CN106045855A - System for preparing ethyl acrylate from acetylene, and method thereof - Google Patents
System for preparing ethyl acrylate from acetylene, and method thereof Download PDFInfo
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- CN106045855A CN106045855A CN201610659229.5A CN201610659229A CN106045855A CN 106045855 A CN106045855 A CN 106045855A CN 201610659229 A CN201610659229 A CN 201610659229A CN 106045855 A CN106045855 A CN 106045855A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/36—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates
- C07C67/38—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates by addition to an unsaturated carbon-to-carbon bond
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
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Abstract
The invention discloses a system for preparing ethyl acrylate from acetylene, and a method thereof. The system comprises an acetylene dissolving tank, a reactor, a first gas-liquid separator, a second gas-liquid separator, a carbon monoxide extraction device and a compressor, and the acetylene dissolving tank is provided with an acetylene inlet, a nonpolar organic solvent inlet and a liquid outlet; the reactor comprises an acetylene solvent inlet, a carbon monoxide gas inlet and a gas outlet; the first gas-liquid separator comprises a gas inlet, a gas outlet and an ethyl acrylate outlet; and the second gas-liquid separator comprises a gas inlet and a gas outlet. The system and the method allow the above product, byproducts and solvents to be separated at different distillation temperatures and carbon monoxide and the organic solvent to be recycled, so raw materials are saved, and the cost is reduced.
Description
Technical field
The invention belongs to chemical field, particularly relate to the system and method for a kind of acetylene ethyl acrylate.
Background technology
Along with petroleum resources are the most exhausted, Development of Coal chemical products are that the chemical process of raw material becomes petroleum replacing chemical industry road
The significant process of line, obtains extensive concern, and obtains fast development.
Esters of acrylic acid is one of important fine chemical material, is mainly used as organic synthesis intermediate and synthesis macromolecule
The monomer of material.The polymer products that ethyl acrylate and polyvinyl monomers perhaps are formed fabric and the modification of plastics,
The aspect tools such as the processing of leather and fiber have been widely used.It is together with the various polymer of acrylic acid and acrylates, structure
Become oleic series chemical products, be the important monomer preparing macromolecular compound.Ethyl acrylate is to prepare carbamate
The intermediate of insecticides Benfuracard micro, also acts as protective coating, adhesive and the raw material of paper impregnating agent, its polymer
The anti-cracking agent of leather can be made.At present, the production of ethyl acrylate mainly has acrylic acid and ethanol lactate synthesis and acetylene, an oxidation
The direct oxo process of carbon, ethanol.The acrylic acid of acroleic acid esterification method mainly uses propylene fraction oxidizing process to prepare, and production cost is relatively
Low, but this method too relies on the most nervous petroleum resources.And acetylene carbonylation method is directly synthesized ethyl acrylate, it is independent of
Oil, is particularly suitable for oil-poor, rich gas, rich coal country development fine chemistry industry.China's coal, natural gas resource are abundant, and
And can be as synthesizing acrylic acid from acetylene carbonyl second containing substantial amounts of carbon monoxide in richness product carbide, and carbide legal system acetylene tail gas
The carbonyl source of ester, therefore, this route has resources advantage in China's development.
Owing to acetylene carbonyl turns to strong exothermal reaction, reaction selectivity temperature influence is obvious, and reaction is many in solution-air mode
Carry out.Even if acetylene, carbon monoxide react in very harsh condition the most hardly with ethanol, develop effective catalyst one
It it is directly the focus of synthesizing acrylic acid from acetylene carbonyl route.Reppe method original adoption Nickel tetracarbonyl. makees catalyst, enters catalyst subsequently
The substantial amounts of improvement of row, the stechiometry that has been born, catalysis method, the Reppe method of Rohm&Haas company improvement and Dow-Badische
The high pressure Reppe method that company improves.But Nickel tetracarbonyl. toxicity is high, totally unfavorable to labour protection, there is knot in the catalyst system and catalyzing after improvement
Carbon and conversion ratio, yield are relatively low.
Summary of the invention
In order to solve the problems referred to above, the present invention provides the system and method for a kind of acetylene ethyl acrylate, by distillating
The difference of temperature can be by product, and by-product and solvent separate, and reclaims ethanol, organic solvent and carbon monoxide cycle again
Utilize, economize in raw materials, reduce cost.
An object of the present invention is to provide the system of a kind of acetylene ethyl acrylate, and this system includes: acetylene dissolves
Tank, reactor, the first gas-liquid separator, the second gas-liquid separator, carbon monoxide extraction element and compressor.
