CN210367490U - Gas phase hydrogenation reaction device for octenal - Google Patents
Gas phase hydrogenation reaction device for octenal Download PDFInfo
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- CN210367490U CN210367490U CN201921389012.2U CN201921389012U CN210367490U CN 210367490 U CN210367490 U CN 210367490U CN 201921389012 U CN201921389012 U CN 201921389012U CN 210367490 U CN210367490 U CN 210367490U
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Abstract
The utility model belongs to the technical field of chemical industry equipment, concretely relates to octenal gaseous phase hydrogenation device. The device comprises a hydrogen input pipeline, a hydrogen heater, a gas stripping evaporator, a heater, a hydrogenation converter, a heat exchanger, a condenser and a gas-liquid separator which are sequentially connected, wherein a multi-stream heat exchanger is arranged between the heat exchanger and the condenser, circulating gas at the temperature of about 120 ℃ at the outlet of the heat exchanger is fed into the multi-stream heat exchanger for secondary heat exchange, excessive heat is taken out and used for heating two cold materials, one cold material is fed into the evaporator, and the other cold material is used for heating the condensed materials. And finally, the circulating gas is condensed and separated from the liquid by a condenser, the separated target product enters a subsequent rectification system after heat exchange, and the circulating gas is used as a carrier, enters a circulating gas compressor for compression, is heated by a heat exchanger and then enters an air stripping evaporator for continuous circulation. The utility model discloses the condensation is effectual, and energy-conserving effect is showing, can reduce steam and circulating water unit consumption.
Description
Technical Field
The utility model belongs to the technical field of chemical industry equipment, concretely relates to octenal gaseous phase hydrogenation device.
Background
The hydrogenation process is common in chemical industry, and is an exothermic reaction, and hydrogen and raw materials produce target products under the action of a catalyst. The hydrogenation system is a closed circulation system, mainly comprising evaporation, reaction, condensation, pressurization and the like, hydrogen is used as a raw material and a carrier to circulate in a loop, the temperature is raised in front of an evaporator in the circulation process, better reaction conditions are provided for subsequent working sections, hydrogenation reaction is carried out on the hydrogen in a hydrogenation converter, the reaction heat is taken away by the circulating gas, products are separated out through heat exchange and condensation, and the circulating gas returns to the evaporator for continuous circulation.
The circulating gas is powered by a compressor, and a certain hydrogen concentration is maintained by supplementing hydrogen, so that the normal operation of the hydrogenation reaction is ensured. The evaporation section is mainly based on the stripping of heated hydrogen and the heating of a reboiler at the bottom, and the bottom temperature of the evaporator is controlled to be over 140 ℃ so as to ensure that effective components are not discharged along with heavy components. The condensation section mainly carries out condensation after heat exchange, and in order to better condense and remove products, the temperature after condensation is below 50 ℃ as much as possible so as to ensure that effective components are collected as much as possible. The whole hydrogenation process can affect the condensation effect along with higher load or high summer temperature. If the condensing effect is not good, gas with liquid can appear, the compressor inlet can cavitation erosion occur to the compressor self has the high temperature interlocking, if the condensing effect is not good will trigger the interlocking and lead to stopping.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an octenal gaseous phase hydrogenation reaction unit, simple structure, reasonable in design, the condensation is effectual, can not cause the interlocking, can also reduce effective component and smuggle the loss secretly to the protection compressor, energy-conserving effect is showing, can reduce steam and circulating water unit consumption.
The utility model provides a technical scheme that its technical problem adopted is:
the octenal gas phase hydrogenation reaction device comprises a hydrogen input pipeline, a hydrogen heater, a gas stripping evaporator, a heater, a hydrogenation converter, a heat exchanger, a condenser and a gas-liquid separator which are sequentially connected, wherein a multi-stream heat exchanger is arranged between the heat exchanger and the condenser and comprises a heat source inlet, a heat source outlet, two cold source inlets a and b and two cold source outlets a and b;
the hydrogenation converter is connected with a heat source inlet of the heat exchanger, a heat source outlet of the heat exchanger is connected with a heat source inlet of the multi-flow heat exchanger, and a heat source outlet of the multi-flow heat exchanger is connected with a condenser inlet; the circulating gas outlet of the gas-liquid separator is connected with the inlet of the circulating gas compressor, the outlet of the circulating gas compressor is connected with the cold source inlet of the heat exchanger, and the cold source outlet of the heat exchanger is connected with the circulating gas inlet of the air stripping evaporator;
the product outlet of the gas-liquid separator is connected with the cold source inlet a of the multi-stream heat exchanger, and the cold source outlet a of the multi-stream heat exchanger is connected with the rectification system;
and a cold source inlet b of the multi-flow heat exchanger is connected with a feed pipeline, and a cold source outlet b of the multi-flow heat exchanger is connected with a feed inlet of the air stripping evaporator.
