CN109438167B - Cyclohexene energy-saving production system and production method - Google Patents
Cyclohexene energy-saving production system and production method Download PDFInfo
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- CN109438167B CN109438167B CN201811610923.3A CN201811610923A CN109438167B CN 109438167 B CN109438167 B CN 109438167B CN 201811610923 A CN201811610923 A CN 201811610923A CN 109438167 B CN109438167 B CN 109438167B
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- benzene
- separation
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- extractant
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- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 43
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 627
- 238000000926 separation method Methods 0.000 claims abstract description 130
- 238000006243 chemical reaction Methods 0.000 claims abstract description 101
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000000746 purification Methods 0.000 claims abstract description 30
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 19
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 238000011084 recovery Methods 0.000 claims abstract description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 52
- 239000001257 hydrogen Substances 0.000 claims description 51
- 229910052739 hydrogen Inorganic materials 0.000 claims description 51
- 238000003860 storage Methods 0.000 claims description 35
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 27
- 239000003054 catalyst Substances 0.000 claims description 21
- 238000010992 reflux Methods 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 13
- 238000010926 purge Methods 0.000 claims description 8
- 238000004062 sedimentation Methods 0.000 claims description 8
- 239000007790 solid phase Substances 0.000 claims description 8
- 239000006228 supernatant Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000011259 mixed solution Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 8
- 239000000047 product Substances 0.000 abstract description 8
- 238000004064 recycling Methods 0.000 abstract description 5
- 238000006555 catalytic reaction Methods 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 2
- 239000007795 chemical reaction product Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 12
- 230000005484 gravity Effects 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 2
- 235000011037 adipic acid Nutrition 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
- C07C5/11—Partial hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
-
- 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
-
- 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
Abstract
The invention discloses an energy-saving cyclohexene production system and a production method, and belongs to the technical field of cyclohexene production. According to the invention, benzene raw materials are used for hydrogenation catalysis, a reaction product is separated and purified through a separation and purification system to prepare cyclohexene, and meanwhile, the heat of reaction feed liquid in the separation and purification process is recycled through the arrangement of a heat recovery system, so that the co-workers who save energy sources also improve the production efficiency, and in addition, the raw materials involved in the invention are as follows: benzene and extractant are recycled again, and after separation and purification, the benzene and the extractant are returned to the feeding system for recycling, so that resources are saved. Meanwhile, as no byproducts are generated in the whole production process, the obtained product cyclohexane and cyclohexene can be used as products, and the method is very green and environment-friendly.
Description
Technical Field
The invention relates to the technical field of cyclohexene preparation, in particular to an energy-saving cyclohexene production system and a production method.
Background
The production route of adipic acid and caprolactam based on cyclohexene hydration method is the main stream process in the current industrial production. Wherein, the cyclohexene is produced by partially hydrogenating benzene, and reacting in a gas-liquid-solid four-phase system under the action of a catalyst to generate cyclohexene, cyclohexane and water.
The traditional cyclohexene generated by partial hydrogenation of benzene is not utilized for reaction heat, and is cooled only by circulating cooling water, so that energy waste is caused, and the production cost is increased.
Disclosure of Invention
The invention aims to provide an energy-saving cyclohexene production system and a production method thereof, which aim to solve the problems of resource waste and high production cost of the existing cyclohexene production technology.
The technical scheme for solving the technical problems is as follows:
a cyclohexene energy-saving production system, comprising: a feeding system, a reaction system, a separation and purification system and a heat recovery system; wherein:
the feeding system comprises a benzene adding device, a hydrogenation device and a nitrogen purging device which are respectively connected with the reaction system, and an extractant adding device which is connected with the separation and purification system;
the reaction system comprises a reaction kettle connected with the benzene adding device, the hydrogenation device and the nitrogen purging device, and a sedimentation tank connected with the reaction kettle, wherein a liquid phase outlet of the sedimentation tank is connected with the separation and purification system;
the separation and purification system comprises a benzene separation tower, a benzene rectifying tower, a cyclohexane separation tower and a cyclohexene rectifying tower; the inlet of the benzene separation tower is respectively connected with the liquid phase outlet of the settling tank and the extractant adding device, and the bottom outlet and the top outlet of the benzene separation tower are respectively connected with the inlet of the benzene rectifying tower and the bottom inlet of the cyclohexane separation tower; the top outlet and the bottom outlet of the benzene rectifying tower are respectively connected with a benzene adding device and an extracting agent adding device; the bottom outlet of the cyclohexane separating tower is connected with a cyclohexene rectifying tower; the bottom outlet of the cyclohexene rectifying tower is connected with an extracting agent adding device;
the heat recovery system comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, a first reboiler and a second reboiler; the first heat exchanger is respectively connected with an outlet of the benzene adding device and an inlet of the reaction kettle, and is also respectively connected with the second heat exchanger and an inlet of the benzene rectifying tower; the first reboiler is respectively connected with the bottom outlet of the benzene separation tower and the second heat exchanger, and is connected with the bottom outlet of the benzene rectifying tower; the second heat exchanger, the third heat exchanger and the second reboiler are sequentially connected in series on the bottom outlet of the cyclohexane separation tower; the third heat exchanger is respectively connected with the bottom outlet of the cyclohexene rectifying tower and the inlet of the extractant adding device; the outlet of the second reboiler is respectively connected with the cyclohexane separation tower and the cyclohexene rectifying tower.
Further, in a preferred embodiment of the present invention, the solid phase outlet of the settling tank is connected to the reaction vessel through a pipe.
