CN106866379A - Reactive distillation decomposes the method that CHP prepares phenol-acetone - Google Patents
Reactive distillation decomposes the method that CHP prepares phenol-acetone Download PDFInfo
- Publication number
- CN106866379A CN106866379A CN201710178844.9A CN201710178844A CN106866379A CN 106866379 A CN106866379 A CN 106866379A CN 201710178844 A CN201710178844 A CN 201710178844A CN 106866379 A CN106866379 A CN 106866379A
- Authority
- CN
- China
- Prior art keywords
- reactive distillation
- acetone
- chp
- phenol
- distillation column
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/08—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by decomposition of hydroperoxides, e.g. cumene hydroperoxide
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
- C07C45/53—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition of hydroperoxides
-
- 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
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The method that CHP prepares phenol-acetone is decomposed the present invention relates to a kind of reactive distillation, mainly solves the problems, such as that product selectivity is relatively low in the prior art, it is larger to invest higher, floor space.The present invention decomposes the method that CHP prepares phenol-acetone by using a kind of reactive distillation, CHP raw materials feeding reactive distillation column containing 25~80wt% is carried out into decomposition reaction generation phenol-acetone, catalyst is in flow regime to keep high activity material gasification boiling using reaction heat；Carry out product acetone rectifying separation simultaneously, the selectivity of phenol brings up to 99.35~99.55%, the selectivity of acetone brings up to 99.25~99.45%, and the technical scheme of product acetone purity >=99.9wt% preferably solves above mentioned problem, can be used in phenol-acetone production.
Description
Technical field
The method that CHP prepares phenol-acetone is decomposed the present invention relates to a kind of reactive distillation.
Background technology
Phenol and acetone are widely used basic organic chemical industry raw materials, and domestic and international market demand is very vigorous.Production benzene
The phenol-acetone device of phenol acetone prepares cumyl hydroperoxide using isopropyl benzene raw materials and air in oxidation reaction tower first
CHP, then CHP is carried out decomposition reaction generation phenol and acetone under catalyst action, is carried finally by rectifying separation and purification
It is pure to obtain phenol product and product acetone.
Number of patent application CN201210512571.4 of the prior art is used for the novel reaction essence that phenol and acetone are produced
Technique is evaporated, is disclosed and is decomposed CHP, isopropylbenzene is separated, in three PROCESS COUPLINGs of phenol crude separation a to rectifying column, so as to carry
Utilization of Heat of Reaction rate high.A kind of cumyl hydroperoxides of number of patent application CN201410337795.5 decompose the side of phynol/acetone
Method, discloses and uses with fine grain solid acid as catalyst, using multipoles reactors, by controlling reaction temperature, catalysis
Agent consumption, residence time and then control conversion ratio and the method for temperature rise prepare phenol-acetone.Number of patent application
A kind of reactive distillation methods for producing methyl chloroacetate of CN201510026002.2, disclose and use reactive distillation column, enter promoting the circulation of qi
Liquid solid phase reaction, thus flow is simple, and investment reduction, energy consumption reduction, high conversion rate, selectivity is also high.Number of patent application
The method that CN201510654488.4 prepares phenol-acetone using moving-burden bed reactor, discloses CHP raw materials anti-into moving bed
Answer device top, contact with solid catalyst decompose reaction and it is highly exothermic, by liquid phase acetone evaporated for gas phase acetone and from
The method of moving-burden bed reactor top discharge is improving the selectivity of phenol and acetone.
In the prior art, number of patent application CN201210512571.4 is only the side that laboratory scale prepares phenol-acetone
There is the problems such as number of devices is more, and construction investment is high, floor space is big, it is necessary to set 2 rectifying tower systems in method；And, big
During technical scale application, there are problems that " enlarge-effect "；Meanwhile, liquid phase isopropylbenzene enters reactor, isopropylbenzene elder generation together with CHP
Flowed out from reactive distillation column top gaseous phase after gasification, then there is high energy consumption from the outflow of ketone fractionator tower reactor liquid phase after condensing
Problem.There is consersion unit floor space greatly in number of patent application CN201410337795.5, control process is complicated, especially reacts
Later stage, catalyst activity reduction, the selectivity of phenol-acetone further declines, and accessory substance increases, and major product yield declines etc.
