alcohol product extraction; Tower bottoms is interrupted extraction;
The working pressure of ethanol tower (3) is negative pressure or the normal pressure of 0.01-0.09MPa, tower top temperature 40-90 DEG C, bottom temperature 50-100 DEG C, reflux ratio 1-30;
(2) Energy Coupling
Under lightness-removing column (1) normal pressure, methanol column (2) malleation, ethanol tower (3) negative pressure or atmospheric operation condition, utilize methanol column overhead vapours heat of condensation supply lightness-removing column (1) tower bottoms and ethanol tower (3) tower bottoms boiling hot again, concrete grammar is as follows:
Lightness-removing column (1) tower reactor arranges two reboilers (5), (6), uses the first reboiler (6), steam heating during driving; Use the second reboiler (5) by the heat supply of methanol column (2) overhead gas gas phase during normal running, reboiler (5) forms a loop with between the tower top of methanol column and condenser (7);
Interchanger (11) is set between lightness-removing column (1) tower reactor and methanol column (2) tower reactor, the tower bottoms of lightness-removing column (1) enters methanol column (2) after interchanger (11) preheating, and the tower bottoms of methanol column (2) enters ethanol tower (3) after ethanol tower feeding pump (13) and interchanger (11) heat exchange;
Ethanol tower (3) tower reactor arranges the 4th reboiler (10), and reboiler (10) forms a loop with between the tower top of methanol column and condenser (7).
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105693468A (en) * | 2016-03-22 | 2016-06-22 | 凯凌化工(张家港)有限公司 | Post treatment device and post treatment method of ethanol and isopropanol produced by isopropyl acetate hydrogenation method |
| CN106554253A (en) * | 2016-11-08 | 2017-04-05 | 西南化工研究设计院有限公司 | A kind of product separated energy-saving technique of acetate preparation of ethanol by hydrogenating |
| CN106588572A (en) * | 2017-01-23 | 2017-04-26 | 神华集团有限责任公司 | Three-tower differential pressure coupling rectifying system and method separating low-carbon mixed alcohols |
| CN108079610A (en) * | 2018-01-15 | 2018-05-29 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system and its rectificating method |
| CN108299157A (en) * | 2018-01-29 | 2018-07-20 | 安徽皖维高新材料股份有限公司 | A method of preparing ethyl alcohol using calcium carbide stove exhaust |
| CN110498736A (en) * | 2019-09-19 | 2019-11-26 | 天津中科拓新科技有限公司 | A kind of benzyl alcohol adds hydrogen to prepare the process of cyclohexanemethanol |
| CN111423308A (en) * | 2019-01-10 | 2020-07-17 | 惠生工程（中国）有限公司 | Product separation system and separation method for preparing ethanol by methyl acetate hydrogenation |
| CN114478193A (en) * | 2022-01-06 | 2022-05-13 | 北京泽华化学工程有限公司 | Separation method and separation device for preparing ethanol from dimethyl ether |
| CN115707680A (en) * | 2021-08-19 | 2023-02-21 | 北京石油化工工程有限公司 | Progressive separation method and system for preparing ethanol crude product by methyl acetate hydrogenation |
| CN115707679A (en) * | 2021-08-19 | 2023-02-21 | 北京石油化工工程有限公司 | Separation method and system for preparing ethanol crude product by methyl acetate hydrogenation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103387481A (en) * | 2013-08-06 | 2013-11-13 | 上海华谊（集团）公司 | Method for producing ethanol through acetic acid esterification-hydrogenation |
| CN103739443A (en) * | 2014-01-21 | 2014-04-23 | 上海华谊（集团）公司 | Method for cogeneration ethanol and methanol employing synthesis gas and ethyl acetate reaction |
| CN104649862A (en) * | 2015-02-05 | 2015-05-27 | 天津大学 | Method and equipment for producing ethanol product by taking ethyl acetate as raw material |