Further, in a preferred embodiment of the present invention, the cyclohexene energy-saving production system further includes an extractant storage tank, an inlet of the extractant storage tank is connected to the first reboiler and the third heat exchanger, and an outlet of the extractant storage tank is connected to an inlet of the extractant adding device.
Further, in a preferred embodiment of the present invention, the benzene adding device includes a benzene storage tank, and a refined benzene pipe and a circulating benzene pipe connected to an inlet of the benzene storage tank, respectively, and the circulating benzene pipe is connected to an outlet of the top of the benzene rectifying tower.
Further, in a preferred embodiment of the present invention, the hydrogenation apparatus includes a hydrogen input pipe and a hydrogen circulation pipe, the hydrogen input pipe and the hydrogen circulation pipe are connected to an inlet of the reaction kettle through a booster pump, and the hydrogen circulation pipe is connected to a hydrogen outlet of the reaction kettle.
A method for producing cyclohexene by using the cyclohexene energy-saving production system comprises the following steps:
(1) The method comprises the steps of (1) reacting raw material benzene hydrogenation with a catalyst in a reaction kettle, and settling the reacted mixed solution in a settling tank;
(2) Conveying the supernatant obtained after sedimentation to a benzene separation tower for separation and purification, conveying tower top distillate obtained by the benzene separation tower to a cyclohexane separation tower, conveying tower bottom mixed liquor obtained by the benzene separation tower to a first reboiler for heat exchange with tower bottom feed liquid of a benzene rectifying tower, and conveying the tower bottom mixed liquor into the benzene rectifying tower after heat exchange through a pipeline by a second heat exchanger and a first heat exchanger; the heat of the tower bottom mixed liquor of the benzene separation tower entering the first heat exchanger is used for preheating raw material benzene, the tower bottom mixed liquor of the benzene separation tower comprises benzene and an extractant, and the tower top distillate of the benzene separation tower comprises cyclohexane and cyclohexene;
(3) Benzene obtained after separation and purification by a benzene rectifying tower is output from the tower top and returns to a benzene adding device through a pipeline, and after heat exchange of a first reboiler, vaporized part returns to the benzene rectifying tower through a pipeline, and unvaporized part returns to the extractant adding device through a pipeline; wherein, the tower bottom feed liquid of the benzene rectifying tower comprises benzene and an extractant;
(4) Separating and purifying the tower top distillate from the benzene separation tower through a cyclohexane separation tower, outputting the obtained cyclohexane from the tower top, conveying the tower bottom mixed liquor of the cyclohexane separation tower into a second heat exchanger to be heated with the tower bottom mixed liquor from the benzene separation tower, enabling the heated mixed liquor to enter a third heat exchanger to exchange heat with the tower bottom feed liquor from the cyclohexene rectifying tower, enabling the heated mixed liquor to enter a second reboiler, enabling the vaporized part in the second reboiler to return to the cyclohexane separation tower through a pipeline, and enabling the unvaporized part to enter the cyclohexene rectifying tower;
(5) And (3) separating and purifying the unvaporized part in the step (4) through a cyclohexene rectifying tower, outputting the obtained cyclohexene from the tower top, outputting the residual extractant from the tower bottom, exchanging heat through a third heat exchanger, and returning the residual extractant to the extractant adding device through a pipeline.
Further, in a preferred embodiment of the present invention, the reaction conditions in the reaction vessel include: the reaction is carried out for 10 to 50 minutes under the conditions of the hydrogen pressure of 4 to 7MPa and the reaction temperature of 140 to 180 ℃, hydrogen is continuously introduced in the reaction process, the pressure is kept constant, and the mass ratio of raw material benzene to catalyst is (10 to 30): 1.
the invention can control the hydrogen pressure to be 4-7MPa in the reaction process, and can simultaneously consider the hydrogen activity and the selectivity to cyclohexene. When the hydrogen pressure is lower than 4MPa, the hydrogenation activity is too low, so that the conversion rate of benzene is reduced, and the production efficiency is not improved; when the hydrogen pressure is higher than 7MPa, the hydrogenation activity is too high, so that the cyclohexene selectivity is reduced, excessive cyclohexane is easy to generate, and the production of the cyclohexene serving as a main target product is not facilitated. In addition, by combining the proper 140-180 ℃ reaction temperature, the benzene can be fully converted in the temperature range, the productivity is improved, and the reduction of cyclohexene selectivity caused by overhigh temperature can be avoided.
Further, in a preferred embodiment of the present invention, the reaction conditions of the benzene separation column include: the temperature of the tower bottom is 120-140 ℃, the temperature of the tower top is 80-100 ℃, the pressure drop of the whole tower is 0.01-0.04MPa, and the molar reflux ratio of the tower top is more than or equal to 1.5; the reaction conditions of the benzene rectifying tower comprise: the temperature of the tower bottom is 75-85 ℃, the temperature of the tower top is 42-48 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the reflux ratio is more than or equal to 0.8.
Further, in a preferred embodiment of the present invention, the reaction conditions of the cyclohexane separation column include: the temperature of the tower bottom is 90-110 ℃, the temperature of the tower top is 85-95 ℃, the pressure drop of the whole tower is 0.01-0.04MPa, and the reflux ratio of the tower top is more than or equal to 3.0; the reaction conditions of the cyclohexene rectifying column include: the temperature of the tower bottom is 130-150 ℃, the temperature of the tower top is 42-50 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the molar reflux ratio of the tower top is more than or equal to 0.8.