Described acetylene dissolving tank is provided with acetylene entrance, non-polar organic solvent entrance and liquid outlet, and acetylene is passed through nonpolar
Organic solvent dissolves and reaches saturation.
Described reactor includes solvents for ethyne entrance, carbon monoxide gas inlet and gas outlet, and reactor is used for acetylene
Carbonylation.
Described first gas-liquid separator includes gas access, gas outlet and ethyl acrylate outlet.
Described second gas-liquid separator includes gas access and gas outlet.
Described acetylene dissolving tank liquid outlet is connected with described reactor solvents for ethyne entrance, described gas reactor outlet with
Described first gas-liquid separator gas access connects, described first gas-liquid separator gas outlet and described second gas-liquid separator
Gas access connects, and described second gas-liquid separator gas outlet is connected with described carbon monoxide extraction element gas access, institute
Stating carbon monoxide extraction element to be connected with described compressor, described compressor is with described reactor carbon monoxide gas inlet even
Connect.
In the present invention, described second gas-liquid separator includes liquid-phase outlet, described liquid-phase outlet and described acetylene dissolving tank
Non-polar organic solvent entrance connect, it is achieved ethanol and the recycling of non-polar organic solvent.
In the present invention, described carbon monoxide extraction element is provided with offgas outlet, extracts the tail gas after carbon monoxide through tail gas
Reaction system is discharged in outlet.
In the present invention, described second gas-liquid separator is provided with byproduct discharge, and reaction gained by-product is by byproduct discharge
Derive.
It is a further object of the present invention to provide a kind of method utilizing said system acetylene carbonylation ethyl acrylate, bag
Include following steps:
Acetylene dissolves, and acetylene is passed through non-polar organic solvent and dissolves and reach saturation；
Acetylene carbonylation, is passed through the carbon monoxide of pressurization beds and enters with ethanol and dissolving acetylene in a solvent
Row reaction, reaction pressure is 0.3～10MPa, and reaction temperature is 150～250 DEG C, acetylene and mol ratio n of carbon monoxide
(C2H2): the mol ratio n (C of n (CO)=1:l～1:15, acetylene and ethanol2H2):n(C2H5OH)=1:1～1:10, acetylene is with molten
The mass ratio of agent is m (C2H2): m (solvent)=1:5～1:30, obtain containing ethyl acrylate, unreacted acetylene, unreacted
Carbon monoxide, unreacted ethanol, non-polar organic solvent, the gas-liquid mixture of by-product；
Gas-liquid first separation, by described gas-liquid mixture through cooling down laggard row gas-liquid separation, prepares ethyl acrylate；
Gas-liquid secondary separation, further separates gained gas after described gas-liquid first separation, obtains unreacted second
Alcohol, non-polar organic solvent containing a small amount of unreacted acetylene and by-product, unreacted ethanol and containing a small amount of unreacted second
The non-polar organic solvent recycle and reuse of alkynes；
Extract carbon monoxide, the gas extraction carbon monoxide after described gas-liquid secondary separation, the carbon monoxide of described extraction
Utilize as carbonylation feedstock circulation, extract the tail gas after carbon monoxide and discharge reaction system.
This reaction is gas-liquid two-phase haptoreaction, does not has solid catalyst, thus avoid catalyst in reaction system
Loss.Acetylene is dissolved and reacts in a solvent, it is to avoid the danger that acetylene explodes under high-temperature and high-pressure conditions, and ensure bed
Temperature stabilization, will not occur beds temperature runaway.Can directly be recycled by the solvent that product is separated and recovered.
In the present invention, described process further comprises the steps of: carbon monoxide and pressurizes through compressor.
In the present invention, described non-polar organic solvent includes oxolane, 2-methyltetrahydrofuran, N-crassitude
One or more in ketone, acetone and acetylacetone,2,4-pentanedione.Non-polar organic solvent is not limited only to enumerated above several, this area
Technical staff can optionally choose.
In the present invention, the compound that catalyst is active metal described in described step acetylene carbonylation and auxiliary agent mixed
Close solution.
