CN112079696A - Energy-saving device and process for cyclohexanol dehydrogenation reaction in cyclohexanone production process - Google Patents
Energy-saving device and process for cyclohexanol dehydrogenation reaction in cyclohexanone production process Download PDFInfo
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- CN112079696A CN112079696A CN202011029103.2A CN202011029103A CN112079696A CN 112079696 A CN112079696 A CN 112079696A CN 202011029103 A CN202011029103 A CN 202011029103A CN 112079696 A CN112079696 A CN 112079696A
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- cyclohexanol
- crude alcohol
- alcohol ketone
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- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 title claims abstract description 219
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 179
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- -1 alcohol ketone Chemical class 0.000 claims abstract description 173
- 239000007789 gas Substances 0.000 claims abstract description 68
- 239000012495 reaction gas Substances 0.000 claims abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000007791 liquid phase Substances 0.000 claims abstract description 35
- 230000003647 oxidation Effects 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 22
- 239000000498 cooling water Substances 0.000 claims abstract description 19
- 238000001035 drying Methods 0.000 claims abstract description 19
- 239000001257 hydrogen Substances 0.000 claims abstract description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- 238000000926 separation method Methods 0.000 claims abstract description 17
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 claims abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000010521 absorption reaction Methods 0.000 claims abstract description 14
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 239000011368 organic material Substances 0.000 claims abstract description 4
- 239000012071 phase Substances 0.000 claims description 40
- 238000001704 evaporation Methods 0.000 claims description 17
- 230000008020 evaporation Effects 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 17
- 239000006227 byproduct Substances 0.000 claims description 11
- 239000003507 refrigerant Substances 0.000 claims description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 5
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 4
- 230000002745 absorbent Effects 0.000 claims description 3
- 239000002250 absorbent Substances 0.000 claims description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims 2
- 238000005192 partition Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
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- 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
- C07C45/002—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by dehydrogenation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0022—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for chemical reactors
-
- 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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- Engineering & Computer Science (AREA)
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- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to an energy-saving device and a process for cyclohexanol dehydrogenation reaction in the cyclohexanone production process, wherein high-temperature reaction gas from a cyclohexanol dehydrogenation reactor exchanges heat with feeding of the dehydrogenation reactor, liquid-phase cyclohexanol, hot water, low-temperature crude cyclohexanone entering a drying tower or a light tower, circulating cooling water and chilled water in sequence to reach the temperature required by separation of hydrogen and organic materials; collecting reaction gas condensate in two sections according to temperature, wherein low-temperature crude alcohol ketone is generated by cooling circulating cooling water and chilled water, and high-temperature crude alcohol ketone is generated by other heat exchange; in the cyclohexane oxidation device, part of low-temperature crude alcohol ketone is directly sent to an oxidation tail gas absorption tower, the rest low-temperature crude alcohol ketone exchanges heat with dehydrogenation reaction gas and then enters a drying tower, and high-temperature crude alcohol ketone enters a light tower; in the cyclohexene method device, the low-temperature crude alcohol ketone and the dehydrogenation reaction gas exchange heat and then respectively enter the light tower from different tower plate positions with the high-temperature crude alcohol ketone, so that the energy requirement of the rectification of the drying tower or the light tower is reduced. The invention fully utilizes the heat of the dehydrogenation reaction gas and reduces the energy consumption of the cyclohexanone device.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and relates to an energy-saving device and process for cyclohexanol dehydrogenation reaction in a cyclohexanone production process.
Background
In the production process of cyclohexanone, cyclohexanol dehydrogenation reaction is that cyclohexanol is subjected to dehydrogenation reaction at 220-270 ℃ and low pressure under the action of a catalyst to generate hydrogen and cyclohexanone. The temperature of reaction gas at the outlet of the dehydrogenation reactor reaches 220-270 ℃, the reaction gas is respectively used for heat exchange with the feeding material of the dehydrogenation reactor and liquid-phase cyclohexanol in the prior art, the temperature of the reaction gas after heat exchange is 140-150 ℃, and then circulating cooling water and frozen water are directly adopted for cooling to reach the temperature required by the separation of hydrogen and organic materials. The heat of dehydrogenation reaction in the prior production process is not fully utilized, and the consumption of circulating cooling water is higher.