According to the invention, by controlling the tower bottom temperature, the tower top temperature, the total tower pressure drop and the molar reflux ratio of the benzene separation tower, the benzene rectification tower, the cyclohexane separation tower and the cyclohexene rectification tower, the evaporation rate and the cooling rate of tower bottom materials can be met, and meanwhile, the mass fractions of tower top materials and tower bottom material products can reach the expected targets, so that the normal operation of the tower is maintained. In addition, when the benzene rectifying tower and the cyclohexene rectifying tower are separated and purified, the invention controls the vacuum degree of the whole tower to be more than or equal to 0.03MPa, and can maintain the boiling point of the tower top material to be more than 42 ℃ under the condition that the absolute pressure is higher than 0.03MPa, thereby cooling the material by using a cheaper heat source (cooling medium) and further achieving the aim of energy conservation.
The invention has the following beneficial effects:
according to the invention, benzene raw materials are used for hydrogenation catalysis, a reaction product is separated and purified through a separation and purification system to prepare cyclohexene, and meanwhile, the heat of reaction feed liquid in the separation and purification process is recycled through the arrangement of a heat recovery system, so that energy is saved, the production efficiency is improved, and in addition, the raw materials participating in the invention are: benzene and extractant are recycled again, and after separation and purification, the benzene and the extractant are returned to the feeding system for recycling, so that resources are saved. Meanwhile, as no byproducts are generated in the whole production process, the obtained product cyclohexane and cyclohexene can be used as products, and the method is very green and environment-friendly. The invention obtains high-purity cyclohexane in the whole normal production process, and can also be used as a cyclohexane production system.
According to the invention, the sedimentation tank is used for carrying out sedimentation separation on the reacted product, the settled solid phase is the catalyst, and the pipeline is arranged at the solid phase outlet, so that the catalyst can be returned to the reaction kettle again for catalytic reaction, and resource waste is avoided.
According to the invention, the extractant after the whole separation and purification process is recovered through the first reboiler and the third heat exchanger, then is stored in the extractant storage tank in a concentrated manner, and is returned to the extractant adding device through the pipeline to participate in the separation and purification system again, so that the resources are recycled.
According to the invention, the pipeline is arranged at the hydrogen outlet at the top of the reaction kettle, so that unreacted hydrogen can be returned to the hydrogenation device again for use, and resource waste is avoided.
Drawings
FIG. 1 is a schematic diagram of a production system according to the present invention.
In the figure: 10-a reaction kettle; a 21-benzene separation column; 22-benzene rectifying tower; a 23-cyclohexane separation column; 24-cyclohexene rectifying column; 31-a first heat exchanger; 32-a first reboiler; 33-a second heat exchanger; 34-a third heat exchanger; 35-a second reboiler; 41-benzene storage tank; 42-settling tank; 43-extractant storage tank; 44-an extractant adding device; 50-a circulation pump; 60-booster pump.
Detailed Description
The principles and features of the present invention are described below with reference to the drawings and examples, which are provided for illustration only and are not intended to limit the scope of the invention. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
Example 1
Referring to fig. 1, the cyclohexene energy-saving production system of the present invention comprises: a feeding system, a reaction system, a separation and purification system and a heat recovery system.
The feed system includes a benzene adding device, a hydrogenation device and a nitrogen purging device, which are respectively connected with the reaction system, and an extractant adding device 44 connected with the separation and purification system. The outlets of the benzene adding device, the hydrogenation device and the nitrogen purging device are respectively connected with the inlet of the reaction kettle 10 of the reaction system.
Benzene in the benzene adding device is conveyed to the reaction kettle 10 through a circulating pump 50. Benzene in the benzene adding device is derived from two parts: additional refined benzene and recycled benzene in the production system. The benzene adding apparatus includes a benzene storage tank 41, and a refined benzene pipe and a circulating benzene pipe connected to inlets of the benzene storage tank 41, respectively. The circulating benzene pipeline is connected with the top outlet of the benzene rectifying tower 22 of the separation and purification system.
The hydrogen in the hydrogenation apparatus is pressurized by the booster pump 60, and then is fed into the reaction vessel 10, and the hydrogen at the pressure required for the reaction is fed into the reaction vessel 10. The hydrogen in the hydrogenation unit originates from two parts: additional hydrogen and the remaining hydrogen in the reaction vessel 10 in the production system that has not been reacted. The hydrogenation device comprises a hydrogen input pipeline and a hydrogen circulation pipeline. The hydrogen input pipe and the hydrogen circulation pipe are connected to the inlet of the reaction tank 10 through a booster pump 60. The hydrogen input pipeline is connected with the hydrogen storage tank. The hydrogen circulation pipeline is connected with a hydrogen outlet of the reaction kettle 10.
The nitrogen purging device is pressurized by the booster pump 60 and then blown into the reaction kettle 10, so as to remove air in the reaction kettle 10 before the reaction. The extractant in the extractant adding device 44 is conveyed to the separation and extraction system through a circulating pump 50 for separation and purification of benzene, cyclohexane and cyclohexene. The extractant in the extractant-adding device 44 comprises two parts: the external extractant from the storage tank and the production system separate the purified extractant.