Problem.Number of patent application CN201510026002.2 is only the method for producing methyl chloroacetate product, tower reactor heating-up temperature 100
~140 DEG C, it is impossible to prepare phenol-acetone product.Number of patent application 201510654488.4 is gasified-is condensed and removed instead by acetone
Should be hot, acetone is used only for diabatic process, and liquid phase acetone flows out from reactor tower reactor, is unfavorable for that CHP decomposition reactions generate phenol
Product acetone, similarly there are the problems such as number of devices is more, and construction investment is high, floor space is big.
The content of the invention
The technical problems to be solved by the invention are that product selectivity is relatively low in the prior art, invest higher, floor space
Larger problem, there is provided a kind of new reactive distillation decomposes the method that CHP prepares phenol-acetone.The method has product selectivity
Higher, the investment less advantage of relatively low, floor space.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of reactive distillation decomposes CHP and prepares phenol third
The method of ketone, cumyl hydroperoxide CHP raw materials (11) enters reactive distillation column (1), enters under reactive distillation column (1) with gravity stream
The conversion zone in portion is contacted with solid catalyst, and CHP decomposition reactions generation phenol-acetone occurs and a large amount of reaction heat are produced, will all
Liquid phase acetone and a small amount of raw material CHP and a small amount of isopropylbenzene are evaporated to gas phase and are discharged from conversion zone top, the liquid without acetone
Phase materials are drawn from reactive distillation column (1) reaction pars infrasegmentalis, are exchanged heat and are removed with recirculated cooling water in intercooler
Decomposition reaction heat, reactive distillation column (1) tower reactor outflow liquid phase phenol product and unreacted raw material CHP and isopropylbenzene (15)；
The rectifying section for entering reactive distillation column (1) top from the gaseous phase materials of reactive distillation column (1) conversion zone discharge carries out gas-liquid contact,
In reactive distillation column (1), tower top obtains high-purity acetone material (12), is condensed by overhead condenser (2), a part of liquid phase third
Ketone is sent outside as product (14), and another part liquid phase acetone returns to reactive distillation column (1) to keep rectifying as phegma (13)
The gas-liquid contact of section.
In above-mentioned technical proposal, it is preferable that catalyst is resin catalyst, using macropore styrene ion exchange resin
Polymerization process, adds (methyl) fluoroalkyl base esters monomer and phenol to participate in polymerization, then it is sulfonated prepare, its
In, (methyl) fluoroalkyl base esters monomer is hexafluorobutyl acrylate, dodecafluorhe-ptylacrylate and/or acrylic acid 13
Fluorine monooctyl ester.
In above-mentioned technical proposal, it is preferable that the technological parameter of reactive distillation column conversion zone is：Operation temperature is 75~100
DEG C, operating pressure is 110~195kPaA, and reactive distillation column conversion zone device parameter is：Draw ratio is 16：1, conversion zone is built-in
Fill out n sections of solid catalyst bed, wherein n=1~12.
In above-mentioned technical proposal, it is highly preferred that the technological parameter of reactive distillation column conversion zone is：Operation temperature is 80~95
DEG C, operating pressure is 125~180kPaA, and reactive distillation column conversion zone device parameter is：Draw ratio is 6：1, filling in conversion zone
N sections of solid catalyst bed, wherein n=2~11.
In above-mentioned technical proposal, most preferably, the technological parameter of reactive distillation column conversion zone is：Operation temperature for 85~
90℃；Operating pressure is 140~165kPaA；Reactive distillation column conversion zone device parameter is：Draw ratio is 2：1；Conversion zone is built-in
Fill out n sections of solid catalyst bed, wherein n=2~10.
In above-mentioned technical proposal, it is preferable that the technological parameter of reactive distillation column rectifying section is：Operation temperature is 45~70
DEG C, operating pressure be 68~156kPaA, reflux ratio 0.55~0.95, rectifiying plate quantity be 40~48 pieces, charging Board position from
On down the 38th~46 block of column plate.
In above-mentioned technical proposal, it is highly preferred that the technological parameter of reactive distillation column rectifying section is：Operation temperature is 50~65
DEG C, operating pressure is 83~141kPaA.