In the prior art, the dehydrogenation reaction gas is subjected to heat exchange, cooling and condensation to generate condensate, the condensate is collected in a crude alcohol ketone product tank, and the temperature of crude alcohol ketone in the crude alcohol ketone product tank is about 90 ℃; the high-temperature section condensate collected by the tank is mixed with the low-temperature section condensate to be directly cooled, the low-temperature section condensate is heated, a small part of light components are gasified and returned to the condenser, and the consumption of circulating cooling water and chilled water is increased; meanwhile, for a cyclohexane oxidation device, a part of crude alcohol ketone in a crude alcohol ketone product tank is used as an absorbent of an oxidation tail gas absorption tower in an oxidation unit and needs to be cooled to about 10 ℃ and then enters the absorption tower, the temperature of the crude alcohol ketone generated by the existing device process technology is higher, and the cold consumption for cooling the crude alcohol ketone is increased.
Aiming at the problems, the invention fully utilizes the heat of dehydrogenation reaction gas and the process of separately collecting low-temperature crude alcohol ketone and high-temperature crude alcohol ketone, thereby reducing the energy consumption of the cyclohexanone device.
Disclosure of Invention
The invention aims to provide an energy-saving process for cyclohexanol dehydrogenation reaction in a cyclohexanone production process. The method fully utilizes the heat of dehydrogenation reaction gas, and reduces the energy consumption of a cyclohexanone device by a process of separately collecting low-temperature crude alcohol ketone and high-crude alcohol ketone, thereby reducing the production cost.
Technical scheme of the invention
In the production process of cyclohexanone, the dehydrogenation reaction of cyclohexanol is that cyclohexanol is subjected to dehydrogenation reaction at the temperature of 220-270 ℃ and under low pressure under the action of a catalyst to generate hydrogen and cyclohexanone, the temperature of reaction gas at the outlet of a dehydrogenation reactor reaches 220-270 ℃, the reaction gas is utilized to respectively exchange heat with feeding material of the dehydrogenation reactor and liquid-phase cyclohexanol, the reaction gas exchanges heat with hot water and then exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower, and the reaction gas after heat exchange is sequentially cooled by circulating cooling water and freezing water to reach the temperature required by separation of hydrogen and organic materials; the condensate of heat exchange between the reaction gas and the liquid-phase cyclohexanol and the condensate of heat exchange between the reaction gas and the hot water and the condensate of the reaction gas cooled by the circulating cooling water and the chilled water are separately collected, wherein the condensate of heat exchange between the reaction gas and the liquid-phase cyclohexanol is high-temperature crude alcohol ketone, and the condensate of heat exchange between the reaction gas and the hot water is low-. For a device for producing cyclohexanone by a cyclohexane oxidation method, part of low-temperature crude alcohol ketone is directly removed from an oxidation tail gas absorption tower, so that the cold consumption of cooling absorption feeding is reduced, the rest low-temperature crude alcohol ketone exchanges heat with dehydrogenation reaction gas after exchanging heat with hot water and then enters a drying tower, and the high-temperature crude alcohol ketone enters a light tower; for the device for producing cyclohexanone by the cyclohexene method, the low-temperature crude alcohol ketone and dehydrogenation reaction gas after heat exchange with hot water respectively enter the light tower at different tower plate positions after heat exchange with the high-temperature crude alcohol ketone.
The energy-saving device and process for dehydrogenation reaction of cyclohexanol of the present invention are further described below:
the device for producing cyclohexanone by cyclohexane oxidation adopts an energy-saving device and a process for dehydrogenation reaction of cyclohexanol as shown in figure 1:
