CN106008155A - Integrated device and method for preparing ethanol from acetic acid and ethyl acetate through hydrogenation reaction - Google Patents
Integrated device and method for preparing ethanol from acetic acid and ethyl acetate through hydrogenation reaction Download PDFInfo
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- CN106008155A CN106008155A CN201610456928.XA CN201610456928A CN106008155A CN 106008155 A CN106008155 A CN 106008155A CN 201610456928 A CN201610456928 A CN 201610456928A CN 106008155 A CN106008155 A CN 106008155A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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Abstract
The invention discloses an integrated device and a method for preparing ethanol from acetic acid and ethyl acetate through hydrogenation reaction. The device comprises a raw material gas compressor, a recycle gas compressor, a heat exchanger, an acetic acid storage tank, an ethyl acetate storage tank, a raw material pump, a raw material preheater, a vaporization device, an evaporation separator, a reaction device, a water cooler, a high-pressure separator, a low-pressure separator, a flare header pipe, a crude ethanol preheater and a purification device. The production technology for preparing ethanol from acetic acid and ethyl acetate is realized through hydrogenation in the same device by switching connection relations, the operation is convenient, the energy consumption is low, and investment cost and production cost are saved; the raw material conversion rate is 99% or higher, the ethanol selectivity is 98.9% or higher, and ethanol with high purity is produced by the whole device through regulation of technological parameters such as pressure, temperature, hydrogen-acid ratio and the like.
Description
Technical field
The present invention relates to the apparatus and method of a kind of ethanol processed, be specifically related to a kind of acetic acid, ethyl acetate hydrogenation reaction integration system
The device and method of ethanol.
Background technology
Ethanol is important solvent and industrial chemicals, the pollution-free vehicle fuel being well recognized as and additive thereof, and in recent years, China exists
Multiple provinces implement the popularization of ethanol petrol.The industrial process of ethanol is based on grain fermentation method, grain fermentation method
Often producing one ton of ethanol to need to consume 3.2 tons of Semen Maydiss, in order to solve " striving ground with grain " problem, China halted grain in 2007
Ethanol project examination.Additionally, produce at present alcohol industry or China's environmental emission organic pollution is the highest, environmental pollution is serious
An industry, the pollution of alcohol waste water is one of the most serious polluter of food and fermentation industries.China is populous, ploughs
Area is not enough, and China's oil resource lacks relatively simultaneously, and coal resources are abundanter, therefore studies and studies from coal resources
New ethanol route, both can solve grain, can solve again environmental issue, it may be said that be to have politics, economy, ring
Protect triple meaning.Current domestic coal ethanol technology mainly has three kinds of process routes, and after coal gasification, direct reaction prepares ethanol；Coal
Ethanol is prepared through acetic acid direct reaction after gasification；After coal gasification, reaction obtains acetic acid, and after acetic acid esterified, further Hydrogenation obtains ethanol.
It it is the primary study object of current industrialization ethanol both rear.
Patent CN102757308B discloses a kind of method of high purity ethanol, describes acetic acid and hydrogen reaction generates ethanol
And by-product, there is acetic acid conversion low, repeatedly rectification removing light component, acetic acid, ethyl acetate just can obtain second alcohol and water
Mixture, purifying plant flow process is complex, and steam consumption is big, causes the operating cost purified higher with capital cost.
Patent CN102718627A discloses the process of a kind of ethyl ester preparation of ethanol by hydrogenating, and this method ethyl acetate is in internal system
A large amount of recycle, ethyl acetate raw material can only gasifying section, ethyl acetate conversion ratio is the highest, and acetic acid is more difficult to than ethyl acetate
Gasification, so this technique is not applied for acetic acid and is gasified totally hydrogenation reaction.
Patent CN201320068681 discloses the purifying plant of a kind of acetic acid gas phase hydrogenation ethanol, solves existing ethanol and carries
Pure device flow process is complex, and steam consumption is big, causes the operating cost purified and invests the highest problem.
Patent CN201210081309 discloses a kind of acetic acid evaporation and gas conglomerate integration device, solves existing acetic acid hydrogenation
Acetum is flashed to acetic acid steam by ethanol processed not only needs higher evaporating temperature, in addition it is also necessary to bulky vaporization dress
Put, simultaneously in order to make acetic acid steam and unstrpped gas be sufficiently mixed uniformly, it is also desirable to the problem of bulky blender.