In above-mentioned technical proposal, most preferably, the technological parameter of reactive distillation column rectifying section is：Operation temperature is 55~60
℃；Operating pressure is 98~126kPaA.
In above-mentioned technical proposal, it is preferable that every section of beds of reactive distillation column conversion zone are provided with and catalyst
The passage that regenerative system is connected with each other, the catalyst of flow regime can realize on-line regeneration and online replacing.
The present invention is anti-by the CHP raw materials feeding containing 25~80wt% on large-scale commercial phenol-acetone process units
Answering rectifying column carries out decomposition reaction generation phenol-acetone, catalyst is in flow regime material gasification boiling using reaction heat
To keep high activity；Carry out product acetone rectifying separation simultaneously.Thus, the selectivity of phenol brings up to 99.35~99.55%,
The selectivity of acetone brings up to 99.25~99.45%, and product acetone purity >=99.9wt% achieves preferable technique effect.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1. reactive distillation column, 2. overhead condenser, 3. intercooler, 4. intercooler, 5. cooling during rolling
Device, 11. liquid phase CHP raw materials, 12. gas phase tower top acetone, 13. liquid phase acetone reflux liquid, 14. liquid phase product acetones, 15. liquid phase towers
Kettle material.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Comparative example 1】
Prior art phenol-acetone process units carries out decomposition reaction generation benzene first by CHP raw materials under catalyst action
Phenol and acetone, are then purified by rectifying separation and purification and obtain phenol product and product acetone.Thus, it is desirable to set CHP decomposition
2 equipment of reactor and ketone fractionator, number of devices is more, and construction investment is high, and floor space is big.
【Embodiment 1】
A kind of reactive distillation decomposes the method that CHP prepares phenol-acetone, as shown in figure 1, to load 3 sections of solid catalyst beds
Layer as a example by, cumyl hydroperoxide CHP raw materials (11) from middle part enter reactive distillation column (1), with gravity stream enter conversion zone with
Solid catalyst is contacted, and CHP decomposition reactions generation phenol-acetone occurs and a large amount of reaction heat are produced, by whole liquid phase acetone and less
Content of starting materials CHP and a small amount of isopropylbenzene are evaporated to gas phase and are discharged from conversion zone top；Liquid phase material without acetone is from reaction
Rectifying column (1) reaction pars infrasegmentalis is drawn, in intercooler (3), intercooler (4), in intercooler (5), with circulation
Cooling water is exchanged heat and is removed decomposition reaction heat, and reactive distillation column (1) tower reactor flows out liquid phase phenol product and unreacted original
Material CHP and isopropylbenzene (15).Enter reactive distillation column (1) rectifying from the gaseous phase materials of reactive distillation column (1) conversion zone discharge
Duan Jinhang gas-liquid contacts, material is separated in this mass transfer, and the content of acetone in gaseous phase materials is stepped up, in reactive distillation column (1)
Tower top obtains high-purity acetone material (12), by overhead condenser (2) condense, a part of liquid phase acetone as product (14) outward
Send, another part liquid phase acetone returns to reactive distillation column (1) to keep the gas-liquid contact of rectifying section as phegma (13).
By taking 100,000 tons/year of phenol-acetone devices of production scale as an example, CHP is decomposed using reactive distillation of the present invention and prepares phenol
The method of acetone, the rectifying column of the moving-burden bed reactor of filling solid catalyst and separation of material is united two into one anti-as one
Rectifying column (1) is answered, so as to reduce number of devices, construction investment is reduced, floor space is reduced.