Wherein:
the multi-flow heat exchanger is a novel spiral tube heat exchanger.
The working principle and the process are as follows:
the hydrogenation system is a closed circulation system and mainly comprises evaporation, reaction, condensation, pressurization and the like, and hydrogen is used as a raw material and a carrier to circulate in a loop. The system can continuously supplement hydrogen through a hydrogen input pipeline, the hydrogen is heated to about 138 ℃ through a hydrogen heater, the heated hydrogen and the circulating gas enter a stripping evaporator, the hot circulating gas and the raw material are evaporated and stripped in the stripping evaporator, the raw material is taken out as an effective component carried by the hot circulating gas and is heated to about 155 ℃ through an outlet heater, the gas is ensured not to carry liquid, and the gas enters a hydrogenation converter, and the hydrogen and the raw material react under the action of a catalyst to produce a target product. The hot spot temperature of the hydro-converter is about 270 ℃, and the heat quantity is more. Part of the heat generated by the reaction is taken away by a steam drum at the shell side of the hydro-converter to generate low-pressure steam which is merged into a steam pipe network; the other part is carried away by the recycle gas. After a part of heat taken away by the circulating gas is taken out through heat exchange of the heat exchanger, the circulating gas at the outlet of the heat exchanger can be reduced by about 30 ℃, the taken-out part of heat is used for heating the circulating gas at the outlet of the circulating gas compressor, the circulating gas can be approximately improved by about 25 ℃, the circulating gas at the outlet of the heat exchanger is about 120 ℃, and the heat is still a higher load for a subsequent condenser, so that the heat is further processed.
Before the circulating gas gets into the condenser, for reducing condenser load and take out partly heat again, set up the multiple stream heat exchanger between heat exchanger and condenser for take out too much heat, because the circulating gas circulation volume is great, ordinary shell and tube heat exchanger can not satisfy the requirement, so adopt novel spiral pipe heat exchanger, and according to actual operation technology, selected the multiple stream heat exchanger, promptly: two or more materials and one input material are used for heat exchange, and heat is taken out to achieve heat conservation and balance.
The circulating gas with the temperature of about 120 ℃ at the outlet of the heat exchanger is sent to a multi-flow heat exchanger for secondary heat exchange, and excessive heat is taken out for heating two cold materials, one is feeding of an evaporator, and the other is heating of the condensed material (target product). The outlet temperature of the multi-stream heat exchanger is about 100 ℃, finally, the liquid is condensed and separated by the circulating gas through the condenser, the separated target product enters a subsequent rectification system after heat exchange, the circulating gas is used as a carrier and enters a circulating gas compressor for compression, and the circulating gas enters a gas stripping evaporator after being heated by the heat exchanger for continuous circulation.
After the two cold materials are heated by the multi-stream heat exchanger, the heating temperature of the raw materials can be increased by about 45 ℃, the raw materials are heated to be beneficial to reboiling evaporation and gas stripping of a gas stripping evaporator, the steam consumption of a reboiler can be reduced, and the same evaporation and gas stripping effects are achieved. The heating of the target product can be increased by about 50 ℃, and the target product enters a subsequent rectification system after being heated, and the steam consumption is also reduced.
The multi-flow heat exchanger integrates multiple fluids, can simultaneously realize heat exchange among the multiple fluids, can realize the functions of a two-flow heat exchanger network, has the advantages of compact structure, high heat exchange efficiency, low equipment investment cost and the like which are not possessed by the two-flow heat exchanger network, and is widely applied to the industrial fields of low temperature, petrochemical industry, aviation, vehicles, power machinery, electronics, atomic energy, space navigation and the like at present.
The plate type and plate fin type heat exchangers in the high-efficiency heat exchanger can be arranged into a multi-flow heat exchanger with different channel arrangements according to requirements, one or more cold (hot) fluids can simultaneously cool (heat) other one or more hot (cold) fluids, and therefore the effect of a plurality of two-flow heat exchangers or a heat exchange network is achieved.
The utility model has the advantages that:
1. the utility model discloses simple structure, reasonable in design sets up the multiple stream heat exchanger between heat exchanger and condenser, takies away a part heat back away at original heat exchanger, takes out a part heat again by the multiple stream heat exchanger, just so can reduce the condenser load, can guarantee can not cause the interlocking, can also reduce effective component and smuggle the loss secretly to the protection compressor. The taken heat is used for heating two cold materials, one is fed by the gas stripping evaporator, and the steam consumption of a reboiler at the bottom can be reduced after the feeding and heating are carried out, so that the steam is saved; and the other strand is used for heating the condensed material, and the condensed material is subjected to a subsequent rectification unit, so that the steam can be saved.
