CN111285752A - Multistage heat exchange reaction system for chloropropene production - Google Patents
Multistage heat exchange reaction system for chloropropene production Download PDFInfo
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- CN111285752A CN111285752A CN202010208268.XA CN202010208268A CN111285752A CN 111285752 A CN111285752 A CN 111285752A CN 202010208268 A CN202010208268 A CN 202010208268A CN 111285752 A CN111285752 A CN 111285752A
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- Prior art keywords
- propylene
- reaction system
- reactor
- heat
- heat exchange
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Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 54
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 59
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 59
- 238000000034 method Methods 0.000 claims abstract description 14
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 7
- 239000000460 chlorine Substances 0.000 claims abstract description 7
- 239000000376 reactant Substances 0.000 claims abstract description 3
- 230000001105 regulatory effect Effects 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 239000003507 refrigerant Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 238000005660 chlorination reaction Methods 0.000 description 3
- OSDWBNJEKMUWAV-UHFFFAOYSA-N Allyl chloride Chemical compound ClCC=C OSDWBNJEKMUWAV-UHFFFAOYSA-N 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- 235000013599 spices Nutrition 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 1
- -1 allyl carbinol ketone Chemical class 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- IRUJZVNXZWPBMU-UHFFFAOYSA-N cartap Chemical compound NC(=O)SCC(N(C)C)CSC(N)=O IRUJZVNXZWPBMU-UHFFFAOYSA-N 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- GBCKRQRXNXQQPW-UHFFFAOYSA-N n,n-dimethylprop-2-en-1-amine Chemical compound CN(C)CC=C GBCKRQRXNXQQPW-UHFFFAOYSA-N 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- QSOHVSNIQHGFJU-UHFFFAOYSA-L thiosultap disodium Chemical compound [Na+].[Na+].[O-]S(=O)(=O)SCC(N(C)C)CSS([O-])(=O)=O QSOHVSNIQHGFJU-UHFFFAOYSA-L 0.000 description 1
- MBNMHBAJUNHZRE-UHFFFAOYSA-M thiosultap monosodium Chemical compound [Na+].OS(=O)(=O)SCC(N(C)C)CSS([O-])(=O)=O MBNMHBAJUNHZRE-UHFFFAOYSA-M 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/10—Preparation of halogenated hydrocarbons by replacement by halogens of hydrogen atoms
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a multistage heat exchange reaction system for producing chloropropene, which comprises a reactor and a plurality of heat exchangers, the reactor and the heat exchanger are connected by pipelines, a flow regulating valve is arranged in the pipeline, the reactants in the reactor are propylene and chlorine, the propylene exchanges heat with the reaction distillate before entering the reactor, the invention fully utilizes the heat generated by the chloropropene reaction through multi-stage heat exchange so that the heat can be recycled in a reaction system for multiple times, and various process designs in the reaction system meet the process conditions of heat recycling, the recycling rate of water and heat conducting oil in the reaction system is improved, and the reaction system is energy-saving, environment-friendly and efficient.
Description
Technical Field
The invention belongs to the technical field of chloropropene production reaction, and particularly relates to a multistage heat exchange reaction system for chloropropene production.
Background
Chloropropene, a chemical, a colorless liquid, is an organic synthetic raw material. Can be used as an intermediate for producing epoxy chloropropane, allyl alcohol, glycerol and the like, is used as a solvent for special reaction, and is also a raw material of pesticide, medicine, spice and paint. The 3-chloropropene, also known as allyl chloride, is an organic synthetic raw material, is used for synthesizing N, N-dimethylallylamine and an allyl carbinol ketone intermediate of monosultap, dimehypo and cartap in pesticides, and is also an important raw material for medicines, synthetic resins, coatings, spices and the like.
The method for preparing chloropropene comprises the following steps: the high-temperature chlorination method, the propylene oxychlorination method and the allyl alcohol chlorination method have the advantages that the heat generated by the chloropropene reaction in the method for preparing the chloropropene is large, the generated heat is reasonably utilized, and the heat exchange temperature of each stage is accurately mastered to greatly influence the heat consumption of the whole system and the product quality.
Disclosure of Invention
In order to reasonably utilize the heat generated by the chloropropene reaction and correctly grasp the heat consumption of the whole system by the heat exchange temperature of each stage, a multistage heat exchange reaction system for producing chloropropene is provided.