Acetylene is first dissolved in repressurization in non-polar organic solvent by the present invention, reduces direct compressed acetylene body and brings
Potential safety hazard；By the difference of recovered (distilled) temperature can be by ethyl acrylate, by-product and solvent separate, it is to avoid increase
Solvent reclamation device；In system of the present invention, ethanol after secondary gas-liquid separation and organic solvent can be again with, as
The raw material of acetylene dissolving tank, and the carbon monoxide that carbon monoxide extraction element obtains is back in reactor as raw material；This
Invent described system can cycling and reutilization organic solvent and carbon monoxide, economize in raw materials, reduce cost, system structure is simple,
Easy to operate.
Accompanying drawing explanation
Fig. 1 is the system structure schematic diagram of acetylene ethyl acrylate of the present invention；
Fig. 2 is the schematic flow sheet of the method for acetylene ethyl acrylate of the present invention.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and various aspects thereof.But, specific embodiments described below and enforcement
Example is only descriptive purpose rather than limitation of the present invention.
An object of the present invention is to provide the system of a kind of acetylene ethyl acrylate, as it is shown in figure 1, this system bag
Include: acetylene dissolving tank 1, reactor the 2, first gas-liquid separator the 3, second gas-liquid separator 4, carbon monoxide extraction element 5 and pressure
Contracting machine 6.
Acetylene dissolving tank 1 is provided with acetylene entrance, non-polar organic solvent entrance and liquid outlet.Acetylene is passed through nonpolar organic
Solvent dissolves and reaches saturation.
Reactor 2 is acetylene carbonylation apparatus, including solvents for ethyne entrance, carbon monoxide gas inlet and gas outlet.
Acetylene carbonyl is there is in the be dissolved with solvent of acetylene, carbon monoxide and the ethanol importing reactor 2 of pressurization under the effect of catalyst
Glycosylation reaction.The non-polar organic solvent of dissolved acetylene undergoes phase transition along with temperature raises, and utilizes gasification latent heat to carry off acetylene and adds
The big calorimetric that hydrogen process is released, keeps stablizing of reaction bed temperature with this.
First gas-liquid separator 3 includes gas access, gas outlet and ethyl acrylate outlet.Gas-liquid separation gained
Ethyl acrylate is derived by ethyl acrylate outlet.
Second gas-liquid separator 4 includes gas access, gas outlet, liquid-phase outlet and byproduct discharge.Liquid-phase outlet with
The non-polar organic solvent entrance of acetylene dissolving tank 1 connects, it is achieved ethanol and the recycling of non-polar organic solvent.Reaction
Gained by-product is derived by byproduct discharge.
Carbon monoxide extraction element 5 is provided with carbon monoxide outlet and offgas outlet, and the carbon monoxide of extraction is through carbon monoxide
Outlet imports compressor 6, extracts the tail gas after carbon monoxide and discharges reaction system through offgas outlet.
Compressor 6 is for the pressurization of carbon monoxide, compressor 6 coupled reaction device 2 carbon monoxide gas inlet.
Acetylene dissolving tank 1 liquid outlet is connected with reactor 2 solvents for ethyne entrance, reactor 2 gas outlet and the first gas-liquid
Separator 3 gas access connects, and the first gas-liquid separator 3 gas outlet is connected with the second gas-liquid separator 4 gas access, and second
Gas-liquid separator 4 gas outlet is connected with carbon monoxide extraction element 5 gas access, carbon monoxide extraction element 5 and compressor 6
Connecting, compressor 6 is connected with reactor 2 carbon monoxide gas inlet.
It is a further object of the present invention to provide the method utilizing said system acetylene carbonylation ethyl acrylate, such as Fig. 2
Shown in, the method comprises the steps:
1, acetylene dissolves, and acetylene and non-polar organic solvent is passed through acetylene dissolving tank, makes acetylene nonpolar organic molten
Agent is dissolved and reaches saturation；
2, acetylene carbonylation, is passed through beds and ethanol and dissolving acetylene in a solvent by the carbon monoxide of pressurization
Reacting, reaction pressure is 0.3～10MPa, and reaction temperature is 150～250 DEG C, acetylene and mol ratio n of carbon monoxide
(C2H2): the mol ratio n (C of n (CO)=1:l～1:15, acetylene and ethanol2H2):n(C2H5OH)=1:l～1:10, acetylene is with molten
The mass ratio of agent is m (C2H2): m (solvent)=1:5～1:30, obtain containing ethyl acrylate, unreacted acetylene, unreacted
Carbon monoxide, unreacted ethanol, non-polar organic solvent, the gas-liquid mixture of by-product；
3, gas-liquid first separation, described gas-liquid mixture imports described first gas-liquid separator, carries out after cooling down
Gas-liquid separation, prepares ethyl acrylate；
4, gas-liquid secondary separation, after described gas-liquid first separation, gained gas imports the second gas-liquid separator and further divides
From, obtain unreacted ethanol, non-polar organic solvent containing a small amount of unreacted acetylene and by-product, unreacted ethanol and
Non-polar organic solvent recycle and reuse containing a small amount of unreacted acetylene；
5, extracting carbon monoxide, the gas after described gas-liquid secondary separation imports carbon monoxide extraction element, the one of extraction
Carbonoxide utilizes as carbonylation feedstock circulation, extracts the tail gas after carbon monoxide and discharges reaction system；
6, the carbon monoxide extracted imports reactor after compressor pressurizes.