The reaction system includes a reaction vessel 10 connected to a benzene addition unit, a hydrogenation unit, and a nitrogen purge unit, and a settling tank 42 connected to the reaction vessel 10. The liquid phase outlet of the settling tank 42 is connected with a separation and purification system, so that supernatant obtained after settling enters the separation and purification system for separation and purification. The solid phase outlet of the settling tank 42 is connected with the reaction kettle 10 through a pipeline, and the settled catalyst is returned to the reaction kettle 10 to continuously participate in the catalytic reaction. Catalyst is withdrawn from the bottom of the settling tank 42 back into the reactor 10 by a circulation pump 50.
The separation and purification system comprises a benzene separation column 21, a benzene rectification column 22, a cyclohexane separation column 23 and a cyclohexene rectification column 24.
The inlet of the benzene separation column 21 is connected to the liquid phase outlet of the settling tank 42 and the extractant-adding device 44, respectively. The conduit for transporting the supernatant of the settling tank 42 is connected to the lower section of the benzene separation column 21. The pipe for transporting the extractant is connected to the upper section of the benzene separation column 21. The bottom outlet and the top outlet of the benzene separation column 21 are connected to the inlet of the benzene rectification column 22 and the bottom inlet of the cyclohexane separation column 23, respectively. The mixed solution of cyclohexane and cyclohexene distilled from the top of the benzene separation column 21 is pumped to the lower stage of the cyclohexane separation column 23 by the circulation pump 50, and further separated and purified. The mixed solution of benzene and extractant distilled from the bottom tower kettle of the benzene separation tower 21 is conveyed to the benzene rectifying tower 22 after heat exchange of the first reboiler 32, the second heat exchanger 33 and the first heat exchanger 31 of the heat recovery system, and further separation and purification are carried out. The top outlet and bottom outlet of the benzene rectification column 22 are respectively connected with a benzene adding device and an extractant adding device 44. Benzene distilled from the top of the benzene rectifying tower is conveyed to a benzene adding device through a pipeline and recycled. The extractant distilled from the bottom of the benzene rectification column 22 is conveyed to the first reboiler 32 through a pipeline, the vaporized part is returned to the benzene rectification column 22 for separation and purification again, and the unvaporized part is returned to the extractant-adding device 44 through a pipeline. The bottom outlet of the cyclohexane separation column 23 is connected with a cyclohexene rectifying column 24. The bottom outlet of the cyclohexene rectifying column 24 is connected with an extractant-adding device 44.
The heat recovery system comprises a first heat exchanger 31, a second heat exchanger 33, a third heat exchanger 34, a first reboiler 32 and a second reboiler 35. The first heat exchanger 31 is connected with the outlet of the benzene adding device and the inlet of the reaction kettle 10 respectively, and is used for preheating raw benzene from the benzene adding device. The first heat exchanger 31 is also connected with the second heat exchanger 33 and the inlet of the benzene rectifying tower 22 respectively, and is used for carrying out heat exchange on the raw materials in the first heat exchanger 31 after heating and reboiling the tower kettle mixed liquid of the benzene separating tower 21, and preheating raw material benzene. The first reboiler 32 is connected to the bottom outlet of the benzene separation column 21 and the second heat exchanger 33, and the first reboiler 32 is connected to the bottom outlet of the benzene rectification column 22, and is used for exchanging heat between benzene and extractant from the benzene separation column 21 and the mixed liquid of the benzene rectification column and the bottom of the first reboiler 32, exchanging heat between the second heat exchanger 33 and the first heat exchanger 31, and returning the mixed liquid to the benzene rectification column 22. The second heat exchanger 33, the third heat exchanger 34 and the second reboiler 35 are sequentially connected in series to the bottom outlet of the cyclohexane separation tower 23, and are used for enabling the tower bottom mixed liquid of the cyclohexane separation tower 23 to enter the second reboiler 35 after heat exchange by the second heat exchanger 33 and the third heat exchanger 34, and under the action of low-pressure steam, a part of vaporized tower bottom mixed liquid returns to the cyclohexane separation tower 23, and another part of unvaporized tower bottom mixed liquid enters the cyclohexene rectifying tower 24. The third heat exchanger 34 is respectively connected with the bottom outlet of the cyclohexene rectifying column 24 and the inlet of the extractant adding device 44, and is used for returning the distilled extractant of the cyclohexene rectifying column 24 to the extractant adding device 44 after heat exchange. The outlet of the second reboiler 35 is respectively connected with the cyclohexane separation tower 23 and the cyclohexene rectifying tower 24, and is used for heat exchange of tower kettle mixed liquor from the cyclohexane separation tower 23, one part of the mixed liquor is vaporized and returned to the cyclohexane separation tower 23, and the other part of the mixed liquor is not vaporized and enters the cyclohexene rectifying tower 24.
The cyclohexene energy-saving production system further comprises an extractant storage tank 43, wherein the inlet of the extractant storage tank 43 is respectively connected with the first reboiler 32 and the third heat exchanger 34, and the outlet of the extractant storage tank 43 is connected with the inlet of the extractant adding device 44.
Example 2
The cyclohexene production method of the present embodiment includes:
firstly, the treated Ru-Zn catalyst is prepared according to the mass ratio of raw material benzene to catalyst of 10:1 are added into a reaction kettle 10, and the air in the reaction kettle 10 is replaced by nitrogen for 3 times continuously. The added refined benzene and the circulating benzene from the top of the benzene rectifying tower 22 are mixed and then enter a benzene storage tank, the mixed raw materials enter a first heat exchanger 31 through a benzene conveying pump, and the benzene after heat exchange is conveyed to the reaction kettle 10 through a pipeline. The hydrogen was supplied to the reaction vessel 10 through the pipe by the booster pump 60, and in this process, the nitrogen in the reaction vessel 10 was replaced with hydrogen for 3 consecutive times. After replacement, hydrogen is introduced again to enable the hydrogen pressure in the reaction kettle 10 to reach 4.0MPa, then the reaction kettle 10 is heated to 140 ℃, stirring is carried out for 10min at the temperature, and hydrogen is continuously introduced in the reaction process to enable the pressure in the reaction kettle 10 to be kept constant. After the reaction time was reached, the hydrogen valve was closed, stirring was stopped, and heating was stopped.