The utility model provides a chloropropene production is with multistage heat transfer reaction system, reaction system includes reactor and a plurality of heat exchanger, link to each other by the pipeline between reactor and the heat exchanger and between heat exchanger and the heat exchanger, install flow control valve in the pipeline, the reactant in the reactor is propylene and chlorine, propylene carries out heat exchange with the reaction distillate before getting into the reactor, preheats the propylene that gets into the reactor, the reaction distillate gets into subsequent handling after tertiary cooling.
Further, the propylene is divided into three branches, and enters the reactor through four-stage preheating, wherein the three branches comprise a first branch, a second branch and a third branch.
Further, the preheaters used for the four-stage preheating comprise a primary propylene evaporator, a secondary propylene evaporator, a tertiary propylene preheater and a distillate cooler.
Furthermore, the first branch and the third branch enter the reactor after exchanging heat with the reaction distillate, and the second branch is used as the tower top refrigerant and reflux liquid of the prefractionator.
Further, the cooler for the third stage cooling in the tertiary cooling of the reaction distillate is a primary propylene evaporator.
Further, the cooler for the first stage cooling in the tertiary cooling of the reaction distillate is a reaction distillate cooler.
Furthermore, the heat sources of the secondary propylene evaporator and the tertiary propylene preheater are heating media.
Furthermore, the heat medium is heat conducting oil, and the heat conducting oil enters the reaction system from the heat oil receiving groove.
Compared with the prior art, the invention has the advantages and the technical effects that: according to the invention, through multi-stage heat exchange, heat generated by chloropropene reaction is fully utilized, so that the heat can be recycled in the reaction system for multiple times, and various process designs in the reaction system meet the process conditions of heat recycling, so that the recycling rate of water and heat conducting oil in the reaction system is improved, and the method is energy-saving, environment-friendly and efficient.
Drawings
FIG. 1 is a flow chart of a multistage heat exchange reaction process for producing chloropropene.
In the figure: VE-1103, propylene feed tank, VE-1108, chlorine entrainment separator, VE-1109, gas separator, VE-1111, expansion tank, VE-1112, hot oil receiving tank, VE-1114, propylene entrainment separator, VE-1113, steam separator, HE-1115, heat medium cooler, RE-1101, reactor, PU-1104E, hot oil pump, HE-1107, distillate cooler, HE-1108, distillate secondary cooler, HE-1109, tertiary propylene preheater, HE-1111, secondary propylene evaporator, HE-1110, primary propylene evaporator, HE-1112 and overhead heat exchanger. HE-1113, a distillate cooler, TW-1101, a prefractionating column, HE-1114 and a prefractionating column reboiler;
Detailed Description
The technical solution of the present invention will be described in further detail with reference to the accompanying drawings and the detailed description.
Example 1
A multistage heat exchange reaction system for chloropropene production comprises a reactor and a plurality of heat exchangers, wherein chlorine and propylene react in the reactor, the chlorine and propylene react to generate exothermic reaction, huge heat is generated at the outlet of the reactor, reaction distillate is subjected to first heat exchange cooling to 235-335 ℃ in a distillate cooler HE-1107, is subjected to second heat exchange cooling to 155-165 ℃ with a heating medium through a distillate secondary cooler HE-1108, is subjected to buffer separation in a gas separator VE-1109, enters a first-stage propylene evaporator HE-1110 to perform third heat exchange with propylene, is cooled to 25-35 ℃, and enters a subsequent treatment process.
The heat medium is heat conducting oil shown in the attached drawing, the heat conducting oil enters the reaction system from a hot oil receiving groove VE-1112, and is divided into two branches through flow control, one branch is heated and cooled to 125-135 ℃ through a secondary propylene evaporator HE-1111 and then is combined with the other branch to return to a heat medium expansion groove VE-1111 for expansion, the other branch is heated through a tertiary propylene preheater HE-1109, and the temperature of the two branches is 140-150 ℃ after the two branches are combined. After the heat medium is expanded by the expansion groove VE-1111, the heat medium is heated in a heat medium cooler HE-1115 to warm water at 85-95 ℃ to generate low-pressure steam at 125-130 ℃ for subsequent processes.