At present, the overwhelming majority having been reported that is only to realize acetic acid hydrogenation or the single device of ethyl acetate preparation of ethanol by hydrogenating and technique,
Apply same device and technique to solve acetic acid, ethyl acetate is gasified totally preparation of ethanol by hydrogenating, and purify simple in construction, easy to operate,
Steam consumption is low, and the report that feed stock conversion is high, selectivity is good is the most visible.
Summary of the invention
Solve the technical problem that: the deficiency existed for prior art, the invention provides a kind of acetic acid, ethyl acetate hydrogenation instead
Answer the device and method of integration system ethanol, same device and technique realize acetic acid, ethyl acetate is gasified totally Hydrogenation second
Alcohol, and feed stock conversion is high, selectivity is good, and purify simple in construction, easy to operate, steam consumption is low.
Technical scheme: a kind of acetic acid of present invention offer, the device of ethyl acetate hydrogenation reaction integration system ethanol, including raw material
Air compressor, recycle gas compressor, heat exchanger, acetic acid tank, ethyl acetate storage tank, raw material pump, feed preheater, vapour
Gasifying device, vapor seperator, reaction unit, water cooler, high-pressure separator, low pressure separator, torch house steward, coarse ethanol are pre-
Hot device and purifying plant；
Described acetic acid tank, ethyl acetate outlet are connected with raw material pump intake respectively, and each pipeline that connects is respectively equipped with one
Valve；Described raw material pump discharge is connected with feed preheater material channel entrance, and the outlet of feed preheater material channel is sequentially connected with
Vapourizing unit, vapor seperator, the gaseous phase outlet of vapor seperator is connected with reaction unit, and liquid-phase outlet is connected with vapourizing unit；
Described reaction unit includes steam heater, acetic acid hydrogenation reactor and ethyl acetate hydrogenation reactor, and three is linked in sequence, respectively
Connect pipeline enclosure and be equipped with a valve, between described acetic acid hydrogenation reactor and heat exchanger, be additionally provided with a valve；Reaction dress
Putting outlet to be connected with heat exchanger hot gas path entrance, the outlet of described heat exchanger hot gas path enters with feed preheater hot gas path
Mouth connects, and the outlet of feed preheater hot gas path is sequentially connected with water cooler, high-pressure separator, low pressure separator, coarse ethanol preheating
Device and purifying plant；Described high-pressure separator and low pressure separator gaseous phase outlet are connected with torch house steward, and high-pressure separator gas phase goes out
Mouth branch is connected with recycle gas compressor, and recycle gas compressor is with feed gas compressor outlet with heat exchanger material channel import even
Connecing, the outlet of heat exchanger material channel is connected with vapourizing unit.
A kind of acetic acid of present invention offer, the method for ethyl acetate hydrogenation reaction integration system ethanol, comprise the following steps:
(1) from the hydrogen outside battery limit (BL), after feed gas compressor is compressed to 6MpaG～10.0MpaG, and through circulation air pressure
Contracting machine be pressurized to 6MpaG～10.0MpaG circulating air mixing after, more in a heat exchanger with working off one's feeling vent one's spleen from reaction unit
Heat exchange, is heated to 170 DEG C～200 DEG C；
(2) if desired acetic acid preparation of ethanol by hydrogenating, the acetum from acetic acid tank is pumped to feed preheater through raw material and is preheated to
After 120 DEG C～140 DEG C, in vapourizing unit, mix vaporization with the gaseous mixture of the raw hydrogen carrying out automatic heat-exchanger and circulating air；Vapour
After the gaseous mixture of acetic acid steam, raw hydrogen and circulating air after change removes the liquid phase of entrained with in vapor seperator, liquid phase is returned
The bottom of back-steam gasifying device, gas phase enters steam heater, delivers to acetic acid hydrogenation reactor and carry out after being heated to 200 DEG C～230 DEG C
