CN110724025B - Device and method for preparing styrene by dehydrating phenethyl alcohol - Google Patents
Device and method for preparing styrene by dehydrating phenethyl alcohol Download PDFInfo
- Publication number
- CN110724025B CN110724025B CN201810779177.4A CN201810779177A CN110724025B CN 110724025 B CN110724025 B CN 110724025B CN 201810779177 A CN201810779177 A CN 201810779177A CN 110724025 B CN110724025 B CN 110724025B
- Authority
- CN
- China
- Prior art keywords
- dehydration tower
- dehydration
- tower
- reboiler
- phenethyl alcohol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
- C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention belongs to the field of styrene, and discloses a device and a method for preparing styrene by dehydrating phenethyl alcohol. The device comprises: a dehydration tower, a dehydration tower condenser, a dehydration tower reflux tank, a dehydration tower kettle circulating pump and a dehydration tower reboiler; wherein, the catalyst feed pipeline is connected with the dehydration tower kettle, and the crude phenethyl alcohol feed pipeline is connected with the dehydration tower kettle and/or the inlet of a reboiler of the dehydration tower; the top of the dehydration tower is sequentially connected with a dehydration tower condenser and a dehydration tower reflux tank; the reflux tank of the dehydration tower is connected with the dehydration tower; the bottom of the dehydration tower is sequentially connected with a dehydration tower kettle circulating pump and a dehydration tower reboiler; the outlet of the reboiler of the dehydration tower is connected with the dehydration tower; wherein the reboiler of the dehydration tower is a shell-and-tube heat exchanger. The invention uses the reboiler of the dehydration tower as the reactor, so that the phenethyl alcohol and the catalyst are uniformly mixed and immediately react after entering the reboiler of the dehydration tower, thereby reducing the retention time of the phenethyl alcohol, reducing the volume of the reactor and reducing the equipment investment.
Description
Technical Field
The invention belongs to the field of styrene, and particularly relates to a device and a method for preparing styrene by dehydrating phenethyl alcohol.
Background
The styrene compound is an important monomer for synthesizing the polystyrene resin, and various substituent groups on the benzene ring can endow the polystyrene resin with various properties, so that the polystyrene resin is suitable for various purposes. For example, the ion exchange resin is used for synthesizing the ion exchange resin, has good mechanical property and heat resistance, and can be used for preparing high-purity water in a thermal power plant, a nuclear submarine, the semiconductor industry, pharmacy and sugar industry. In addition, the styrene compound can be used for preparing various functional polymer materials such as photosensitive resin, adhesive, polymer film and the like, and is suitable for many fields.
One of the current methods for synthesizing styrene compounds is to dehydrate alpha or beta-phenylethanol compounds under high temperature and high pressure conditions. In JP49086332 and US3917223 p-chloroacetophenone is mixed with aluminium isopropoxide to supply heat, and p-chloroacetophenone is first reduced to 1- (p-chlorophenyl) ethanol and then dehydrated under reduced pressure at high temperature to obtain p-chlorostyrene. EP355983, US5041614, US5345074 and US5151546 prepare acetoxystyrene by continuous or semi-continuous dehydration of acetoxyphenyl methyl methanol in potassium hydrogen sulfate at about 240 deg.C and 150mmHg in a thin film evaporator. The solid-liquid mixing feeding method has the advantages of high difficulty, uneven mixing and poor separation effect. CN200510067856 discloses that alpha or beta-phenylethanol compounds are taken as raw materials to be subjected to dehydration reaction under the action of a catalyst to prepare styrene compounds, the basic process is that alpha or beta-phenylethanol compounds are dripped into a reaction raw material alpha or beta-phenylethanol compound (part), a catalyst and a polymerization inhibitor solution which are uniformly mixed in advance, and the product styrene compounds are continuously distilled out under reduced pressure while dehydration reaction is carried out. The technology is carried out in a reaction kettle, but the problems of long retention time, low heat transfer efficiency and the like still exist.
The inventor finds in research that the prior art styrene production device by phenylethanol dehydration has the following defects: 1. the retention time of the phenethyl alcohol in the reactor is long, the volume of the reactor is large, and the occupied area and investment are large; 2. local mixing is not uniform, circulation is poor, hot spots and dead zones are easy to occur, overheating is often needed to maintain reaction conversion rate, and main reaction selectivity and conversion rate are reduced; 3. the effective utilization volume in the reaction zone is not high.
Therefore, there is a need to develop a new process for preparing styrene by dehydrating phenethyl alcohol.