the utility model provides an economizer of cyclohexanol dehydrogenation reaction in cyclohexanone production process, mainly by cyclohexanol dehydrogenation preheater, cyclohexanol dehydrogenation evaporimeter, cyclohexanol evaporation vapour-liquid knockout drum, cyclohexanol dehydrogenation heat exchanger, cyclohexanol dehydrogenation reactor, hot water heat exchanger, hot crude alcohol ketone jar, hot crude alcohol ketone pump, low temperature crude alcohol ketone heat exchanger, cyclohexanol dehydrogenation cooler, cyclohexanol dehydrogenation tail gas cooler, cold crude alcohol ketone jar, cold crude alcohol ketone pump constitute, its characterized in that: a cyclohexanol feeding pipeline is connected with a cyclohexanol dehydrogenation preheater, a gas phase outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a hot water heat exchanger, a liquid phase pipeline is connected with a crude alcohol ketone tank, and a cyclohexanol outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a cyclohexanol evaporator; a cyclohexanol evaporator is connected with a cyclohexanol evaporation vapor-liquid separation tank, a gas phase pipeline of the cyclohexanol evaporation vapor-liquid separation tank is connected with a cyclohexanol dehydrogenation reactor, and a liquid phase pipeline is connected with an alcohol tower; the outlet of the cyclohexanol dehydrogenation reactor is connected with a cyclohexanol dehydrogenation heat exchanger, and the middle of the outlet of the cyclohexanol dehydrogenation heat exchanger is connected with a gas phase inlet of a cyclohexanol preheater; a gas phase outlet of the hot water heat exchanger is connected with the low-temperature crude alcohol ketone heat exchanger, a gas phase outlet of the low-temperature crude alcohol ketone heat exchanger is connected with the cyclohexanol dehydrogenation cooler, a liquid phase outlet is connected with the hot alcohol ketone tank, a refrigerant side inlet of the cyclohexanol dehydrogenation cooler is connected with a cold crude alcohol ketone pump outlet, and a refrigerant side outlet of the cyclohexanol dehydrogenation cooler is connected with the drying tower; a gas phase outlet of the cyclohexanol dehydrogenation cooler is connected with a cyclohexanol dehydrogenation tail gas cooler, a liquid phase outlet is connected with a cold crude alcohol ketone tank, a gas phase outlet of the cyclohexanol dehydrogenation tail gas cooler is a hydrogen pipeline, and a liquid phase outlet is connected with the cold crude alcohol ketone tank; the cold crude alcohol ketone tank is connected with a cold crude alcohol ketone pump, and the outlet of the cold crude alcohol ketone pump is respectively connected with a low-temperature crude alcohol ketone heat exchanger and an oxidation tail gas absorption tower; the inlet of the hot crude alcohol ketone tank is respectively connected with the liquid phase outlets of the hot water heat exchanger and the low-temperature crude alcohol ketone heat exchanger, and the outlet of the hot crude alcohol ketone tank is connected with a hot crude alcohol ketone pump; the outlet of the hot crude alcohol ketone pump is connected with a light tower.
The method comprises the following steps of enabling raw material cyclohexanol to enter a cyclohexanol dehydrogenation preheater to exchange heat with dehydrogenation reaction gas, then heating the cyclohexanol dehydrogenation evaporator through steam, separating the heated cyclohexanol dehydrogenation evaporator through a cyclohexanol evaporation steam-liquid separation tank, heating a gas phase in a cyclohexanol dehydrogenation heat exchanger through the cyclohexanol dehydrogenation reaction gas, and then enabling the heated gas phase to enter a cyclohexanol dehydrogenation reactor. In a reactor, cyclohexanol is converted into cyclohexanone under the action of a catalyst, the converted reaction gas exchanges heat with gas-phase cyclohexanol through a cyclohexanol dehydrogenation heat exchanger, then exchanges heat with raw material cyclohexanol through a cyclohexanol dehydrogenation feed preheater, condensate is sent to a hot crude alcohol ketone tank, the reaction gas exchanges heat with hot water in a hot water heat exchanger, low-pressure steam or high-temperature hot water is produced as a byproduct, condensate of the reaction gas is sent to the hot crude alcohol ketone tank, the reaction gas after heat exchange exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower through a low-temperature crude alcohol ketone heat exchanger, the condensate is sent to the hot crude alcohol ketone tank, the hot crude alcohol ketone is sent to the light tower through a hot crude alcohol ketone pump, the reaction gas after heat exchange is sequentially cooled by circulating cooling water through a cyclohexanol dehydrogenation cooler and by cooling water through a cyclohexanol dehydrogenation tail gas cooler, most of the cyclohexanone and the cyclohexanol are condensed into a liquid phase, and then sent to a cold crude alcohol ketone tank, the noncondensable gas is mainly hydrogen and is sent to a hydrogen compressor. And pressurizing the cold crude alcohol ketone by a cold crude alcohol ketone pump, conveying part of the cold crude alcohol ketone to an oxidation tail gas absorption tower, and conveying the rest part of the cold crude alcohol ketone to a drying tower after exchanging heat with reaction gas after exchanging heat with hot water.