Acetic acid catalytic hydrogenation reaction, generates ethanol and ethyl acetate；Ethyl acetate enters ethyl acetate hydrogenation reactor, reacts further
Generate ethanol and by-product；
If desired ethyl acetate preparation of ethanol by hydrogenating, the ethyl acetate solution from ethyl acetate storage tank is pumped to raw material preheating through raw material
After device is preheated to 120 DEG C～140 DEG C, mix in vapourizing unit with the gaseous mixture of the raw hydrogen carrying out automatic heat-exchanger and circulating air
Vaporization；The gaseous mixture of ethyl acetate steam, raw hydrogen and circulating air after vaporization removes the liquid of entrained with in vapor seperator
Xiang Hou, liquid phase returns to the bottom of vapourizing unit, and gas phase enters steam heater, delivers to acetic acid second after being heated to 230 DEG C～270 DEG C
Ester through hydrogenation reactor carries out ethyl acetate catalytic hydrogenation reaction, generates ethanol and by-product；
(3) exhaust gas of ethyl acetate hydrogenation reactor in a heat exchanger with the gaseous mixture heat exchange of raw hydrogen and circulating air after,
After entering back into feed preheater and raw material acetic acid or ethyl acetate heat exchange, water cooled device is cooled to 30 DEG C～50 DEG C, delivers to high pressure and divides
From device gas-liquid separation；Gas phase after separation, a part is pressurized to 6MpaG～10.0MpaG as circulating air through recycle gas compressor
Participating in circulation, a part is emitted into torch house steward as off-gas, and liquid phase is decompressed to 0.5MPaG and enters low pressure separator；
(4) gas phase through low pressure separator flash distillation delivers to torch house steward, and liquid phase enters coarse ethanol preheater and is preheating to
100 DEG C～125 DEG C are sent purifying plant, and the purified device of coarse ethanol purifies and obtains alcohol product.
In described acetic acid preparation of ethanol by hydrogenating technique containing the equipment of acetic acid raw material and pipeline use resistant material built-up welding inconel or
Kazakhstan G.
During described acetic acid catalytic hydrogenation reaction, hydracid mol ratio is 1/10～1/30, and described catalyst is to be catalyzed containing precious metal palladium
Agent.In described ethyl acetate hydrogenation process, hydrogen ester mol ratio is 1/30～1/60, and described catalyst is Cu-contained catalyst.
Beneficial effect: (1) present invention achieves acetic acid, ethyl acetate Hydrogenation second at same device by switching annexation
The production technology of alcohol product, easy to operate, energy consumption is low, saves cost of investment and production cost.
(2) vapourizing unit that the present invention uses can solve acetic acid or acetic acid in acetic acid, ethyl acetate preparation of ethanol by hydrogenating technique simultaneously
The problem that ethyl ester completely vaporizes, the purifying plant of employing makes the steam consumption of alcohol product per ton less than 1.5 tons, is significantly less than
The steam consumption of prior art.
(3) acetic acid of the present invention, the device of ethyl acetate hydrogenation integration system ethanol, feed stock conversion is more than 99%, and ethanol selects
Property more than 98.9%, the most existing Technology all increases.Package unit passes through technological parameter such as pressure, temperature, hydrogen
The regulation of acid ratio etc., produces the alcohol product of purity 95%～99.5%, and wherein 99.5% alcohol product can reach anhydrous alcohol
High-class product indices.
(4) for acetic acid hydrogenation reaction, in order to prevent acetic acid etching problem, the equipment containing acetic acid raw material and pipe in whole technique
Road employs the resistant materials such as built-up welding inconel, Kazakhstan G.
(5) equal non-pollution discharge in whole technical process, has good environment-friendly advantage.
Accompanying drawing explanation
Fig. 1 is the process unit schematic flow sheet of the present invention.
Detailed description of the invention
Further illustrate the present invention below by the mode of embodiment, but the most therefore protection scope of the present invention is confined to following reality
Execute example, but limited by description and claims of this specification.