Disclosure of Invention
In order to solve the problems, the invention provides a device and a method for preparing styrene by dehydrating phenethyl alcohol. Through setting up the dehydration tower reboiler, improve and mix the effect, reduce equipment and take up an area of, reduce equipment investment.
In a first aspect of the present invention, there is provided an apparatus for producing styrene by dehydrating phenethyl alcohol, as shown in fig. 1, the apparatus comprising: a dehydration tower, a dehydration tower condenser, a dehydration tower reflux tank, a dehydration tower kettle circulating pump and a dehydration tower reboiler; wherein, the first and the second end of the pipe are connected with each other,
the catalyst feeding pipeline is connected with the dehydration tower kettle;
the crude phenethyl alcohol feeding pipeline is connected with the kettle of the dehydration tower and/or the inlet of a reboiler of the dehydration tower; preferably connected to the inlet of the reboiler of the dehydration column;
the top of the dehydration tower is sequentially connected with a dehydration tower condenser and a dehydration tower reflux tank;
the reflux tank of the dehydration tower is connected with the dehydration tower;
the bottom of the dehydration tower is sequentially connected with a dehydration tower kettle circulating pump and a dehydration tower reboiler;
the outlet of the reboiler of the dehydration tower is connected with the dehydration tower; the reboiler of the dehydration tower is a shell-and-tube heat exchanger.
Preferably, the reflux tank of the dehydration tower is a liquid-liquid separation tank, an organic phase extraction pipeline and a water phase extraction pipeline are arranged at the bottom of the reflux tank of the dehydration tower, and one branch of the water phase extraction pipeline is connected with the dehydration tower.
Preferably, the dewatering column internals are sieve plates, float valves, bubble caps or packings.
The second aspect of the invention provides a method for preparing styrene by dehydrating phenethyl alcohol by using the device, which comprises the following steps:
the crude phenethyl alcohol raw material enters the device through a crude phenethyl alcohol feeding pipeline and a catalyst through a catalyst feeding pipeline, a water phase and an organic phase mainly containing styrene are obtained at the top of the tower after heating, dehydration reaction and separation, and heavy oil is extracted at the bottom of the tower.
Specifically, the method comprises the following steps:
(a) feeding the crude phenethyl alcohol raw material into a dehydration tower kettle and/or a reboiler inlet, and feeding the catalyst into the dehydration tower kettle;
(b) the materials at the bottom of the dehydration tower are sent into a reboiler of the dehydration tower through a circulating pump at the bottom of the dehydration tower, and crude phenethyl alcohol is subjected to dehydration reaction in the reboiler of the dehydration tower under the action of a catalyst to obtain an outlet material flow of the reboiler of the dehydration tower containing styrene, acetophenone, phenethyl alcohol, water and heavy oil;
(c) rectifying and separating the material flow at the outlet of the reboiler of the dehydration tower through the dehydration tower, and condensing the tower top components through a condenser of the dehydration tower and then entering a reflux tank of the dehydration tower for settling and separation;
(d) respectively extracting a water phase and an organic phase rich in styrene and acetophenone from a reflux tank of the dehydration tower;
(e) the by-product containing heavy oil is extracted from the bottom of the dehydration tower.
According to the invention, preferably, the organic phase is sent to a downstream facility for further refining and separation to obtain high-purity styrene, the water phase is divided into two paths, one path is refluxed to enter a dehydration tower, and the other path is sent to the downstream facility for treatment.
According to the invention, steam or hot oil is preferably used as a heat source for the reboiler of the dehydration tower.
According to the present invention, preferably, the operating conditions of the dehydration column include: the pressure is 10-100 kPaA, the operation temperature at the top of the tower is 40-120 ℃, and the number of tower plates is 2-20.
According to the invention, the operating temperature of the reboiler of the dehydration tower is preferably not higher than the decomposition temperature of the liquid phase reaction medium, preferably 160-280 ℃, further preferably 180-250 ℃, and most preferably 200-230 ℃.
According to the present invention, preferably, the catalyst is at least one selected from the group consisting of inorganic acids, organic acids, inorganic oxides, and hydrogen sulfates, and further preferably sulfonic acid type sulfur-containing organic acids.
The beneficial effects of the invention include:
1) the dehydrating tower reboiler is used as a reactor, the phenethyl alcohol and the catalyst are uniformly mixed and immediately react after entering the dehydrating tower reboiler, so that the retention time of the phenethyl alcohol is reduced, the volume of the reactor is reduced, and the equipment investment is reduced.