This reaction is gas-liquid two-phase haptoreaction, does not has solid catalyst, thus avoid catalyst in reaction system
Loss.Acetylene is dissolved and reacts in a solvent, it is to avoid the danger that acetylene explodes under high-temperature and high-pressure conditions, and ensure bed
Temperature stabilization, will not occur beds temperature runaway.Can be the most sharp by the second alcohol and solvent that product is separated and recovered
With, whole technique is simpler, easy to operate.
In the present invention, non-polar organic solvent include oxolane, 2-methyltetrahydrofuran, N-Methyl pyrrolidone, third
One or more in ketone and acetylacetone,2,4-pentanedione.Below it is only that non-polar organic solvent is enumerated, not as to nonpolar organic
The restriction of solvent.
In the present invention, the compound that catalyst is active metal and the mixing of auxiliary agent in described step acetylene carbonylation are molten
Liquid.
Below, by specific embodiment, the method for acetylene ethyl acrylate of the present invention is illustrated.
Process embodiment
Embodiment 1:
Acetylene raw gas pressure is 0.5MPa, is passed through in the non-polar organic solvent containing ethanol dissolving.
Organic solvent-acetone containing acetylene is forced into 5.5MPa by pump, delivers to reactor, then passes to 5.5MPa's
Carbon monoxide reacts, reaction temperature 200 DEG C, obtains containing ethyl acrylate, unreacted acetylene, a unreacted oxidation
Carbon, unreacted ethanol, non-polar organic solvent, the gas-liquid mixture of by-product.Catalyst in reactor is nickelous bromide, helps
Agent is copper bromide.
Reacted gas-liquid mixture temperature is 200 DEG C, enters the first gas-liquid separator and is cooled to 95 DEG C and obtains product third
Olefin(e) acid ethyl ester reclaims.
Gas after cooling enters the second gas-liquid separator and is again cooled to 20 DEG C and carries out gas-liquid separation, obtains ethanol and molten
Agent recycle and reuse.
Gas after gas-liquid secondary separation enters carbon monoxide extraction element, and the carbon monoxide of extraction exports through carbon monoxide
Import compressor, after compressor pressurizes, import reactor as carbonylation raw material, extract the tail gas warp after carbon monoxide
Offgas outlet discharges reaction system.
Embodiment 2:
The method using embodiment 1 prepares ethyl acrylate, and difference is: non-polar organic solvent replaces with tetrahydrochysene furan
Mutter；Reaction pressure is 1.5MPa；Reaction temperature is 240 DEG C.
Embodiment 3:
The method using embodiment 1 prepares ethyl acrylate, and difference is: non-polar organic solvent replaces with levulinic
Ketone；Reaction pressure is 8.0MPa；Reaction temperature is 160 DEG C.
Concrete process conditions and non-polar organic solvent in above example is used to carry out acetylene carbonylation acrylic acid
Ethyl ester, conversion of alkyne and ethyl acrylate selectivity result are as shown in table 1.
The conversion of alkyne of table 1 embodiment of the present invention and ethyl acrylate selectivity result
Using technique of the present invention to prepare ethyl acrylate, response speed is fast, and conversion of alkyne is high, ethyl acrylate
Selectivity is high, and can avoid compressing the potential safety hazard that acetylene causes owing to first dissolving repressurization；Course of reaction will not fly
Temperature phenomenon.Additionally, carbon monoxide, ethanol, organic solvent use and are respectively formed circulation line, effectively save cost in the present invention.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate rather than restriction originally
The scope of invention, it will be understood by those within the art that, the most right
Amendment that the present invention is carried out or equivalent, all should contain within the scope of the present invention.Additionally, indication unless the context
Outward, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can use in conjunction with all or part of of any other embodiments.