Embodiment 1
As it is shown in figure 1, a kind of acetic acid, the device of ethyl acetate hydrogenation reaction integration system ethanol, including feed gas compressor,
Recycle gas compressor, heat exchanger, acetic acid tank, ethyl acetate storage tank, raw material pump, feed preheater, vapourizing unit, steaming
Send out separator, reaction unit, water cooler, high-pressure separator, low pressure separator, torch house steward, coarse ethanol preheater and purification
Device；
Described acetic acid tank, ethyl acetate outlet are connected with raw material pump intake respectively, and each pipeline that connects is respectively equipped with one
Valve；Described raw material pump discharge is connected with feed preheater material channel entrance, and the outlet of feed preheater material channel is sequentially connected with
Vapourizing unit, vapor seperator, the gaseous phase outlet of vapor seperator is connected with reaction unit, and liquid-phase outlet is connected with vapourizing unit；
Described reaction unit includes steam heater, acetic acid hydrogenation reactor and ethyl acetate hydrogenation reactor, and three is linked in sequence, respectively
Connect pipeline enclosure and be equipped with a valve, between described acetic acid hydrogenation reactor and heat exchanger, be additionally provided with a valve；Reaction dress
Putting outlet to be connected with heat exchanger hot gas path entrance, the outlet of described heat exchanger hot gas path enters with feed preheater hot gas path
Mouth connects, and the outlet of feed preheater hot gas path is sequentially connected with water cooler, high-pressure separator, low pressure separator, coarse ethanol preheating
Device and purifying plant；Described high-pressure separator and low pressure separator gaseous phase outlet are connected with torch house steward, and high-pressure separator gas phase goes out
Mouth branch is connected with recycle gas compressor, and recycle gas compressor is with feed gas compressor outlet with heat exchanger material channel import even
Connecing, the outlet of heat exchanger material channel is connected with vapourizing unit.
Embodiment 2
As it is shown in figure 1, a kind of acetic acid, the method for ethyl acetate hydrogenation reaction integration system ethanol, comprise the following steps:
(1) from the hydrogen outside battery limit (BL), after feed gas compressor is compressed to 6MpaG～10.0MpaG, and through circulation air pressure
Contracting machine be pressurized to 6MpaG～10.0MpaG circulating air mixing after, more in a heat exchanger with working off one's feeling vent one's spleen from reaction unit
Heat exchange, is heated to 170 DEG C～200 DEG C；
(2), during acetic acid preparation of ethanol by hydrogenating, ethyl acetate storage tank and raw material pump, steam heater and ethyl acetate hydrogenation reaction are closed
Valve between device, the acetum from acetic acid tank is pumped to after feed preheater is preheated to 120 DEG C～140 DEG C through raw material,
In vapourizing unit, vaporization is mixed with the gaseous mixture of the raw hydrogen carrying out automatic heat-exchanger and circulating air；Acetic acid steam after vaporization,
After the gaseous mixture of raw hydrogen and circulating air removes the liquid phase of entrained with in vapor seperator, liquid phase returns to the bottom of vapourizing unit,
Gas phase enters steam heater, delivers to acetic acid hydrogenation reactor and carry out acetic acid catalytic hydrogenation reaction after being heated to 200 DEG C～230 DEG C,
Generate ethanol and ethyl acetate；Ethyl acetate enters ethyl acetate hydrogenation reactor, and reaction generates ethanol and by-product further；
During described acetic acid catalytic hydrogenation reaction, hydracid mol ratio is 1/10～1/30, and described catalyst is containing precious metals palladium catalyst.
During ethyl acetate preparation of ethanol by hydrogenating, close acetic acid tank and raw material pump, steam heater and acetic acid hydrogenation reactor, acetic acid
Valve between hydrogenation reactor and ethyl acetate hydrogenation reactor, acetic acid hydrogenation reactor and heat exchanger hot gas path entrance,
Ethyl acetate solution from ethyl acetate storage tank is pumped to after feed preheater is preheated to 120 DEG C～140 DEG C through raw material, with from
The raw hydrogen of heat exchanger and the gaseous mixture of circulating air mix vaporization in vapourizing unit；Ethyl acetate steam after vaporization, former
After the gaseous mixture of material hydrogen and circulating air removes the liquid phase of entrained with in vapor seperator, liquid phase returns to the bottom of vapourizing unit,
Gas phase enter steam heater, deliver to after being heated to 230 DEG C～270 DEG C ethyl acetate hydrogenation reactor carry out ethyl acetate catalysis add
Hydrogen reacts, and generates ethanol and by-product；In described ethyl acetate hydrogenation process, hydrogen ester mol ratio is 1/30～1/60, described
Catalyst is Cu-contained catalyst.