2) The reboiler of the dehydration tower is used as a reactor, the mass transfer and heat transfer in the reactor are enhanced, the temperature distribution is uniform, no back mixing is caused, and the occurrence of side reactions is reduced.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings, wherein like reference numerals generally represent like parts in the exemplary embodiments of the present invention.
FIG. 1 is a schematic view of an apparatus for producing styrene by dehydrating phenethyl alcohol according to an embodiment of the present invention.
FIG. 2 is a schematic view of an apparatus for producing styrene by dehydration of phenethyl alcohol according to another embodiment of the present invention.
Description of reference numerals:
1. a dehydration tower; 2. a dehydrating tower condenser; 3. a dehydration tower reflux drum; 4. a circulating pump of the dehydration tower kettle; 5. a dehydration column reboiler; 6. a catalyst feed line; 7. a crude phenethyl alcohol feed line; 8. an organic phase extraction line; 9. an aqueous phase production line; 10. a heavy oil containing by-product.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below with reference to the accompanying drawings.
Example 1
The apparatus for producing styrene by dehydrating phenethyl alcohol shown in FIG. 2 was used to carry out the reaction for producing styrene by dehydrating phenethyl alcohol.
The device includes: a dehydration tower 1, a dehydration tower condenser 2, a dehydration tower reflux tank 3, a dehydration tower kettle circulating pump 4 and a dehydration tower reboiler 5; wherein, the catalyst feeding pipeline 6 is connected with the dehydration tower kettle; a crude phenethyl alcohol feed pipeline 7 is connected with an inlet of a dehydrating tower reboiler 5; the top of the dehydration tower 1 is sequentially connected with a dehydration tower condenser 2 and a dehydration tower reflux tank 3; the dehydration tower reflux tank 3 is connected with the dehydration tower 1; the bottom of the dehydration tower 1 is sequentially connected with a dehydration tower kettle circulating pump 4 and a dehydration tower reboiler 5; the outlet of the dehydrating tower reboiler 5 is connected with the dehydrating tower 1; the reboiler 5 of the dehydration tower is a shell-and-tube heat exchanger, the bottom of the reflux tank 3 of the dehydration tower is provided with an organic phase extraction pipeline 8 and a water phase extraction pipeline 9, and one branch of the water phase extraction pipeline 9 is connected with the dehydration tower 1; the internal parts of the dehydration tower 1 are sieve plates.
The method for preparing styrene by dehydrating phenethyl alcohol by adopting the device comprises the following steps:
(a) the crude phenethyl alcohol raw material enters an inlet of a reboiler 5 of a dehydration tower, and a catalyst enters a kettle of the dehydration tower;
(b) the materials at the bottom of the dehydration tower are sent into a reboiler 5 of the dehydration tower through a circulating pump 4 of the bottom of the dehydration tower, and the crude phenethyl alcohol is subjected to dehydration reaction in the reboiler 5 of the dehydration tower under the action of a catalyst to obtain the outlet material flow of the reboiler of the dehydration tower containing styrene, acetophenone, phenethyl alcohol, water and heavy oil;
(c) the material flow at the outlet of a reboiler 5 of the dehydration tower is rectified and separated by a dehydration tower 1, and the tower top components are condensed by a condenser 2 of the dehydration tower and then enter a reflux tank 3 of the dehydration tower for settlement and separation;
(d) the reflux tank 3 of the dehydration tower respectively extracts a water phase and an organic phase rich in styrene and acetophenone;
(e) the by-product 10 containing heavy oil is extracted from the bottom of the dehydration tower.
The reboiler of the dehydration tower adopts steam as a heat source, and the operation conditions of the dehydration tower comprise: the pressure at the top of the column was 22kPaA, the pressure at the bottom of the column was 26kPaA, the operating temperature at the top of the column was 92 ℃ and the number of trays was 10. The operating temperature of the reboiler of the dehydration column was 210 ℃.
The conversion of styrene alcohol was 95% and the selectivity of styrene 98%.
Compared with the traditional process of a kettle type reactor adopting an inner coil for heating, the device and the process method have the advantages that the conversion rate of the styrene is improved by 2 percent, the selectivity of the styrene is improved by 3 percent, the size of equipment is greatly reduced, the occupied area is saved, and the economic benefit is obvious.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (14)
1. The device for preparing styrene by dehydrating phenethyl alcohol is characterized in that:
the device includes: a dehydration tower, a dehydration tower condenser, a dehydration tower reflux tank, a dehydration tower kettle circulating pump and a dehydration tower reboiler; wherein the content of the first and second substances,
the catalyst feeding pipeline is connected with the dehydration tower kettle;
the crude phenethyl alcohol feeding pipeline is connected with the inlet of a reboiler of the dehydration tower or the inlet of a kettle of the dehydration tower and the reboiler of the dehydration tower;
the top of the dehydration tower is sequentially connected with a dehydration tower condenser and a dehydration tower reflux tank;
the reflux tank of the dehydration tower is connected with the dehydration tower;
the bottom of the dehydration tower is sequentially connected with a dehydration tower kettle circulating pump and a dehydration tower reboiler;
the outlet of the reboiler of the dehydration tower is connected with the dehydration tower; the reboiler of the dehydration tower is a shell-and-tube heat exchanger.