Before the propylene enters the reactor, preheating treatment is carried out, and specifically comprises the following steps: the propylene from the outside at the temperature of 8-12 ℃ is divided into three branches and enters a reactor through four-stage preheating, the preheaters used for the four-stage preheating comprise a first-stage propylene evaporator HE-1110, a second-stage propylene evaporator HE-1111, a third-stage propylene preheater HE-1109 and a distillate cooler HE-1107, the three branches comprise a first branch, a second branch and a third branch, the first branch and the third branch enter the reactor after heat exchange with reaction distillates, and the second branch is used as a tower top refrigerant and reflux liquid of a prefractionator. After the pressure of the first branch propylene is reduced to 0.12-0.14 MPaG, carrying out first heat exchange with a reaction distillate in a first-stage propylene evaporator HE-1110, and vaporizing liquid propylene into gas-phase propylene; and then, carrying out secondary heat exchange on gas-phase propylene and a heat medium in a secondary propylene evaporator HE-1111, heating the propylene to 16-24 ℃, buffering and defoaming the propylene by a propylene entrainment separator VE-1114, mixing the propylene with a third branch circuit, carrying out proportional flow regulation on the propylene and chlorine by a flow regulating valve, carrying out tertiary heat exchange with the heat medium in a tertiary propylene preheater HE-1109 to 70-75 ℃, carrying out fourth heat exchange on the propylene and a reaction distillate in a reaction distillate cooler HE-1107, and then feeding the propylene into a reactor RE-1101 after the temperature reaches 260-280 ℃.
The second branch propylene enters the top of a prefractionating tower TW-1101 as a refrigerant and reflux under 0.12-0.14 MPaG through pressure reduction regulation, the top of the prefractionating tower TW-1101 is connected with a top heat exchanger HE-1112, the top heat exchanger HE-1112 can use the top steam of the prefractionating tower as a heat source for prefractionating crude chloropropene, the crude chloropropene is subjected to primary preheating, then the crude chloropropene is subjected to secondary preheating through the heat of the overhead distillate of the fractionating tower in a distillate cooler HE-1113, and finally enters the fractionating tower TW-1101 for fractionation, and a prefractionating tower reboiler HE-1114 is arranged at the bottom of the prefractionating tower TW-1101.
And the third branch propylene is subjected to vaporization heat exchange with crude chloropropene in a distillate fractionating cooler HE-1113 until the pressure is reduced to 0.20-0.25 MPaG and the temperature is reduced to-15 to-20 ℃, is subjected to pressure transmission after passing through a propylene feed tank VE-1103, is mixed with the first branch propylene in a pipeline behind a propylene entrainment separator VE-1114, and then enters a reactor RE-1101.
Removing the entrainment of the chlorine gas from the outside at 15-20 ℃ in an entrainment separator VE-1108, reducing the pressure to 0.2-0.25 MPaG, adjusting the flow through a flow adjusting valve, and then allowing the chlorine gas to enter a chlorination reactor RE-1101 to react with propylene to generate chloropropene, wherein the reaction temperature is 470-480 ℃, and the reaction pressure is 0.05-0.08 MPaG.
The above description is only an example of the present invention, and is not intended to limit the present invention in any way, and those skilled in the art can make many variations and modifications of the present invention without departing from the scope of the present invention by using the method disclosed above, and the present invention is covered by the claims.
Claims (8)
1. A multistage heat exchange reaction system for producing chloropropene is characterized in that: the reaction system comprises a reactor and a plurality of heat exchangers, the reactor and the heat exchangers are connected through pipelines, regulating valves are installed in the pipelines, reactants in the reactor are propylene and chlorine, the propylene exchanges heat with reaction distillate before entering the reactor, the propylene entering the reactor is preheated, and the reaction distillate enters a subsequent process after being cooled in a three-stage mode.
2. The multistage heat exchange reaction system for producing chloropropene according to claim 1, characterized in that: the propylene is divided into three branches and enters the reactor through four-stage preheating, and the three branches comprise a first branch, a second branch and a third branch.
3. The multistage heat exchange reaction system for producing chloropropene according to claim 2, characterized in that: the preheaters used for the four-stage preheating comprise a first-stage propylene evaporator, a second-stage propylene evaporator, a third-stage propylene preheater and a distillate cooler.
4. The multistage heat exchange reaction system for producing chloropropene according to claim 2, characterized in that: the first branch and the third branch enter the reactor after exchanging heat with the reaction distillate, and the second branch is used as the tower top refrigerant and reflux liquid of the prefractionator.