Claims (8)
1. the system of an acetylene ethyl acrylate, it is characterised in that including: acetylene dissolving tank, reactor, the first gas-liquid are divided
From device, the second gas-liquid separator, carbon monoxide extraction element and compressor,
Described acetylene dissolving tank is provided with acetylene entrance, non-polar organic solvent entrance and liquid outlet；
Described reactor includes solvents for ethyne entrance, carbon monoxide gas inlet and gas outlet；
Described first gas-liquid separator includes gas access, gas outlet and ethyl acrylate outlet；
Described second gas-liquid separator includes gas access and gas outlet；
Described acetylene dissolving tank liquid outlet is connected with described reactor solvents for ethyne entrance, and described gas reactor exports with described
First gas-liquid separator gas access connects, described first gas-liquid separator gas outlet and described second gas-liquid separator gas
Entrance connects, and described second gas-liquid separator gas outlet is connected with described carbon monoxide extraction element gas access, and described one
Carbonoxide extraction element is connected with described compressor, and described compressor is connected with described reactor carbon monoxide gas inlet.
System the most according to claim 1, it is characterised in that described second gas-liquid separator farther includes liquid phase and goes out
Mouthful, described liquid-phase outlet is connected with the non-polar organic solvent entrance of described acetylene dissolving tank.
System the most according to claim 1, it is characterised in that described carbon monoxide extraction element is provided with offgas outlet.
System the most according to claim 1, it is characterised in that described second gas-liquid separator is provided with byproduct discharge.
5. the method utilizing the arbitrary described system acetylene ethyl acrylate of claim 1-4, it is characterised in that include step
Rapid:
Acetylene dissolves, and acetylene is passed through non-polar organic solvent and dissolves and reach saturation；
Acetylene carbonylation, is passed through the carbon monoxide of pressurization beds and carries out instead with ethanol and dissolving acetylene in a solvent
Should, reaction pressure is 0.3～10MPa, and reaction temperature is 150～250 DEG C, acetylene and the mol ratio n (C of carbon monoxide2H2):n
(CO) the mol ratio n (C of=1:l～1:15, acetylene and ethanol2H2):n(C2H5The matter of OH)=1:l-1:10, acetylene and solvent
Amount ratio is m (C2H2): m (solvent)=1:5～1:30, obtain containing ethyl acrylate, unreacted acetylene, a unreacted oxygen
Change carbon, unreacted ethanol, non-polar organic solvent, the gas-liquid mixture of by-product；
Gas-liquid first separation, by described gas-liquid mixture through cooling down laggard row gas-liquid separation, prepares ethyl acrylate；
Gas-liquid secondary separation, further separates gained gas after described gas-liquid first separation, obtains unreacted ethanol, contains
There are non-polar organic solvent and a by-product of a small amount of unreacted acetylene, unreacted ethanol and non-containing a small amount of unreacted acetylene
Polar organic solvent recycle and reuse；
Extract carbon monoxide, the gas extraction carbon monoxide after described gas-liquid secondary separation, the carbon monoxide conduct of described extraction
Carbonylation feedstock circulation utilizes, and extracts the tail gas after carbon monoxide and discharges reaction system.
Method the most according to claim 5, it is characterised in that further comprise the steps of: carbon monoxide and pressurize through described compressor.
Method the most according to claim 5, it is characterised in that described non-polar organic solvent includes oxolane, 2-first
One or more in base oxolane, N-Methyl pyrrolidone, acetone or acetylacetone,2,4-pentanedione.