2. The apparatus for producing styrene by dehydration of phenethyl alcohol according to claim 1, wherein:
the dehydration tower reflux tank is a liquid-liquid separation tank, an organic phase extraction pipeline and a water phase extraction pipeline are arranged at the bottom of the dehydration tower reflux tank, and one branch of the water phase extraction pipeline is connected with the dehydration tower.
3. The apparatus for producing styrene by dehydrating phenethyl alcohol according to claim 1, wherein:
the internal parts of the dehydration tower are sieve plates, float valves, bubble caps or fillers.
4. A method for producing styrene by dehydrating phenethyl alcohol according to any one of claims 1 to 3, comprising:
the crude phenethyl alcohol raw material enters the device through a crude phenethyl alcohol feeding pipeline and a catalyst through a catalyst feeding pipeline, a water phase and an organic phase mainly containing styrene are obtained at the top of the tower after heating, dehydration reaction and separation, and heavy oil is extracted from the bottom of the tower.
5. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 4, comprising:
(a) feeding the crude phenethyl alcohol raw material into a dehydration tower kettle and/or an inlet of a reboiler of the dehydration tower, and feeding the catalyst into the dehydration tower kettle;
(b) the materials at the bottom of the dehydration tower are sent into a reboiler of the dehydration tower through a circulating pump at the bottom of the dehydration tower, and crude phenethyl alcohol is subjected to dehydration reaction in the reboiler under the action of a catalyst to obtain an outlet material flow of the reboiler of the dehydration tower containing styrene, acetophenone, phenethyl alcohol, water and heavy oil;
(c) rectifying and separating the material flow at the outlet of the reboiler of the dehydration tower through the dehydration tower, and condensing the tower top components through a condenser of the dehydration tower and then entering a reflux tank of the dehydration tower for settling and separation;
(d) respectively extracting a water phase and an organic phase rich in styrene and acetophenone from a reflux tank of the dehydration tower;
(e) the by-product containing heavy oil is extracted from the dehydration tower kettle.
6. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 4, wherein the organic phase is sent to a downstream facility for further refining and separation to obtain high-purity styrene, the water phase is divided into two paths, one path is refluxed to enter the dehydrating tower, and the other path is sent to the downstream facility for treatment.
7. The method for preparing styrene through phenylethanol dehydration of claim 4, wherein the reboiler of the dehydration tower adopts steam or hot oil as heat source.
8. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 4, wherein the operating conditions of the dehydration column include: the pressure is 10-100 kPaA, the operation temperature at the top of the tower is 40-120 ℃, and the number of tower plates is 2-20.
9. The method for producing styrene by dehydrating phenethyl alcohol according to claim 4, wherein the operating temperature of the reboiler of the dehydration column is not higher than the decomposition temperature of the liquid phase reaction medium.
10. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 9, wherein the operating temperature of the reboiler of the dehydration column is 160 to 280 ℃.
11. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 10, wherein the operating temperature of the reboiler of the dehydration column is 180 to 250 ℃.
12. The method for preparing styrene by dehydrating phenethyl alcohol according to claim 11, wherein the operating temperature of the reboiler of the dehydration column is 200 to 230 ℃.
13. The method for preparing styrene through phenylethanol dehydration according to claim 4, wherein said catalyst is selected from at least one of inorganic acid, organic acid, inorganic oxide and bisulfate.