(3) exhaust gas of ethyl acetate hydrogenation reactor in a heat exchanger with the gaseous mixture heat exchange of raw hydrogen and circulating air after,
After entering back into feed preheater and raw material acetic acid or ethyl acetate heat exchange, water cooled device is cooled to 30 DEG C～50 DEG C, delivers to high pressure and divides
From device gas-liquid separation；Gas phase after separation, a part is pressurized to 6MpaG～10.0MpaG as circulating air through recycle gas compressor
Participating in circulation, a part is emitted into torch house steward as off-gas, and liquid phase is decompressed to 0.5MPaG and enters low pressure separator；
(4) gas phase through low pressure separator flash distillation delivers to torch house steward, and liquid phase enters coarse ethanol preheater and is preheating to
100 DEG C～125 DEG C are sent purifying plant, and the purified device of coarse ethanol purifies and obtains highly purified alcohol product.
The vapourizing unit that the present invention uses can solve acetic acid or ethyl acetate in acetic acid, ethyl acetate preparation of ethanol by hydrogenating technique simultaneously
The problem completely vaporized, the purifying plant of employing makes the steam consumption of alcohol product per ton less than 1.5 tons, is significantly less than existing
The steam consumption of technology.
Feed stock conversion of the present invention is more than 99%, and ethanol selectivity is more than 98.9%, and the most existing Technology all increases.
Package unit is by the regulation of technological parameter such as pressure, temperature, hydracid ratio etc., and the ethanol producing purity 95%～99.5% produces
Product, wherein 99.5% alcohol product can reach the high-class product indices of anhydrous alcohol.
Claims (5)
1. acetic acid, a device for ethyl acetate hydrogenation reaction integration system ethanol, including feed gas compressor, cycle compressor
Machine, heat exchanger, acetic acid tank, ethyl acetate storage tank, raw material pump, feed preheater, vapourizing unit, vapor seperator,
Reaction unit, water cooler, high-pressure separator, low pressure separator, torch house steward, coarse ethanol preheater and purifying plant；
It is characterized in that described acetic acid tank, ethyl acetate outlet are connected with raw material pump intake respectively, each pipeline that connects divides
It is not provided with a valve；Described raw material pump discharge is connected with feed preheater material channel entrance, and feed preheater material channel goes out
Mouth is sequentially connected with vapourizing unit, vapor seperator, and the gaseous phase outlet of vapor seperator is connected with reaction unit, liquid-phase outlet and vapour
Gasifying device connects；Described reaction unit includes steam heater, acetic acid hydrogenation reactor and ethyl acetate hydrogenation reactor, three
Being linked in sequence, each pipeline enclosure that connects is equipped with a valve, is additionally provided with one between described acetic acid hydrogenation reactor and heat exchanger
Valve；Reaction unit outlet is connected with heat exchanger hot gas path entrance, the outlet of described heat exchanger hot gas path and raw material preheating
Device hot gas path entrance connect, feed preheater hot gas path outlet be sequentially connected with water cooler, high-pressure separator, low pressure separator,
Coarse ethanol preheater and purifying plant；Described high-pressure separator and low pressure separator gaseous phase outlet are connected with torch house steward, and high pressure divides
It is connected with recycle gas compressor from device gaseous phase outlet branch, recycle gas compressor and feed gas compressor outlet and heat exchanger raw material
Channel entrance connects, and the outlet of heat exchanger material channel is connected with vapourizing unit.