The reacted solution is transported to the gravity settling tank 42 through a pipeline by an overflow weir built in the reaction kettle 10, and after the solid phase catalyst is separated, the catalyst is circulated to the reaction kettle 10 through a pipeline by a circulating pump 50. The separated supernatant enters the middle lower region of the benzene separation column 21 through an overflow weir in the gravity settling tank 42.
After the external extractant is mixed with the circulating extractant from the circulating pump 50, the mixture is conveyed to the middle upper part of the benzene separation tower 21 through an extractant storage tank and an extractant conveying pump, the tower bottom temperature of the benzene separation tower 21 is controlled to be 120 ℃, the tower top temperature is controlled to be 80 ℃, the total tower pressure drop temperature is 0.01MPa, and the tower top molar reflux ratio is more than or equal to 1.5. The benzene and extractant mixed liquor distilled from the tower kettle enters a first reboiler 32 tube pass, exchanges heat with the feed liquid in the tower kettle of the benzene rectifying tower 22, enters a second heat exchanger 33 tube pass through a pipeline, finally exchanges heat through a first heat exchanger 31, and is conveyed into the benzene rectifying tower 22 through the pipeline. The mixed liquid of cyclohexene and cyclohexane distilled from the top of the benzene separation column 21 is sent to the middle-lower part of the cyclohexane separation column 23 by a circulating pump 50, and the extractant is sent to the middle-upper part of the cyclohexane separation column 23 by the circulating pump 50.
The temperature of the tower bottom of the benzene rectifying tower 22 is controlled to be 75 ℃, the temperature of the tower top is controlled to be 42 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the reflux ratio is more than or equal to 0.8. At this time, the solution at the bottom of the benzene rectifying tower 22 enters the shell side of the first reboiler 32, part of the solution is vaporized and then returns to the benzene rectifying tower 22, and the unvaporized part is conveyed to the extractant storage tank 43 through a pipeline. The distillate at the top of the benzene rectifying tower 22 is benzene and is conveyed into a benzene storage tank through a pipeline.
The temperature of the tower bottom of the cyclohexane separation tower 23 is controlled to be 90 ℃, the temperature of the tower top is 85 ℃, the pressure drop of the whole tower is 0.01MPa, and the reflux ratio of the tower top is more than or equal to 3.0. The high-purity cyclohexane is distilled out from the top of the cyclohexane separation tower 23, the mass fraction is more than 99.5 percent, and the cyclohexane is conveyed out of the system through a pipeline. The mixed liquid at the tower bottom of the cyclohexane separation tower 23 firstly enters a second heat exchanger 33 to exchange heat with the stillage liquid of the cyclohexene rectifying tower 24 through a tube pass of a third heat exchanger 34, then enters a second reboiler 35 to exchange heat with the stillage liquid, low-pressure steam is introduced into the tube pass, so that the distillate is partially vaporized and then returns to the cyclohexane separation tower 23, and unvaporized solution enters the cyclohexene rectifying tower 24 through a pipeline.
The temperature of the tower bottom of the cyclohexene rectifying tower 24 is controlled to be 130 ℃, the temperature of the tower top is controlled to be 42 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the molar reflux ratio of the tower top is more than or equal to 0.8. At this time, the distillate at the top of the cyclohexene rectifying tower 24 is high-purity cyclohexene, the mass fraction of which is more than or equal to 98.0%, and the cyclohexene is conveyed out of the system through a pipeline. The stillage liquid of the cyclohexene rectifying column 24 is used as an extractant, and enters an extractant storage tank 43 after heat exchange by the third heat exchanger 34. The circulating extractant at the bottoms of the benzene rectifying tower 22 and the cyclohexene rectifying tower 24 is conveyed to the extractant adding device 44 for recycling through the circulating pump 50.
Example 3
The cyclohexene production method of the present embodiment includes:
firstly, the treated Ru-Zn catalyst is prepared according to the mass ratio of raw material benzene to catalyst of 30:1 is added into a reaction kettle 10, and the air in the reaction kettle 10 is replaced by nitrogen for 5 times. The added refined benzene and the circulating benzene from the top of the benzene rectifying tower 22 are mixed and then enter a benzene storage tank, the mixed raw materials enter a first heat exchanger 31 through a benzene conveying pump, and the benzene after heat exchange is conveyed to the reaction kettle 10 through a pipeline. The hydrogen gas is transported to the reaction vessel 10 through a pipe by the booster pump 60, and in this process, the nitrogen gas in the reaction vessel 10 is replaced with hydrogen gas for 5 consecutive times. After replacement, hydrogen is again introduced to enable the hydrogen pressure in the reaction kettle 10 to reach 7.0MPa, then the reaction kettle 10 is heated to 180 ℃, stirring is carried out for 50min at the temperature, and hydrogen is continuously introduced in the reaction process to enable the pressure in the reaction kettle 10 to be kept constant. After the reaction time was reached, the hydrogen valve was closed, stirring was stopped, and heating was stopped.