14. The method for producing styrene through dehydration of phenethyl alcohol according to claim 13, wherein the catalyst is a sulfonic acid type sulfur-containing organic acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810779177.4A CN110724025B (en) | 2018-07-16 | 2018-07-16 | Device and method for preparing styrene by dehydrating phenethyl alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810779177.4A CN110724025B (en) | 2018-07-16 | 2018-07-16 | Device and method for preparing styrene by dehydrating phenethyl alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110724025A CN110724025A (en) | 2020-01-24 |
| CN110724025B true CN110724025B (en) | 2022-08-23 |
Family
ID=69217331
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810779177.4A Active CN110724025B (en) | 2018-07-16 | 2018-07-16 | Device and method for preparing styrene by dehydrating phenethyl alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110724025B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114573414A (en) * | 2020-12-01 | 2022-06-03 | 中国石化工程建设有限公司 | Device and method for removing light components in styrene monomer |
| CN114874066B (en) * | 2022-06-16 | 2023-07-21 | 上海优铖工逸技术有限公司 | Method and device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol |
| CN116966621A (en) * | 2023-09-12 | 2023-10-31 | 山西振钢生物科技股份有限公司 | Continuous rectifying device of sebacic acid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5519247A (en) * | 1978-07-28 | 1980-02-09 | Sumitomo Chem Co Ltd | Preparation of high-purity styrene by dehydration reaction of alpha-phenylethyl alcohol |
| RU35600U1 (en) * | 2003-08-18 | 2004-01-27 | Открытое акционерное общество "Нижнекамскнефтехим" | Installation for the production of styrene by liquid-phase dehydration of methylphenylcarbinol |
| RU2296114C1 (en) * | 2005-11-03 | 2007-03-27 | Открытое акционерное общество "Нижнекамскнефтехим" | Process of producing styrene via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock (options) |
-
2018
- 2018-07-16 CN CN201810779177.4A patent/CN110724025B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5519247A (en) * | 1978-07-28 | 1980-02-09 | Sumitomo Chem Co Ltd | Preparation of high-purity styrene by dehydration reaction of alpha-phenylethyl alcohol |
| RU35600U1 (en) * | 2003-08-18 | 2004-01-27 | Открытое акционерное общество "Нижнекамскнефтехим" | Installation for the production of styrene by liquid-phase dehydration of methylphenylcarbinol |
| RU2296114C1 (en) * | 2005-11-03 | 2007-03-27 | Открытое акционерное общество "Нижнекамскнефтехим" | Process of producing styrene via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock (options) |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110724025A (en) | 2020-01-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110724025B (en) | Device and method for preparing styrene by dehydrating phenethyl alcohol | |
| CN104387346B (en) | Prepared the method for furfural by pentose multiple stage continuous adverse current reaction, extraction | |
| CN103566613B (en) | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique | |
| KR20210050511A (en) | System and method for rapid extraction and purification of ethyl acetate after compression esterification synthesis | |
| CN106943764A (en) | The rectifier unit and method of a kind of cyclohexanone | |
| CN103055530A (en) | Solvent reinforced transformation thermal coupling rectification system for separating cyclohexanone and phenol | |
| CN106242970B (en) | A kind of device and method producing dimethyl adipate | |
| CN111689827B (en) | Device and method for preparing styrene | |
| CN101898930B (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN105801408A (en) | Reaction distillation device and method for producing high-purity n-butyl acrylate | |
| CN102225889A (en) | Method for preparing dimethyl ether by dehydration of methanol | |
| CN114105754B (en) | Organic sodium salt treatment process and device in toluene oxidation process | |
| CN215137001U (en) | Rectifying device for separating methyl ethyl ketone and sec-butyl alcohol | |
| CN105217654B (en) | Alkylation waste sulfuric acid recycling treatment device and method | |
| CN212610438U (en) | Tar distillation heat transfer device | |
| CN106866379B (en) | Method for preparing phenol acetone by CHP (CHP) through reactive distillation decomposition | |
| CN109776314B (en) | Preparation method of cinnamate | |
| CN103755515B (en) | A kind of toluene disproportionation produces benzene and the method for dimethylbenzene and equipment thereof | |
| CN101851152A (en) | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration | |
| CN204958761U (en) | Device of cinnamic acid separation benzaldehyde | |
| CN110787476A (en) | High-efficient reaction rectifier unit of n butyl acetate | |
| CN109852413A (en) | A kind of method of coal tar production modified coal tar pitch | |
| CN208591561U (en) | New benzene distillation system in a kind of caprolactam production | |
| AU2021105367A4 (en) | Device and Method for Shortening Ketalization Reaction Time of Ibuprofen Synthesis Process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20221019 Address after: 100101 building 21, Anyuan, Anhui Beili, Chaoyang District, Beijing Patentee after: SINOPEC ENGINEERING Inc. Patentee after: Wanhua Chemical Group Co.,Ltd. Patentee after: Sinopec Engineering (Group) Co.,Ltd. Address before: 100101 building 21, Anyuan, Anhui Beili, Chaoyang District, Beijing Patentee before: SINOPEC ENGINEERING Inc. Patentee before: Sinopec Engineering (Group) Co.,Ltd. |
|
| TR01 | Transfer of patent right |