-
2015
- 2015-08-05 CN CN201510474538.0A patent/CN105037094B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103387481A (en) * | 2013-08-06 | 2013-11-13 | 上海华谊（集团）公司 | Method for producing ethanol through acetic acid esterification-hydrogenation |
| CN103739443A (en) * | 2014-01-21 | 2014-04-23 | 上海华谊（集团）公司 | Method for cogeneration ethanol and methanol employing synthesis gas and ethyl acetate reaction |
| CN104649862A (en) * | 2015-02-05 | 2015-05-27 | 天津大学 | Method and equipment for producing ethanol product by taking ethyl acetate as raw material |
Cited By (18)
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| CN105693468B (en) * | 2016-03-22 | 2017-03-08 | 凯凌化工(张家港)有限公司 | Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol |
| CN105693468A (en) * | 2016-03-22 | 2016-06-22 | 凯凌化工(张家港)有限公司 | Post treatment device and post treatment method of ethanol and isopropanol produced by isopropyl acetate hydrogenation method |
| CN106554253A (en) * | 2016-11-08 | 2017-04-05 | 西南化工研究设计院有限公司 | A kind of product separated energy-saving technique of acetate preparation of ethanol by hydrogenating |
| CN106554253B (en) * | 2016-11-08 | 2019-06-18 | 西南化工研究设计院有限公司 | A kind of product separated energy-saving technique of acetate preparation of ethanol by hydrogenating |
| CN106588572B (en) * | 2017-01-23 | 2023-08-22 | 神华集团有限责任公司 | Three-tower differential pressure coupling rectification system and method for separating low-carbon mixed alcohol |
| CN106588572A (en) * | 2017-01-23 | 2017-04-26 | 神华集团有限责任公司 | Three-tower differential pressure coupling rectifying system and method separating low-carbon mixed alcohols |
| CN108079610A (en) * | 2018-01-15 | 2018-05-29 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system and its rectificating method |
| CN108079610B (en) * | 2018-01-15 | 2024-02-23 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying device and rectifying method thereof |
| CN108299157A (en) * | 2018-01-29 | 2018-07-20 | 安徽皖维高新材料股份有限公司 | A method of preparing ethyl alcohol using calcium carbide stove exhaust |
| CN111423308A (en) * | 2019-01-10 | 2020-07-17 | 惠生工程（中国）有限公司 | Product separation system and separation method for preparing ethanol by methyl acetate hydrogenation |
| CN111423308B (en) * | 2019-01-10 | 2023-03-28 | 惠生工程（中国）有限公司 | Product separation system and separation method for preparing ethanol by methyl acetate hydrogenation |
| CN110498736A (en) * | 2019-09-19 | 2019-11-26 | 天津中科拓新科技有限公司 | A kind of benzyl alcohol adds hydrogen to prepare the process of cyclohexanemethanol |
| CN115707680A (en) * | 2021-08-19 | 2023-02-21 | 北京石油化工工程有限公司 | Progressive separation method and system for preparing ethanol crude product by methyl acetate hydrogenation |
| CN115707679A (en) * | 2021-08-19 | 2023-02-21 | 北京石油化工工程有限公司 | Separation method and system for preparing ethanol crude product by methyl acetate hydrogenation |
| CN115707679B (en) * | 2021-08-19 | 2024-01-05 | 北京石油化工工程有限公司 | Separation method and system for preparing crude product of ethanol by methyl acetate hydrogenation |
| CN115707680B (en) * | 2021-08-19 | 2024-01-30 | 北京石油化工工程有限公司 | Progressive separation method and system for preparing crude product of ethanol by methyl acetate hydrogenation |
| CN114478193A (en) * | 2022-01-06 | 2022-05-13 | 北京泽华化学工程有限公司 | Separation method and separation device for preparing ethanol from dimethyl ether |
| CN114478193B (en) * | 2022-01-06 | 2024-04-30 | 北京泽华化学工程有限公司 | Separation method and separation device for preparing ethanol from dimethyl ether |
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