The reacted solution is transported to the gravity settling tank 42 through a pipeline by an overflow weir built in the reaction kettle 10, and after the solid phase catalyst is separated, the catalyst is circulated to the reaction kettle 10 through a pipeline by a circulating pump 50. The separated supernatant enters the middle lower region of the benzene separation column 21 through an overflow weir in the gravity settling tank 42.
After the external extractant is mixed with the circulating extractant from the circulating pump 50, the mixture is conveyed to the middle upper part of the benzene separation tower 21 through an extractant storage tank and an extractant conveying pump, the tower bottom temperature of the benzene separation tower 21 is controlled to be 140 ℃, the tower top temperature is 100 ℃, the total tower pressure drop temperature is 0.04MPa, and the tower top molar reflux ratio is more than or equal to 1.5. The benzene and extractant mixed liquor distilled from the tower kettle enters a first reboiler 32 tube pass, exchanges heat with the feed liquid in the tower kettle of the benzene rectifying tower 22, enters a second heat exchanger 33 tube pass through a pipeline, finally exchanges heat through a first heat exchanger 31, and is conveyed into the benzene rectifying tower 22 through the pipeline. The mixed liquid of cyclohexene and cyclohexane distilled from the top of the benzene separation column 21 is sent to the middle-lower part of the cyclohexane separation column 23 by a circulating pump 50, and the extractant is sent to the middle-upper part of the cyclohexane separation column 23 by the circulating pump 50.
The temperature of the tower bottom of the benzene rectifying tower 22 is controlled to be 85 ℃, the temperature of the tower top is controlled to be 48 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the reflux ratio is more than or equal to 0.8. At this time, the solution at the bottom of the benzene rectifying tower 22 enters the shell side of the first reboiler 32, part of the solution is vaporized and then returns to the benzene rectifying tower 22, and the unvaporized part is conveyed to the extractant storage tank 43 through a pipeline. The distillate at the top of the benzene rectifying tower 22 is benzene and is conveyed into a benzene storage tank through a pipeline.
The temperature of the tower bottom of the cyclohexane separation tower 23 is controlled to be 110 ℃, the temperature of the tower top is 95 ℃, the pressure drop of the whole tower is 0.04MPa, and the reflux ratio of the tower top is more than or equal to 3.0. The high-purity cyclohexane is distilled out from the top of the cyclohexane separation tower 23, the mass fraction is more than 99.5 percent, and the cyclohexane is conveyed out of the system through a pipeline. The mixed liquid at the tower bottom of the cyclohexane separation tower 23 firstly enters a second heat exchanger 33 to exchange heat with the stillage liquid of the cyclohexene rectifying tower 24 through a tube pass of a third heat exchanger 34, then enters a second reboiler 35 to exchange heat with the stillage liquid, low-pressure steam is introduced into the tube pass, so that the distillate is partially vaporized and then returns to the cyclohexane separation tower 23, and unvaporized solution enters the cyclohexene rectifying tower 24 through a pipeline.
The temperature of the tower bottom of the cyclohexene rectifying tower 24 is controlled to be 150 ℃, the temperature of the tower top is controlled to be 50 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the molar reflux ratio of the tower top is more than or equal to 0.8. At this time, the distillate at the top of the cyclohexene rectifying tower 24 is high-purity cyclohexene, the mass fraction of which is more than or equal to 98.0%, and the cyclohexene is conveyed out of the system through a pipeline. The stillage liquid of the cyclohexene rectifying column 24 is used as an extractant, and enters an extractant storage tank 43 after heat exchange by the third heat exchanger 34. The circulating extractant at the bottoms of the benzene rectifying tower 22 and the cyclohexene rectifying tower 24 is conveyed to the extractant adding device 44 for recycling through the circulating pump 50.
Example 4
The cyclohexene production method of the present embodiment includes:
firstly, the treated Ru-Zn catalyst is prepared according to the mass ratio of raw material benzene to catalyst of 20:1 is added into the reaction kettle 10, and the air in the reaction kettle 10 is replaced by nitrogen for 4 times continuously. The added refined benzene and the circulating benzene from the top of the benzene rectifying tower 22 are mixed and then enter a benzene storage tank, the mixed raw materials enter a first heat exchanger 31 through a benzene conveying pump, and the benzene after heat exchange is conveyed to the reaction kettle 10 through a pipeline. The hydrogen is conveyed to the reaction kettle 10 through a pipeline by the booster pump 60, and in the process, the nitrogen in the reaction kettle 10 is replaced by the hydrogen for 3-5 times continuously. After the replacement, hydrogen is introduced again to enable the hydrogen pressure in the reaction kettle 10 to reach 5MPa, then the reaction kettle 10 is heated to 150 ℃, stirring is carried out for 30min at the temperature, and hydrogen is continuously introduced in the reaction process to enable the pressure in the reaction kettle 10 to be kept constant. After the reaction time was reached, the hydrogen valve was closed, stirring was stopped, and heating was stopped.
The reacted solution is transported to the gravity settling tank 42 through a pipeline by an overflow weir built in the reaction kettle 10, and after the solid phase catalyst is separated, the catalyst is circulated to the reaction kettle 10 through a pipeline by a circulating pump 50. The separated supernatant enters the middle lower region of the benzene separation column 21 through an overflow weir in the gravity settling tank 42.