A kind of acetic acid the most as claimed in claim 1, ethyl acetate hydrogenation reaction integration system ethanol device a kind of acetic acid,
The method of ethyl acetate hydrogenation reaction integration system ethanol, it is characterised in that comprise the following steps:
(1) from the hydrogen outside battery limit (BL), after feed gas compressor is compressed to 6MpaG～10.0MpaG, and through circulation air pressure
Contracting machine be pressurized to 6MpaG～10.0MpaG circulating air mixing after, more in a heat exchanger with working off one's feeling vent one's spleen from reaction unit
Heat exchange, is heated to 170 DEG C～200 DEG C；
(2) if desired acetic acid preparation of ethanol by hydrogenating, the acetum from acetic acid tank is pumped to feed preheater through raw material and is preheated to
After 120 DEG C～140 DEG C, in vapourizing unit, mix vaporization with the gaseous mixture of the raw hydrogen carrying out automatic heat-exchanger and circulating air；Vapour
After the gaseous mixture of acetic acid steam, raw hydrogen and circulating air after change removes the liquid phase of entrained with in vapor seperator, liquid phase is returned
The bottom of back-steam gasifying device, gas phase enters steam heater, delivers to acetic acid hydrogenation reactor and carry out after being heated to 200 DEG C～230 DEG C
Acetic acid catalytic hydrogenation reaction, generates ethanol and ethyl acetate；Ethyl acetate enters ethyl acetate hydrogenation reactor, reacts further
Generate ethanol and by-product；
If desired ethyl acetate preparation of ethanol by hydrogenating, the ethyl acetate solution from ethyl acetate storage tank is pumped to raw material preheating through raw material
After device is preheated to 120 DEG C～140 DEG C, mix in vapourizing unit with the gaseous mixture of the raw hydrogen carrying out automatic heat-exchanger and circulating air
Vaporization；The gaseous mixture of ethyl acetate steam, raw hydrogen and circulating air after vaporization removes the liquid of entrained with in vapor seperator
Xiang Hou, liquid phase returns to the bottom of vapourizing unit, and gas phase enters steam heater, delivers to acetic acid second after being heated to 230 DEG C～270 DEG C
Ester through hydrogenation reactor carries out ethyl acetate catalytic hydrogenation reaction, generates ethanol and by-product；
(3) exhaust gas of ethyl acetate hydrogenation reactor in a heat exchanger with the gaseous mixture heat exchange of raw hydrogen and circulating air after,
After entering back into feed preheater and raw material acetic acid or ethyl acetate heat exchange, water cooled device is cooled to 30 DEG C～50 DEG C, delivers to high pressure and divides
From device gas-liquid separation；Gas phase after separation, a part is pressurized to 6MpaG～10.0MpaG as circulating air through recycle gas compressor
Participating in circulation, a part is emitted into torch house steward as off-gas, and liquid phase is decompressed to 0.5MPaG and enters low pressure separator；
(4) gas phase through low pressure separator flash distillation delivers to torch house steward, and liquid phase enters coarse ethanol preheater and is preheating to 100 DEG C
～125 DEG C sent purifying plant, the purified device of coarse ethanol purifies and obtains alcohol product.
A kind of acetic acid the most according to claim 2, the method for ethyl acetate hydrogenation reaction integration system ethanol, its feature exists
In described acetic acid preparation of ethanol by hydrogenating technique, equipment and pipeline containing acetic acid raw material use resistant material built-up welding inconel or Kazakhstan
Family name G.
A kind of acetic acid the most according to claim 2, the method for ethyl acetate hydrogenation reaction integration system ethanol, its feature exists
During described acetic acid catalytic hydrogenation reaction, hydracid mol ratio is 1/10～1/30, and described catalyst is containing precious metals palladium catalyst.
A kind of acetic acid the most according to claim 2, the method for ethyl acetate hydrogenation reaction integration system ethanol, its feature exists
In described ethyl acetate hydrogenation process, hydrogen ester mol ratio is 1/30～1/60, and described catalyst is Cu-contained catalyst.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942446A (en) * | 2012-12-03 | 2013-02-27 | 大唐国际化工技术研究院有限公司 | Method for preparing ethanol via hydrogenation of acetic ester based on recirculating of recovered hydrogen |
| CN103159588A (en) * | 2011-12-15 | 2013-06-19 | 西南化工研究设计院 | Optimized separation process for ethanol production from ester hydrogenation |
| CN105566063A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Ethanol preparation method |
-
2016
- 2016-06-22 CN CN201610456928.XA patent/CN106008155A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103159588A (en) * | 2011-12-15 | 2013-06-19 | 西南化工研究设计院 | Optimized separation process for ethanol production from ester hydrogenation |
| CN102942446A (en) * | 2012-12-03 | 2013-02-27 | 大唐国际化工技术研究院有限公司 | Method for preparing ethanol via hydrogenation of acetic ester based on recirculating of recovered hydrogen |
| CN105566063A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Ethanol preparation method |
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Application publication date: 20161012 |