Method the most according to claim 5, it is characterised in that in described step acetylene carbonylation, described catalyst is
The compound of active metal and the mixed solution of auxiliary agent.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107185584A (en) * | 2017-05-05 | 2017-09-22 | 北京华福工程有限公司 | Catalyst for acetylene acrylic acid synthesizing ester of low-carbon alcohol and its production and use |
| CN107986965A (en) * | 2016-10-27 | 2018-05-04 | 上海浦景化工技术股份有限公司 | A kind of method of synthesizing acrylic acid from acetylene carbonyl ester of low-carbon alcohol |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2883418A (en) * | 1953-11-14 | 1959-04-21 | Basf Ag | Acrylic acid ester production |
| CN1068105A (en) * | 1991-07-03 | 1993-01-20 | 国际壳牌研究有限公司 | Continuous process for carbonylation of acetylenes |
| CN101633615A (en) * | 2008-07-22 | 2010-01-27 | 中国科学院成都有机化学有限公司 | Method for synthesizing acrylic acid from acetylene carbonyl |
| CN102190583A (en) * | 2010-03-08 | 2011-09-21 | 中国科学院成都有机化学有限公司 | Method for synthesizing low carbon alcohol ester of acrylic acid by catalyzing acetylene carbonyl through palladium-phosphine complex |
| CN105753700A (en) * | 2014-12-19 | 2016-07-13 | 中国科学院大连化学物理研究所 | Method of synthesizing methyl acetate through acetylene carbonylation |
| CN106083582A (en) * | 2016-08-11 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene carbonylation acrylic acid methyl ester. |
| CN106083583A (en) * | 2016-08-11 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene acrylic acid ester of low-carbon alcohol |
| CN106220502A (en) * | 2016-08-11 | 2016-12-14 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene n-butyl acrylate |
| CN206143095U (en) * | 2016-08-11 | 2017-05-03 | 北京神雾环境能源科技集团股份有限公司 | System for acetylene system n -butyl acrylate |
| CN206521416U (en) * | 2016-08-11 | 2017-09-26 | 神雾科技集团股份有限公司 | A kind of system of acetylene ethyl acrylate |
| CN206521414U (en) * | 2016-08-11 | 2017-09-26 | 神雾科技集团股份有限公司 | The system that methyl acrylate processed is carbonylated in a kind of acetylene |
-
2016
- 2016-08-11 CN CN201610659229.5A patent/CN106045855A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2883418A (en) * | 1953-11-14 | 1959-04-21 | Basf Ag | Acrylic acid ester production |
| CN1068105A (en) * | 1991-07-03 | 1993-01-20 | 国际壳牌研究有限公司 | Continuous process for carbonylation of acetylenes |
| CN101633615A (en) * | 2008-07-22 | 2010-01-27 | 中国科学院成都有机化学有限公司 | Method for synthesizing acrylic acid from acetylene carbonyl |
| CN102190583A (en) * | 2010-03-08 | 2011-09-21 | 中国科学院成都有机化学有限公司 | Method for synthesizing low carbon alcohol ester of acrylic acid by catalyzing acetylene carbonyl through palladium-phosphine complex |
| CN105753700A (en) * | 2014-12-19 | 2016-07-13 | 中国科学院大连化学物理研究所 | Method of synthesizing methyl acetate through acetylene carbonylation |
| CN106083582A (en) * | 2016-08-11 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene carbonylation acrylic acid methyl ester. |
| CN106083583A (en) * | 2016-08-11 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene acrylic acid ester of low-carbon alcohol |
| CN106220502A (en) * | 2016-08-11 | 2016-12-14 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for acetylene n-butyl acrylate |
| CN206143095U (en) * | 2016-08-11 | 2017-05-03 | 北京神雾环境能源科技集团股份有限公司 | System for acetylene system n -butyl acrylate |
| CN206521416U (en) * | 2016-08-11 | 2017-09-26 | 神雾科技集团股份有限公司 | A kind of system of acetylene ethyl acrylate |
| CN206521414U (en) * | 2016-08-11 | 2017-09-26 | 神雾科技集团股份有限公司 | The system that methyl acrylate processed is carbonylated in a kind of acetylene |
Non-Patent Citations (3)
| Title |
|---|
| 安一哲等: ""高压法乙炔碳基化合成丙烯酸"", 《天然气化工》 * |
| 董俊强: ""高压法乙炔羰基化合成丙烯酸乙酯的研究"", 《中国优秀硕士学位论文全文数据库 工程科技I辑》 * |
| 邱家明: ""乙炔高压羰化合成丙烯酸 I沉积物形成的研究"", 《天然气化工》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107986965A (en) * | 2016-10-27 | 2018-05-04 | 上海浦景化工技术股份有限公司 | A kind of method of synthesizing acrylic acid from acetylene carbonyl ester of low-carbon alcohol |
| CN107986965B (en) * | 2016-10-27 | 2021-04-13 | 上海浦景化工技术股份有限公司 | Method for synthesizing acrylic acid low-carbon alcohol ester by acetylene carbonyl |
| CN107185584A (en) * | 2017-05-05 | 2017-09-22 | 北京华福工程有限公司 | Catalyst for acetylene acrylic acid synthesizing ester of low-carbon alcohol and its production and use |
| CN107185584B (en) * | 2017-05-05 | 2020-06-16 | 北京华福工程有限公司 | Catalyst for synthesizing acrylic acid low-carbon alcohol ester from acetylene and preparation method and application thereof |
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