After the external extractant is mixed with the circulating extractant from the circulating pump 50, the mixture is conveyed to the middle upper part of the benzene separation tower 21 through an extractant storage tank and an extractant conveying pump, the tower bottom temperature of the benzene separation tower 21 is controlled to be 130 ℃, the tower top temperature is controlled to be 90 ℃, the total tower pressure drop temperature is 0.02MPa, and the tower top molar reflux ratio is more than or equal to 1.5. The benzene and extractant mixed liquor distilled from the tower kettle enters a first reboiler 32 tube pass, exchanges heat with the feed liquid in the tower kettle of the benzene rectifying tower 22, enters a second heat exchanger 33 tube pass through a pipeline, finally exchanges heat through a first heat exchanger 31, and is conveyed into the benzene rectifying tower 22 through the pipeline. The mixed liquid of cyclohexene and cyclohexane distilled from the top of the benzene separation column 21 is sent to the middle-lower part of the cyclohexane separation column 23 by a circulating pump 50, and the extractant is sent to the middle-upper part of the cyclohexane separation column 23 by the circulating pump 50.
The temperature of the tower bottom of the benzene rectifying tower 22 is controlled to be 80 ℃, the temperature of the tower top is controlled to be 45 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the reflux ratio is more than or equal to 0.8. At this time, the solution at the bottom of the benzene rectifying tower 22 enters the shell side of the first reboiler 32, part of the solution is vaporized and then returns to the benzene rectifying tower 22, and the unvaporized part is conveyed to the extractant storage tank 43 through a pipeline. The distillate at the top of the benzene rectifying tower 22 is benzene and is conveyed into a benzene storage tank through a pipeline.
The temperature of the tower bottom of the cyclohexane separation tower 23 is controlled to be 100 ℃, the temperature of the tower top is 90 ℃, the pressure drop of the whole tower is 0.02MPa, and the reflux ratio of the tower top is more than or equal to 3.0. The high-purity cyclohexane is distilled out from the top of the cyclohexane separation tower 23, the mass fraction is more than 99.5 percent, and the cyclohexane is conveyed out of the system through a pipeline. The mixed liquid at the tower bottom of the cyclohexane separation tower 23 firstly enters a second heat exchanger 33 shell side for heat exchange, then enters a second reboiler 35 shell side for heat exchange with the stillage liquid of the cyclohexene rectifying tower 24 through a third heat exchanger 34 tube side, low-pressure steam is introduced into the tube side, so that the distillate is partially vaporized and returns to the cyclohexane separation tower 23, the unvaporized solution enters 140 ℃ through a pipeline, the tower top temperature is 45 ℃, the total tower vacuum degree is more than or equal to 0.03MPa, and the tower top molar reflux ratio is more than or equal to 0.8. At this time, the distillate at the top of the cyclohexene rectifying tower 24 is high-purity cyclohexene, the mass fraction of which is more than or equal to 98.0%, and the cyclohexene is conveyed out of the system through a pipeline. The stillage liquid of the cyclohexene rectifying column 24 is used as an extractant, and enters an extractant storage tank 43 after heat exchange by the third heat exchanger 34. The circulating extractant at the bottoms of the benzene rectifying tower 22 and the cyclohexene rectifying tower 24 is conveyed to the extractant adding device 44 for recycling through the circulating pump 50.
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (5)
1. A cyclohexene energy-saving production system, comprising: a feeding system, a reaction system, a separation and purification system and a heat recovery system; wherein:
the feeding system comprises a benzene adding device, a hydrogenation device and a nitrogen purging device which are respectively connected with the reaction system, and an extractant adding device (44) connected with the separation and purification system;
the reaction system comprises a reaction kettle (10) connected with the benzene adding device, the hydrogenation device and the nitrogen purging device, and a sedimentation tank (42) connected with the reaction kettle (10), wherein a liquid phase outlet of the sedimentation tank (42) is connected with the separation and purification system;
the separation and purification system comprises a benzene separation tower (21), a benzene rectifying tower (22), a cyclohexane separation tower (23) and a cyclohexene rectifying tower (24); the inlet of the benzene separation tower (21) is respectively connected with the liquid phase outlet of the settling tank (42) and the extractant adding device (44), and the bottom outlet and the top outlet of the benzene separation tower (21) are respectively connected with the inlet of the benzene rectifying tower (22) and the bottom inlet of the cyclohexane separation tower (23); the top outlet and the bottom outlet of the benzene rectifying tower (22) are respectively connected with the benzene adding device and the extractant adding device (44); the bottom outlet of the cyclohexane separation tower (23) is connected with the cyclohexene rectifying tower (24); the bottom outlet of the cyclohexene rectifying column (24) is connected with the extractant adding device (44);
the heat recovery system comprises a first heat exchanger (31), a second heat exchanger (33), a third heat exchanger (34), a first reboiler (32) and a second reboiler (35); the first heat exchanger (31) is respectively connected with an outlet of the benzene adding device and an inlet of the reaction kettle (10), and the first heat exchanger (31) is also respectively connected with the second heat exchanger (33) and an inlet of the benzene rectifying tower (22); the first reboiler (32) is respectively connected with the bottom outlet of the benzene separation tower (21) and the second heat exchanger (33), and the first reboiler (32) is connected with the bottom outlet of the benzene rectification tower (22); the second heat exchanger (33), the third heat exchanger (34) and the second reboiler (35) are sequentially connected in series on the bottom outlet of the cyclohexane separation tower (23); the third heat exchanger (34) is respectively connected with the bottom outlet of the cyclohexene rectifying tower (24) and the inlet of the extractant adding device (44); the outlet of the second reboiler (35) is respectively connected with the cyclohexane separation tower (23) and the cyclohexene rectifying tower (24);