The device for producing cyclohexanone by cyclohexene method adopts an energy-saving device and a process of cyclohexanol dehydrogenation reaction as shown in figure 2, and the process comprises the following steps:
the utility model provides an economizer of cyclohexanol dehydrogenation reaction in cyclohexanone production process, mainly by cyclohexanol dehydrogenation preheater, cyclohexanol dehydrogenation evaporimeter, cyclohexanol evaporation vapour-liquid knockout drum, cyclohexanol dehydrogenation heat exchanger, cyclohexanol dehydrogenation reactor, hot water heat exchanger, hot crude alcohol ketone pump, low temperature crude alcohol ketone heat exchanger, cyclohexanol dehydrogenation cooler, cyclohexanol dehydrogenation tail gas cooler, crude alcohol ketone jar, cold crude alcohol ketone pump constitute, its characterized in that: a cyclohexanol feeding pipeline is connected with a cyclohexanol dehydrogenation preheater, a gas phase outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a hot water heat exchanger, a liquid phase pipeline is connected with a crude alcohol ketone tank, and a cyclohexanol outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a cyclohexanol evaporator; a cyclohexanol evaporator is connected with a cyclohexanol evaporation vapor-liquid separation tank, a gas phase pipeline of the cyclohexanol evaporation vapor-liquid separation tank is connected with a cyclohexanol dehydrogenation reactor, and a liquid phase pipeline is connected with an alcohol tower; the outlet of the cyclohexanol dehydrogenation reactor is connected with a cyclohexanol dehydrogenation heat exchanger, and the outlet of the cyclohexanol dehydrogenation heat exchanger is connected with the gas phase inlet of a cyclohexanol preheater; a gas phase outlet of the hot water heat exchanger is connected with the low-temperature crude alcohol ketone heat exchanger, a gas phase outlet of the low-temperature crude alcohol ketone heat exchanger is connected with the cyclohexanol dehydrogenation cooler, a liquid phase outlet is connected with the crude alcohol ketone tank, a refrigerant side inlet of the cyclohexanol dehydrogenation cooler is connected with a cold crude alcohol ketone pump outlet, and a refrigerant side outlet of the cyclohexanol dehydrogenation cooler is connected with the light tower; a gas phase outlet of the cyclohexanol dehydrogenation cooler is connected with the cyclohexanol dehydrogenation tail gas cooler, a liquid phase outlet is connected with the crude alcohol ketone tank, a gas phase outlet of the cyclohexanol dehydrogenation tail gas cooler is a hydrogen pipeline, and a liquid phase outlet is connected with the crude alcohol ketone tank; the crude alcohol ketone tank is respectively connected with a hot crude alcohol ketone pump and a cold crude alcohol ketone pump, the outlet of the hot crude alcohol ketone pump is connected with the light tower, and the outlet of the cold crude alcohol ketone pump is respectively connected with the low-temperature crude alcohol ketone heat exchanger.
The method comprises the following steps of enabling raw material cyclohexanol to enter a cyclohexanol dehydrogenation preheater to exchange heat with dehydrogenation reaction gas, then heating the cyclohexanol dehydrogenation evaporator through steam, separating the heated cyclohexanol dehydrogenation evaporator through a cyclohexanol evaporation steam-liquid separation tank, heating a gas phase in a cyclohexanol dehydrogenation heat exchanger through the cyclohexanol dehydrogenation reaction gas, and then enabling the heated gas phase to enter a cyclohexanol dehydrogenation reactor. In a reactor, cyclohexanol is converted into cyclohexanone under the action of a catalyst, the converted reaction gas exchanges heat with gas-phase cyclohexanol through a cyclohexanol dehydrogenation heat exchanger, then exchanges heat with raw material cyclohexanol through a cyclohexanol dehydrogenation feed preheater, condensate is sent to a hot crude alcohol ketone tank, the reaction gas exchanges heat with hot water in a hot water heat exchanger, low-pressure steam or high-temperature hot water is produced as a byproduct, condensate of the reaction gas is sent to the hot crude alcohol ketone tank, the reaction gas after heat exchange exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower through a low-temperature crude alcohol ketone heat exchanger, the condensate is sent to the hot crude alcohol ketone tank, the hot crude alcohol ketone is sent to the light tower through a hot crude alcohol ketone pump, the reaction gas after heat exchange is sequentially cooled by circulating cooling water through a cyclohexanol dehydrogenation cooler and by cooling water through a cyclohexanol dehydrogenation tail gas cooler, most of the cyclohexanone and the cyclohexanol are condensed into a liquid phase, and then sent to a cold crude alcohol ketone tank, the noncondensable gas is mainly hydrogen and is sent to a hydrogen compressor. The cold crude alcohol ketone is pressurized by a cold crude alcohol ketone pump, exchanges heat with the reaction gas after heat exchange with hot water, and then is sent to a light tower.