Cumyl hydroperoxide CHP raw materials (11) from middle part enter reactive distillation column (1) with gravity stream enter conversion zone with
Catalyst contact reacts and generates phenol-acetone and produce reaction heat to steam whole acetone and a small amount of CHP and a small amount of isopropylbenzene
Send out as gas phase and discharged from conversion zone top；Liquid phase material without acetone is drawn from reaction pars infrasegmentalis, in intercooler,
Reaction heat, the outflow of reactive distillation column tower reactor liquid phase phenol product and unreacted CHP are exchanged heat and removed with recirculated cooling water
And isopropylbenzene (15).Enter rectifying section from the gaseous phase materials of conversion zone discharge, material is separated in this mass transfer, in gaseous phase materials
Content of acetone is stepped up, and high-purity acetone material (12) is obtained in reactive distillation column overhead, cold by overhead condenser (2)
Solidifying, a part of acetone is sent outside as product (14), and another part acetone returns to reactive distillation column as phegma (13).CHP is former
Material composition is as follows：
Technological parameter is：The operation temperature of reactive distillation column conversion zone is 82 DEG C, and operating pressure is 132kPaA；Reactor
Draw ratio be 6：1,4 sections of catalyst of filling in reactor.Catalyst is resin catalyst, is handed over using macropore polystyrene ion
Resin polymerization production technology is changed, adds (methyl) fluoroalkyl base esters monomer and phenol to participate in polymerization, then sulfonated preparation
Obtain, wherein：(methyl) fluoroalkyl base esters monomer is hexafluorobutyl acrylate.The operation temperature of reactive distillation column rectifying section
It is 53 DEG C to spend, and operating pressure is 98kPaA, reflux ratio 0.71；Rectifiying plate quantity is 46 pieces, charging Board position from top to bottom the
44 blocks of column plates.
Thus, the selectivity of phenol is 99.50%, and the selectivity of acetone is 99.35%, product acetone purity
99.91wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 75%, floor space
Drop to 50%.
【Embodiment 2】
According to condition and step described in embodiment 1, simply the production scale of phenol-acetone device is changed to 200,000 tons/year,
The method that CHP prepares phenol-acetone is decomposed using reactive distillation of the present invention, technological parameter is：The operation of reactive distillation column conversion zone
Temperature is 82 DEG C, and operating pressure is 132kPaA；The draw ratio of reactor is 6：1,4 sections of catalyst of filling in reactor.Reaction essence
The operation temperature of tower rectifying section is evaporated for 53 DEG C, and operating pressure is 98kPaA, reflux ratio 0.71；Rectifiying plate quantity is 46 pieces, is entered
Flitch position the 44th block of column plate from top to bottom.
Thus, the selectivity of phenol is 99.50%, and the selectivity of acetone is 99.35%, product acetone purity
99.91wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 74%, floor space
Drop to 50%.
【Embodiment 3】
According to condition and step described in embodiment 1, simply the production scale of phenol-acetone device is changed to 350,000 tons/year,
The method that CHP prepares phenol-acetone is decomposed using reactive distillation of the present invention, technological parameter is：The operation of reactive distillation column conversion zone
Temperature is 82 DEG C, and operating pressure is 132kPaA；The draw ratio of reactor is 6：1,4 sections of catalyst of filling in reactor.Reaction essence
The operation temperature of tower rectifying section is evaporated for 53 DEG C, and operating pressure is 98kPaA, reflux ratio 0.71；Rectifiying plate quantity is 46 pieces, is entered
Flitch position the 44th block of column plate from top to bottom.
Thus, the selectivity of phenol is 99.45%, and the selectivity of acetone is 99.30%, product acetone purity
99.91wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 72%, floor space
Drop to 50%.
【Embodiment 4】
According to condition and step described in embodiment 1, simply the production scale of phenol-acetone device is changed to 400,000 tons/year,
The method that CHP prepares phenol-acetone is decomposed using reactive distillation of the present invention, technological parameter is：The operation of reactive distillation column conversion zone
Temperature is 82 DEG C, and operating pressure is 132kPaA；The draw ratio of reactor is 6：1,4 sections of catalyst of filling in reactor.Reaction essence
The operation temperature of tower rectifying section is evaporated for 53 DEG C, and operating pressure is 98kPaA, reflux ratio 0.71；Rectifiying plate quantity is 46 pieces, is entered
Flitch position the 44th block of column plate from top to bottom.
Thus, the selectivity of phenol is 99.45%, and the selectivity of acetone is 99.30%, product acetone purity
99.91wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 72%, floor space
Drop to 50%.
【Embodiment 5】
According to condition and step described in embodiment 1, simply the production scale of phenol-acetone device is changed to 600,000 tons/year,
The method that CHP prepares phenol-acetone is decomposed using reactive distillation of the present invention, technological parameter is：The operation of reactive distillation column conversion zone
Temperature is 82 DEG C, and operating pressure is 132kPaA；The draw ratio of reactor is 6：1,4 sections of catalyst of filling in reactor.Reaction essence
The operation temperature of tower rectifying section is evaporated for 53 DEG C, and operating pressure is 98kPaA, reflux ratio 0.71；Rectifiying plate quantity is 46 pieces, is entered
Flitch position the 44th block of column plate from top to bottom.