a method for producing cyclohexene by a cyclohexene energy-saving production system, comprising the following steps:
(1) The raw material benzene is hydrogenated and reacts with the catalyst in a reaction kettle (10), and the mixed solution after the reaction is settled by a settling tank (42);
(2) Conveying the supernatant obtained after sedimentation to a benzene separation tower (21) for separation and purification, conveying the tower top distillate obtained by the benzene separation tower (21) to a cyclohexane separation tower (23), conveying the tower bottom mixed liquid obtained by the benzene separation tower (21) to a first reboiler (32) for heat exchange with tower bottom feed liquid of a benzene rectifying tower (22), and conveying the tower bottom mixed liquid into the benzene rectifying tower (22) after heat exchange through a second heat exchanger (33) and a first heat exchanger (31) through a pipeline; the heat of the tower kettle mixed liquor of the benzene separation tower (21) entering the first heat exchanger (31) is used for preheating raw material benzene, the tower kettle mixed liquor of the benzene separation tower (21) comprises benzene and an extractant, and the tower top distillate of the benzene separation tower (21) comprises cyclohexane and cyclohexene;
(3) Benzene obtained after separation and purification by the benzene rectifying tower (22) is output from the tower top and returned to the benzene adding device through a pipeline, and after heat exchange is carried out on tower bottom material liquid of the benzene rectifying tower (22) from tower bottom output by the first reboiler (32), the vaporized part is returned to the benzene rectifying tower (22) through the pipeline, and the unvaporized part is returned to the extractant adding device (44) through the pipeline; wherein, the tower bottom feed liquid of the benzene rectifying tower (22) comprises benzene and an extractant;
(4) Separating and purifying the tower top distillate from the benzene separation tower (21) through a cyclohexane separation tower (23), outputting the obtained cyclohexane from the tower top, conveying the tower kettle mixed liquor of the cyclohexane separation tower (23) to the second heat exchanger (33) to be heated with the tower kettle mixed liquor from the benzene separation tower (21), enabling the tower top mixed liquor to enter the third heat exchanger (34) and then exchange heat with the tower kettle feed liquor from the cyclohexene rectifying tower (24), enabling the tower bottom feed liquor to enter the second reboiler (35), enabling the vaporized part in the second reboiler (35) to return to the cyclohexane separation tower (23) through a pipeline, and enabling the unvaporized part to enter the cyclohexene rectifying tower (24);
(5) Separating and purifying the unvaporized part in the step (4) by a cyclohexene rectifying tower (24), outputting the obtained cyclohexene from the top of the tower, exchanging heat of the residual extractant from the bottom of the tower by a third heat exchanger (34), and returning the residual extractant to an extractant adding device (44) through a pipeline;
the reaction conditions in the reaction kettle (10) comprise: the reaction is carried out for 10 to 50 minutes under the conditions of the hydrogen pressure of 4 to 7MPa and the reaction temperature of 140 to 180 ℃, hydrogen is continuously introduced in the reaction process, the pressure is kept constant, and the mass ratio of raw material benzene to catalyst is (10 to 30): 1, a step of;
the reaction conditions of the benzene separation column (21) include: the temperature of the tower bottom is 120-140 ℃, the temperature of the tower top is 80-100 ℃, the pressure drop of the whole tower is 0.01-0.04MPa, and the molar reflux ratio of the tower top is more than or equal to 1.5; the reaction conditions of the benzene rectification column (22) include: the temperature of the tower bottom is 75-85 ℃, the temperature of the tower top is 42-48 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the reflux ratio is more than or equal to 0.8;
the reaction conditions of the cyclohexane separation column (23) include: the temperature of the tower bottom is 90-110 ℃, the temperature of the tower top is 85-95 ℃, the pressure drop of the whole tower is 0.01-0.04MPa, and the reflux ratio of the tower top is more than or equal to 3.0; the reaction conditions of the cyclohexene rectifying column (24) include: the temperature of the tower bottom is 130-150 ℃, the temperature of the tower top is 42-50 ℃, the vacuum degree of the whole tower is more than or equal to 0.03MPa, and the molar reflux ratio of the tower top is more than or equal to 0.8.
2. The cyclohexene energy-saving production system according to claim 1, wherein the solid phase outlet of the settling tank (42) is connected with the reaction kettle (10) through a pipe.
3. The cyclohexene energy-saving production system according to claim 1, further comprising an extractant storage tank (43), wherein an inlet of the extractant storage tank (43) is connected to the first reboiler (32) and the third heat exchanger (34), respectively, and an outlet of the extractant storage tank (43) is connected to an inlet of the extractant adding device (44).
4. A cyclohexene energy-saving production system according to claim 3, wherein the benzene adding device comprises a benzene storage tank (41), and a refined benzene pipeline and a circulating benzene pipeline which are respectively connected with an inlet of the benzene storage tank (41), and the circulating benzene pipeline is connected with an outlet of the top of the benzene rectifying tower (22).
5. The cyclohexene energy-saving production system according to claim 4, wherein the hydrogenation device comprises a hydrogen input pipeline and a hydrogen circulation pipeline, the hydrogen input pipeline and the hydrogen circulation pipeline are connected with an inlet of the reaction kettle (10) through a booster pump (60), and the hydrogen circulation pipeline is connected with a hydrogen outlet of the reaction kettle (10).
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