Features and effects of the invention
The invention fully utilizes the heat of dehydrogenation reaction gas, separately collects low-temperature crude alcohol ketone and high-crude alcohol ketone, and reduces the energy consumption of the cyclohexanone device, thereby reducing the production cost.
Drawings
FIG. 1 is a schematic diagram of an energy-saving apparatus for cyclohexanol dehydrogenation reaction in the process of producing cyclohexanone by oxidation of cyclohexane, FIG. 2 is a schematic diagram of an energy-saving apparatus for cyclohexanol dehydrogenation reaction in the process of producing cyclohexanone by oxidation of cyclohexane
In the figure: the system comprises a 1-cyclohexanol dehydrogenation preheater, a 2-cyclohexanol dehydrogenation evaporator, a 3-cyclohexanol evaporation vapor-liquid separation tank, a 4-cyclohexanol dehydrogenation heat exchanger, a 5-cyclohexanol dehydrogenation reactor, a 6-hot water heat exchanger, a 7-hot crude alcohol ketone pump, an 8-low-temperature crude alcohol ketone heat exchanger, a 9-cyclohexanol dehydrogenation cooler, a 10-cyclohexanol dehydrogenation tail gas cooler, an 11-crude alcohol ketone tank, an 11A-hot crude alcohol ketone tank, an 11B-cold crude alcohol ketone tank and a 12-cold crude alcohol ketone pump.
The 21-cyclohexanol comes from a tank field, 22-crude alcohol ketone and heavy components are sent to an alcohol tower, 23-hot crude alcohol ketone is sent to a light tower, 24A-hot crude alcohol ketone is sent to a drying tower, 24B-hot crude alcohol ketone is sent to the light tower, 25-hydrogen is sent to a compressor, and 26-cold alcohol ketone is sent to an oxidation tail gas absorption tower.
SH-high pressure steam CWS-recirculated cooling water RWS-chilled water LW-hot water HW-high temperature water LS-low pressure steam.
Detailed Description
The invention will be further described with reference to the accompanying drawings, which are not to be construed as limiting the invention.
Example 1:
a cyclohexanone device with 10 ten thousand tons of cyclohexane oxidation method produced every year, an energy-saving device for cyclohexanol dehydrogenation reaction and a process flow, as shown in figure 1.
The method comprises the following steps of enabling raw material cyclohexanol to enter a cyclohexanol dehydrogenation preheater (1) to exchange heat with dehydrogenation reaction gas to about 165 ℃, then enabling a cyclohexanol dehydrogenation evaporator (2) to be heated to about 173 ℃ through steam, enabling the cyclohexanol dehydrogenation evaporator to be separated through a cyclohexanol evaporation steam-liquid separation tank (3), enabling gas phase to be heated to 244 ℃ in a cyclohexanol dehydrogenation heat exchanger (4) through the cyclohexanol dehydrogenation reaction gas, and enabling the gas phase to enter a cyclohexanol dehydrogenation reactor (5). In a reactor, cyclohexanol is converted into cyclohexanone under the action of a catalyst, the converted reaction gas exchanges heat with gas-phase cyclohexanol to about 189 ℃ through a cyclohexanol dehydrogenation heat exchanger (4), then exchanges heat with raw material cyclohexanol to about 143 ℃ through a cyclohexanol dehydrogenation feed preheater (1), condensate is sent to a hot crude alcohol ketone tank (11A), the reaction gas exchanges heat with hot water in a hot water heat exchanger (6) to about 136 ℃, low-pressure steam or high-temperature hot water is byproduct, the reaction gas condensate is sent to the hot crude alcohol ketone tank (11A), the reaction gas after heat exchange exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower through a low-temperature crude alcohol ketone heat exchanger (8) to about 125 ℃, the condensate is sent to the hot crude alcohol ketone tank (11A), the hot crude alcohol ketone is sent to the light tower through a hot crude alcohol ketone pump (7), the reaction gas after heat exchange sequentially passes through a cyclohexanol dehydrogenation cooler (9) and is cooled to about 45 ℃ by circulating cooling water and is cooled to 20 by a cyclohexanol dehydrogenation tail gas cooler (10) through chilled water Condensing most of cyclohexanone and cyclohexanol at about deg.C to obtain liquid phase, and delivering to a cold crude alcohol ketone tank (11B), wherein the noncondensable gas is mainly hydrogen and is delivered to a hydrogen compressor. The cold crude alcohol ketone is pressurized by a cold crude alcohol ketone pump (12), part of the cold crude alcohol ketone is sent to a feeding cooler of an oxidation tail gas absorption tower, and the rest part of the cold crude alcohol ketone exchanges heat with reaction gas after heat exchange with hot water to 115 ℃ and is sent to a drying tower.