5. The multistage heat exchange reaction system for producing chloropropene according to claim 2, characterized in that: and a cooler for the third stage cooling in the third stage cooling of the reaction distillate is a first-stage propylene evaporator.
6. The multistage heat exchange reaction system for producing chloropropene according to claim 2, characterized in that: and the cooler for the first stage in the three stages of cooling of the reaction distillate is a reaction distillate cooler.
7. The multistage heat exchange reaction system for producing chloropropene according to claim 2, characterized in that: and heat sources of the secondary propylene evaporator and the tertiary propylene preheater are heating media.
8. The multistage heat exchange reaction system for producing chloropropene according to claim 7, characterized in that: the heat medium is heat conducting oil and enters the reaction system from the hot oil receiving groove.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010208268.XA CN111285752A (en) | 2020-03-23 | 2020-03-23 | Multistage heat exchange reaction system for chloropropene production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010208268.XA CN111285752A (en) | 2020-03-23 | 2020-03-23 | Multistage heat exchange reaction system for chloropropene production |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112062668A (en) * | 2020-10-15 | 2020-12-11 | 江苏蓝色星球环保科技股份有限公司 | Method and device for continuously producing 1,1,1, 2-tetrafluoroethane and coproducing 2,2, 2-trifluoroethanol and glycolic acid |
| CN112125775A (en) * | 2020-10-15 | 2020-12-25 | 江苏蓝色星球环保科技股份有限公司 | Method and device for producing 1,1,1, 2-tetrafluoroethane and co-producing glycolic acid |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5504266A (en) * | 1995-05-24 | 1996-04-02 | The Dow Chemical Company | Process to make allyl chloride and reactor useful in that process |
| US6011186A (en) * | 1997-04-25 | 2000-01-04 | Shell Oil Company | Process for manufacturing allylhalide and equipment to be used therefor |
| CN104876792A (en) * | 2015-05-21 | 2015-09-02 | 山东海益化工科技有限公司 | Method for producing high-purity chloropropene |
| CN104892354A (en) * | 2015-05-21 | 2015-09-09 | 山东海益化工科技有限公司 | Chlorination method and chlorination device in chloropropene production process |
| CN108083971A (en) * | 2017-12-27 | 2018-05-29 | 山东凯泰科技股份有限公司 | A kind of refrigerating method in chloropropene production process |
-
2020
- 2020-03-23 CN CN202010208268.XA patent/CN111285752A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5504266A (en) * | 1995-05-24 | 1996-04-02 | The Dow Chemical Company | Process to make allyl chloride and reactor useful in that process |
| US6011186A (en) * | 1997-04-25 | 2000-01-04 | Shell Oil Company | Process for manufacturing allylhalide and equipment to be used therefor |
| CN104876792A (en) * | 2015-05-21 | 2015-09-02 | 山东海益化工科技有限公司 | Method for producing high-purity chloropropene |
| CN104892354A (en) * | 2015-05-21 | 2015-09-09 | 山东海益化工科技有限公司 | Chlorination method and chlorination device in chloropropene production process |
| CN108083971A (en) * | 2017-12-27 | 2018-05-29 | 山东凯泰科技股份有限公司 | A kind of refrigerating method in chloropropene production process |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112062668A (en) * | 2020-10-15 | 2020-12-11 | 江苏蓝色星球环保科技股份有限公司 | Method and device for continuously producing 1,1,1, 2-tetrafluoroethane and coproducing 2,2, 2-trifluoroethanol and glycolic acid |
| CN112125775A (en) * | 2020-10-15 | 2020-12-25 | 江苏蓝色星球环保科技股份有限公司 | Method and device for producing 1,1,1, 2-tetrafluoroethane and co-producing glycolic acid |
| CN112062668B (en) * | 2020-10-15 | 2023-01-17 | 江苏蓝色星球环保科技股份有限公司 | Method and device for continuously producing 1, 2-tetrafluoroethane and coproducing 2, 2-trifluoroethanol and glycolic acid |
| CN112125775B (en) * | 2020-10-15 | 2023-03-24 | 江苏蓝色星球环保科技股份有限公司 | Method and device for producing 1, 2-tetrafluoroethane and co-producing glycolic acid |
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Application publication date: 20200616 |