Thus, the selectivity of phenol is 99.45%, and the selectivity of acetone is 99.30%, product acetone purity
99.91wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 70%, floor space
Drop to 50%.
【Embodiment 6】
According to condition and step described in embodiment 3, the production scale of phenol-acetone device is still 350,000 tons/year, simply
Process condition changes, and the method that CHP prepares phenol-acetone, CHP raw material groups are decomposed using invention reactive distillation
Into as follows：
Technological parameter is：The operation temperature of reactive distillation column conversion zone is 75 DEG C, and operating pressure is 110kPaA；Reactor
Draw ratio be 2：1,1 section of catalyst of filling in reactor.Catalyst is resin catalyst, is handed over using macropore polystyrene ion
Resin polymerization production technology is changed, adds (methyl) fluoroalkyl base esters monomer and phenol to participate in polymerization, then sulfonated preparation
Obtain；Wherein：(methyl) fluoroalkyl base esters monomer is dodecafluorhe-ptylacrylate.The operation of reactive distillation column rectifying section
Temperature is 45 DEG C, and operating pressure is 68kPaA, reflux ratio 0.55；Rectifiying plate quantity is 48 pieces, and charging Board position is from top to bottom
46th block of column plate.
Thus, the selectivity of phenol is 99.35%, and the selectivity of acetone is 99.25%, product acetone purity
99.92wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 73%, floor space
Drop to 50%.
【Embodiment 7】
According to condition and step described in embodiment 3, the production scale of phenol-acetone device is still 350,000 tons/year, simply
Process condition changes, and the method that CHP prepares phenol-acetone, CHP raw material groups are decomposed using invention reactive distillation
Into as follows：
Technological parameter is：The operation temperature of reactive distillation column conversion zone is 100 DEG C, and operating pressure is 195kPaA；Reactor
Draw ratio be 16：1,12 sections of catalyst of filling in reactor.Catalyst is resin catalyst, using macropore polystyrene ion
Exchanger resin polymerization process, adds (methyl) fluoroalkyl base esters monomer and phenol to participate in polymerization, then sulfonated system
It is standby to obtain；Wherein：(methyl) fluoroalkyl base esters monomer is perluorooctyl acrylate.The behaviour of reactive distillation column rectifying section
Make temperature for 70 DEG C, operating pressure is 156kPaA, reflux ratio 0.95；Rectifiying plate quantity is 40 pieces, and charging Board position is from upper past
Lower 38th block of column plate.
Thus, the selectivity of phenol is 99.55%, and the selectivity of acetone is 99.45%, product acetone purity
99.92wt%.With【Comparative example 1】Compare, number of devices is reduced to 1 from 2, and construction investment is reduced to 73%, floor space
Drop to 50%.
Claims (9)
1. a kind of reactive distillation decomposes the method that CHP prepares phenol-acetone, and cumyl hydroperoxide CHP raw materials (11) enters reaction essence
Tower (1) is evaporated, the conversion zone for entering reactive distillation column (1) bottom with gravity stream is contacted with solid catalyst, CHP decomposition reactions occur
Generate phenol and acetone and produce a large amount of reaction heat, by whole liquid phase acetone and a small amount of raw material CHP and the evaporation of a small amount of isopropylbenzene
For gas phase and from the discharge of conversion zone top, the liquid phase material without acetone is drawn from reactive distillation column (1) reaction pars infrasegmentalis, in
Between exchanged heat with recirculated cooling water in cooler and removed decomposition reaction heat, reactive distillation column (1) tower reactor outflow liquid phase phenol
Product and unreacted raw material CHP and isopropylbenzene (15)；Enter anti-from the gaseous phase materials of reactive distillation column (1) conversion zone discharge
Answering the rectifying section on rectifying column (1) top carries out gas-liquid contact, and in reactive distillation column (1), tower top obtains high-purity acetone material
(12), condensed by overhead condenser (2), a part of liquid phase acetone is sent outside as product (14), another part liquid phase acetone is made
Return to reactive distillation column (1) to keep the gas-liquid contact of rectifying section for phegma (13).
2. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 1, it is characterised in that catalyst is tree
Fat catalyst, using macropore styrene ion exchange resin polymerization process, adds (methyl) fluoroalkyl base ester class
Monomer and phenol participate in polymerization, then it is sulfonated prepare, wherein, (methyl) fluoroalkyl base esters monomer is acrylic acid six
Fluorine butyl ester, dodecafluorhe-ptylacrylate and/or perluorooctyl acrylate.
3. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 1, it is characterised in that reactive distillation column
The technological parameter of conversion zone is：Operation temperature is 75~100 DEG C, and operating pressure is 110~195kPaA, reactive distillation column reaction
Section device parameter be：Draw ratio is 16：1, n sections of solid catalyst bed of filling, wherein n=1~12 in conversion zone.
4. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 3, it is characterised in that reactive distillation column
The technological parameter of conversion zone is：Operation temperature is 80~95 DEG C, and operating pressure is 125~180kPaA, reactive distillation column conversion zone
Device parameter is：Draw ratio is 6：1, n sections of solid catalyst bed of filling, wherein n=2~11 in conversion zone.
5. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 4, it is characterised in that reactive distillation column
The technological parameter of conversion zone is：Operation temperature is 85~90 DEG C；Operating pressure is 140~165kPaA；Reactive distillation column reacts
Section device parameter be：Draw ratio is 2：1；N sections of solid catalyst bed of filling, wherein n=2~10 in conversion zone.
6. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 1, it is characterised in that reactive distillation column
The technological parameter of rectifying section is：Operation temperature be 45~70 DEG C, operating pressure be 68~156kPaA, reflux ratio 0.55~0.95,
Rectifiying plate quantity is 40~48 pieces, feeds Board position the 38th~46 block of column plate from top to bottom.
7. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 6, it is characterised in that reactive distillation column
The technological parameter of rectifying section is：Operation temperature is 50~65 DEG C, and operating pressure is 83~141kPaA.
8. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 7, it is characterised in that reactive distillation column
The technological parameter of rectifying section is：Operation temperature is 55~60 DEG C；Operating pressure is 98~126kPaA.
9. reactive distillation decomposes the method that CHP prepares phenol-acetone according to claim 1, it is characterised in that reactive distillation column
Every section of beds of conversion zone are provided with the passage being connected with each other with catalyst regeneration system, the catalyst energy of flow regime
Enough realize on-line regeneration and online replacing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710178844.9A CN106866379B (en) | 2017-03-23 | 2017-03-23 | Method for preparing phenol acetone by CHP (CHP) through reactive distillation decomposition |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710178844.9A CN106866379B (en) | 2017-03-23 | 2017-03-23 | Method for preparing phenol acetone by CHP (CHP) through reactive distillation decomposition |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106866379A true CN106866379A (en) | 2017-06-20 |
| CN106866379B CN106866379B (en) | 2020-11-10 |
Family
ID=59172010
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710178844.9A Active CN106866379B (en) | 2017-03-23 | 2017-03-23 | Method for preparing phenol acetone by CHP (CHP) through reactive distillation decomposition |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106866379B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109534952A (en) * | 2018-12-17 | 2019-03-29 | 实友化工（扬州）有限公司 | A kind of phenol preparation method can reduce by-product tar yield |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020058845A1 (en) * | 1999-12-21 | 2002-05-16 | Doron Levin | Production of phenol using reactive distillation |
| CN101027269A (en) * | 2004-07-27 | 2007-08-29 | Abb路慕斯全球股份有限公司 | Process for the selective hydrogenation of alkynes and/or dienes in an olefin-containing hydrocarbon stream |
| CN101342497A (en) * | 2008-08-15 | 2009-01-14 | 厦门大学 | Catalyst for preparing phenol with catalysis distillation and method for preparing phenol |