The invention can produce 0.2MPa.G low-pressure steam as a byproduct at 0.5t/h, and the consumption of the circulating cooling water of the cyclohexanol dehydrogenation cooler is reduced by 53 percent; the oxidized tail gas absorption feeding cooler saves energy consumption by 59 percent, and reduces steam consumption of the drying tower and the light tower by about 13 percent.
Example 2:
a device for producing 20 ten thousand tons of cyclohexene method cyclohexanone annually, an energy-saving device for cyclohexanol dehydrogenation reaction and a process flow, as shown in figure 2.
The method comprises the following steps of enabling raw material cyclohexanol to enter a cyclohexanol dehydrogenation preheater (1) to exchange heat with dehydrogenation reaction gas to about 165 ℃, then enabling a cyclohexanol dehydrogenation evaporator (2) to be heated to about 173 ℃ through steam, enabling the cyclohexanol dehydrogenation evaporator to be separated through a cyclohexanol evaporation steam-liquid separation tank (3), enabling gas phase to be heated to 244 ℃ in a cyclohexanol dehydrogenation heat exchanger (4) through the cyclohexanol dehydrogenation reaction gas, and enabling the gas phase to enter a cyclohexanol dehydrogenation reactor (5). In a reactor, cyclohexanol is converted into cyclohexanone under the action of a catalyst, the converted reaction gas exchanges heat with gas-phase cyclohexanol to about 189 ℃ through a cyclohexanol dehydrogenation heat exchanger (4), then exchanges heat with raw material cyclohexanol to about 143 ℃ through a cyclohexanol dehydrogenation feeding preheater (1), condensate is sent to the hot side of a crude alcohol ketone tank (11), the reaction gas exchanges heat with hot water in a hot water heat exchanger (6) to about 136 ℃, low-pressure steam or high-temperature hot water is produced as a byproduct, the condensate of the reaction gas is sent to the hot side of the crude alcohol ketone tank (11), the reaction gas after heat exchange exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower by a low-temperature crude alcohol ketone heat exchanger (8) to about 125 ℃, the condensate is sent to the hot side of the crude alcohol ketone tank (11), the hot crude alcohol ketone is sent to the light tower by a hot crude alcohol ketone pump (7), and the reaction gas after heat exchange is sequentially cooled to about 45 ℃ by circulating cooling water through a cyclohexanol dehydrogenation cooler (9) and cooled to 20) by cooling water through a cyclohexanol dehydrogenation tail gas cooler (10) Condensing most cyclohexanone and cyclohexanol at about deg.C to obtain liquid phase, delivering to cold side of crude alcohol ketone tank (11), and delivering noncondensable gas mainly containing hydrogen to hydrogen compressor. The cold crude alcohol ketone is pressurized by a cold crude alcohol ketone pump (12), and then exchanges heat with the reaction gas after heat exchange with hot water to 115 ℃, and the reaction gas is sent to a light tower.
The invention can produce a byproduct of low-pressure steam of 0.2MPa.G at 2 t/h; the consumption of circulating cooling water of the cyclohexanol dehydrogenation cooler is reduced by 53 percent; the steam consumption of the light tower is reduced by 15 percent.
Claims (10)
1. The utility model provides an economizer of cyclohexanol dehydrogenation reaction in cyclohexanone production process, mainly by cyclohexanol dehydrogenation preheater, cyclohexanol dehydrogenation evaporimeter, cyclohexanol evaporation vapour-liquid knockout drum, cyclohexanol dehydrogenation heat exchanger, cyclohexanol dehydrogenation reactor, hot water heat exchanger, hot crude alcohol ketone pump, low temperature crude alcohol ketone heat exchanger, cyclohexanol dehydrogenation cooler, cyclohexanol dehydrogenation tail gas cooler, crude alcohol ketone jar, cold crude alcohol ketone pump constitute, its characterized in that: a cyclohexanol feeding pipeline is connected with a cyclohexanol dehydrogenation preheater, a gas phase outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a hot water heat exchanger, a liquid phase pipeline is connected with a crude alcohol ketone tank, and a cyclohexanol outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a cyclohexanol evaporator; a cyclohexanol evaporator is connected with a cyclohexanol evaporation vapor-liquid separation tank, a gas phase pipeline of the cyclohexanol evaporation vapor-liquid separation tank is connected with a cyclohexanol dehydrogenation reactor, and a liquid phase pipeline is connected with an alcohol tower; the outlet of the cyclohexanol dehydrogenation reactor is connected with a cyclohexanol dehydrogenation heat exchanger, and the outlet of the cyclohexanol dehydrogenation heat exchanger is connected with the gas phase inlet of a cyclohexanol preheater; a gas phase outlet of the hot water heat exchanger is connected with the low-temperature crude alcohol ketone heat exchanger, a gas phase outlet of the low-temperature crude alcohol ketone heat exchanger is connected with the cyclohexanol dehydrogenation cooler, a liquid phase outlet is connected with the crude alcohol ketone tank, a refrigerant side inlet of the cyclohexanol dehydrogenation cooler is connected with a cold crude alcohol ketone pump outlet, and a refrigerant side outlet of the cyclohexanol dehydrogenation cooler is connected with the light tower; a gas phase outlet of the cyclohexanol dehydrogenation cooler is connected with the cyclohexanol dehydrogenation tail gas cooler, a liquid phase outlet is connected with the crude alcohol ketone tank, a gas phase outlet of the cyclohexanol dehydrogenation tail gas cooler is a hydrogen pipeline, and a liquid phase outlet is connected with the crude alcohol ketone tank; the crude alcohol ketone tank is respectively connected with a hot crude alcohol ketone pump and a cold crude alcohol ketone pump, the outlet of the hot crude alcohol ketone pump is connected with the light tower, and the outlet of the cold crude alcohol ketone pump is respectively connected with the low-temperature crude alcohol ketone heat exchanger.
2. The apparatus of claim 1, wherein the apparatus is used for the dehydrogenation of cyclohexanol in the production of cyclohexanone by cyclohexene process or for the dehydrogenation of cyclohexanol in the production of cyclohexanone by phenol process.
3. The utility model provides an economizer of cyclohexanol dehydrogenation reaction in cyclohexanone production process, mainly by cyclohexanol dehydrogenation preheater, cyclohexanol dehydrogenation evaporimeter, cyclohexanol evaporation vapour-liquid knockout drum, cyclohexanol dehydrogenation heat exchanger, cyclohexanol dehydrogenation reactor, hot water heat exchanger, hot crude alcohol ketone jar, hot crude alcohol ketone pump, low temperature crude alcohol ketone heat exchanger, cyclohexanol dehydrogenation cooler, cyclohexanol dehydrogenation tail gas cooler, cold crude alcohol ketone jar, cold crude alcohol ketone pump constitute, its characterized in that: a cyclohexanol feeding pipeline is connected with a cyclohexanol dehydrogenation preheater, a gas phase outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a hot water heat exchanger, a liquid phase pipeline is connected with a crude alcohol ketone tank, and a cyclohexanol outlet pipeline of the cyclohexanol dehydrogenation preheater is connected with a cyclohexanol evaporator; a cyclohexanol evaporator is connected with a cyclohexanol evaporation vapor-liquid separation tank, a gas phase pipeline of the cyclohexanol evaporation vapor-liquid separation tank is connected with a cyclohexanol dehydrogenation reactor, and a liquid phase pipeline is connected with an alcohol tower; the outlet of the cyclohexanol dehydrogenation reactor is connected with a cyclohexanol dehydrogenation heat exchanger, and the middle of the outlet of the cyclohexanol dehydrogenation heat exchanger is connected with a gas phase inlet of a cyclohexanol preheater; a gas phase outlet of the hot water heat exchanger is connected with the low-temperature crude alcohol ketone heat exchanger, a gas phase outlet of the low-temperature crude alcohol ketone heat exchanger is connected with the cyclohexanol dehydrogenation cooler, a liquid phase outlet is connected with the hot alcohol ketone tank, a refrigerant side inlet of the cyclohexanol dehydrogenation cooler is connected with a cold crude alcohol ketone pump outlet, and a refrigerant side outlet of the cyclohexanol dehydrogenation cooler is connected with the drying tower; a gas phase outlet of the cyclohexanol dehydrogenation cooler is connected with a cyclohexanol dehydrogenation tail gas cooler, a liquid phase outlet is connected with a cold crude alcohol ketone tank, a gas phase outlet of the cyclohexanol dehydrogenation tail gas cooler is a hydrogen pipeline, and a liquid phase outlet is connected with the cold crude alcohol ketone tank; the cold crude alcohol ketone tank is connected with a cold crude alcohol ketone pump, and the outlet of the cold crude alcohol ketone pump is respectively connected with a low-temperature crude alcohol ketone heat exchanger and an oxidation tail gas absorption tower; the inlet of the hot crude alcohol ketone tank is respectively connected with the liquid phase outlets of the hot water heat exchanger and the low-temperature crude alcohol ketone heat exchanger, and the outlet of the hot crude alcohol ketone tank is connected with a hot crude alcohol ketone pump; the outlet of the hot crude alcohol ketone pump is connected with a light tower.