| CN102698801A (en) * | 2012-06-01 | 2012-10-03 | 凯瑞化工股份有限公司 | Resin catalyst applied to preparation of phenol through decomposition of cumene hydroperoxide (CHP) and preparation method for resin catalyst |
| CN102992961A (en) * | 2012-11-28 | 2013-03-27 | 沙丽 | Novel reactive distillation technology for producing phenol and acetone |
| CN105218304A (en) * | 2015-10-12 | 2016-01-06 | 中石化上海工程有限公司 | Moving-burden bed reactor is adopted to prepare the method for phenol-acetone |
-
2017
- 2017-03-23 CN CN201710178844.9A patent/CN106866379B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020058845A1 (en) * | 1999-12-21 | 2002-05-16 | Doron Levin | Production of phenol using reactive distillation |
| CN101027269A (en) * | 2004-07-27 | 2007-08-29 | Abb路慕斯全球股份有限公司 | Process for the selective hydrogenation of alkynes and/or dienes in an olefin-containing hydrocarbon stream |
| CN101342497A (en) * | 2008-08-15 | 2009-01-14 | 厦门大学 | Catalyst for preparing phenol with catalysis distillation and method for preparing phenol |
| CN102698801A (en) * | 2012-06-01 | 2012-10-03 | 凯瑞化工股份有限公司 | Resin catalyst applied to preparation of phenol through decomposition of cumene hydroperoxide (CHP) and preparation method for resin catalyst |
| CN102992961A (en) * | 2012-11-28 | 2013-03-27 | 沙丽 | Novel reactive distillation technology for producing phenol and acetone |
| CN105218304A (en) * | 2015-10-12 | 2016-01-06 | 中石化上海工程有限公司 | Moving-burden bed reactor is adopted to prepare the method for phenol-acetone |
Non-Patent Citations (1)
| Title |
|---|
| 周道伟等: ""过氧化氢异丙苯分解制苯酚的反应精馏工艺"", 《厦门大学学报（自然科学版）》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109534952A (en) * | 2018-12-17 | 2019-03-29 | 实友化工（扬州）有限公司 | A kind of phenol preparation method can reduce by-product tar yield |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106866379B (en) | 2020-11-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109456190A (en) | A kind of method of the continuous synthesizing propylene glycol monomethyl ether acetate of the highly selective catalytic distillation of low temperature | |
| CN101967133B (en) | Process for preparing furan through decarbonylation of furfural | |
| CN101255109A (en) | Process for producing acrylic acid by dehydrating biomass lactic acid | |
| KR20240095299A (en) | Maleic anhydride hydrogenation method and succinic acid production method comprising the same | |
| CN109134217B (en) | Oxidation device and oxidation process improvement method in cyclohexanone production process by cyclohexane oxidation method | |
| CN105461515A (en) | Method for preparing cyclopentanol from cyclopentene | |
| CN109438196B (en) | Method for preparing 2, 2-dimethoxypropane | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN106866379A (en) | Reactive distillation decomposes the method that CHP prepares phenol-acetone | |
| CN109721469A (en) | A kind of preparation method of cyclopentanone | |
| CN101074187B (en) | Production of o-phenylphenol | |
| CN216404259U (en) | System for continuously preparing acetophenone | |
| CN102603486A (en) | Method for preparing cyclopentanol from cyclopentene | |
| CN115677461A (en) | Method for continuously producing 4-oxoisophorone by using tower reactor | |
| CN102268307A (en) | Method for producing synthetic natural gas by using methanol exhaust gas | |
| CN114349589B (en) | Method for preparing p-methyl ethylbenzene by using toluene and ethylene | |
| CN101260093B (en) | Modified epoxy ethane washing technique for epoxy ethane/ethylene glycol producing device | |
| CN105218304B (en) | The method that phenol-acetone is prepared using moving-burden bed reactor | |
| CN208907089U (en) | Oxidation unit during a kind of cyclohexane oxidation process production cyclohexanone | |
| CN1032813C (en) | Prepn. of formaldehyde with low energy consumption | |
| CN102179059A (en) | Hydrolysis separation device of methyl acetate and process method thereof | |
| CN113149810A (en) | Reactive distillation system and method for preparing cyclohexanol by cyclohexene hydration | |
| CN102826965B (en) | Process and device for producing dimethyl ether by gas-phase catalytic dehydration of methanol | |
| CN218901792U (en) | Synthesizer for preparing methanol by carbon dioxide hydrogenation | |
| CN113277924B (en) | Heat exchange system for propylene preparation |
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 |