4. The apparatus for saving energy in dehydrogenation reaction of cyclohexanol in production process of cyclohexanone according to claim 3, wherein the apparatus is an apparatus for saving energy in dehydrogenation reaction of cyclohexanol in production apparatus of cyclohexanone by oxidation of cyclohexane.
5. An energy-saving process for cyclohexanol dehydrogenation reaction in cyclohexanone production process, wherein reaction gas from a cyclohexanol dehydrogenation reactor exchanges heat with feed and liquid-phase cyclohexanol of the dehydrogenation reactor respectively, then exchanges heat with hot water to generate low-pressure steam or high-temperature hot water as a by-product, and then exchanges heat with low-temperature crude alcohol ketone entering a drying tower or a light tower, and the reaction gas after heat exchange is cooled by adopting circulating cooling water and chilled water in sequence to reach the temperature required by separation of hydrogen and organic materials; the condensate of heat exchange between the reaction gas and the liquid-phase cyclohexanol and the condensate of heat exchange between the reaction gas and the hot water and the condensate of the reaction gas cooled by the circulating cooling water and the chilled water are separately collected, wherein the condensate of heat exchange between the reaction gas and the liquid-phase cyclohexanol is high-temperature crude alcohol ketone, and the condensate of heat exchange between the reaction gas and the hot water is low-. For a device for producing cyclohexanone by a cyclohexane oxidation method, part of low-temperature crude alcohol ketone is directly removed from an oxidation tail gas absorption tower, so that the cold consumption of cooling absorption feeding is reduced, the rest low-temperature crude alcohol ketone exchanges heat with a dehydrogenation reaction gas which exchanges heat with hot water to generate a byproduct of low-pressure steam or high-temperature hot water and then enters a drying tower, and the high-temperature crude alcohol ketone enters a light tower; for the device for producing cyclohexanone by the cyclohexene method, the low-temperature crude alcohol ketone exchanges heat with the dehydrogenation reaction gas which exchanges heat with hot water and produces low-pressure steam or high-temperature hot water as a byproduct, and then the low-temperature crude alcohol ketone and the high-temperature crude alcohol ketone enter the light tower at different tower plate positions respectively.
6. The process of claim 5, wherein the reaction gas obtained by heat exchange between the cyclohexanol and the feed of the dehydrogenation reactor and the liquid-phase cyclohexanol can be used to exchange heat with hot water to produce low-pressure steam as a byproduct, or exchange heat with hot water to produce high-temperature hot water as a byproduct.
7. The energy-saving process for cyclohexanol dehydrogenation reaction in cyclohexanone production process according to claim 5, wherein the process is suitable for a device for producing cyclohexanone by cyclohexane oxidation method, a device for producing cyclohexanone by cyclohexene method, or a device for producing cyclohexanone by phenol method.
8. The energy-saving process for cyclohexanol dehydrogenation reaction in cyclohexanone production process according to claim 5, wherein for the device for producing cyclohexanone by cyclohexane oxidation, part of low-temperature crude alcohol ketone is directly removed from the oxidation tail gas absorption tower absorbent cooler, thereby reducing the cold consumption of cooling absorbent, the rest low-temperature crude alcohol ketone enters the drying tower after exchanging heat with dehydrogenation reaction gas after exchanging heat with hot water, and the high-temperature crude alcohol ketone enters the light tower.
9. The energy-saving process for cyclohexanol dehydrogenation reaction in the cyclohexanone production process according to claim 5, wherein in the device for producing cyclohexanone by cyclohexene method, the low-temperature crude alcohol ketone exchanges heat with the dehydrogenation reaction gas after heat exchange with hot water and then enters the drying tower or the high-temperature crude alcohol ketone enters the light tower at different tower plate positions.
10. The process of claim 5, wherein the high temperature crude alcohol ketone and the low temperature crude alcohol ketone are collected separately in the same vessel with internal partition plate or in two vessels.
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| CN111662160A (en) * | 2019-03-06 | 2020-09-15 | 中国石油化工股份有限公司 | Method for improving productivity of cyclohexanol dehydrogenation device |
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