2. The utility model discloses a production technology of energy consumption is practiced thrift in the high-efficient heat transfer of heterogeneous material, and double-phase cold material reduces steam and circulating water unit consumption with the heat material heat transfer. Two-phase cold materials and hot materials are adopted for heat exchange, and the unit consumption of steam and circulating water is reduced.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a schematic structural diagram of a comparative example of the present invention;
in the figure: 1. a hydrogen input line; 2. a hydrogen heater; 3. a stripping evaporator; 4. a heater; 5. a hydroconversion vessel; 6. a heat exchanger; 7. a condenser; 8. a gas-liquid separator; 9. a multi-stream heat exchanger; 10. a recycle gas compressor; 11. a rectification system; 12. a feed line.
Detailed Description
The embodiments of the present invention will be further explained with reference to the accompanying drawings:
examples
As shown in fig. 1, the octenal gas phase hydrogenation reaction apparatus comprises a hydrogen input pipeline 1, a hydrogen heater 2, a stripping evaporator 3, a heater 4, a hydrogenation converter 5, a heat exchanger 6, a condenser 7 and a gas-liquid separator 8 which are connected in sequence, wherein a multi-stream heat exchanger 9 is arranged between the heat exchanger 6 and the condenser 7, and the multi-stream heat exchanger 9 comprises a heat source inlet, a heat source outlet, two cold source inlets a and b and two cold source outlets a and b;
the hydrogenation converter 5 is connected with a heat source inlet of a heat exchanger 6, a heat source outlet of the heat exchanger 6 is connected with a heat source inlet of a multi-flow heat exchanger 9, and a heat source outlet of the multi-flow heat exchanger 9 is connected with an inlet of a condenser 7; a circulating gas outlet of the gas-liquid separator 8 is connected with an inlet of a circulating gas compressor 10, an outlet of the circulating gas compressor 10 is connected with a cold source inlet of the heat exchanger 6, and a cold source outlet of the heat exchanger 6 is connected with a circulating gas inlet of the air stripping evaporator 3;
a product outlet of the gas-liquid separator 8 is connected with a cold source inlet a of the multi-stream heat exchanger 9, and a cold source outlet a of the multi-stream heat exchanger 9 is connected with the rectification system 11;
the cold source inlet b of the multi-flow heat exchanger 9 is connected with the feeding pipeline 12, and the cold source outlet b of the multi-flow heat exchanger 9 is connected with the feeding hole of the air stripping evaporator 3.
Wherein:
the multi-stream heat exchanger 9 is a novel spiral tube heat exchanger 6.
The hydrogenation system is a closed circulation system and mainly comprises evaporation, reaction, condensation, pressurization and the like, and hydrogen is used as a raw material and a carrier to circulate in a loop. The system can continuously supplement hydrogen through a hydrogen input pipeline 1, the hydrogen is heated to about 138 ℃ through a hydrogen heater 2, the heated hydrogen and circulating gas enter a gas stripping evaporator 3, the hot circulating gas and raw materials are evaporated and stripped in the gas stripping evaporator 3, the raw materials are taken out as entrained effective components, the raw materials are heated to about 155 ℃ through an outlet heater 4, the gas is ensured not to carry liquid, the gas enters a hydrogenation converter 5, and the hydrogen and the raw materials react under the action of a catalyst to produce a target product. The hot spot temperature of the hydrogenation converter 5 is about 270 ℃, and the heat quantity is large. Part of the heat generated by the reaction is taken away by a steam drum at the shell side of the hydrogenation converter 5 to generate low-pressure steam which is merged into a steam pipe network; the other part is carried away by the recycle gas. After a part of the heat taken away by the circulating gas is taken out through heat exchange of the heat exchanger 6, the temperature of the circulating gas at the outlet of the heat exchanger 6 can be reduced by about 30 ℃, the taken-out part of the heat is used for heating the circulating gas at the outlet of the circulating gas compressor 10, the circulating gas can be approximately raised by about 25 ℃, the circulating gas at the outlet of the heat exchanger 6 is about 120 ℃, and the subsequent condenser 7 is still subjected to higher load, so that the circulating gas is further processed.
Before the circulating gas gets into condenser 7, for reducing condenser 7 load and take out partly heat again, set up the heat exchanger 9 that flows of many shares between heat exchanger 6 and condenser 7 for take out too much heat, because the circulating gas circulation volume is great, ordinary shell and tube heat exchanger 6 can not satisfy the requirement, so adopt novel spiral pipe heat exchanger 6, and according to actual operation technology, selected many shares and flowed heat exchanger 9, promptly: two or more materials and one input material are used for heat exchange, and heat is taken out to achieve heat conservation and balance.
The circulating gas at the outlet of the heat exchanger 6 at about 120 ℃ is sent to the multi-flow heat exchanger 9 for secondary heat exchange, and the excessive heat is taken out for heating two cold materials, one is feeding of the evaporator, and the other is heating of the condensed material (target product). The outlet temperature of the multi-stream heat exchanger 9 is about 100 ℃, finally, the liquid is condensed and separated by the circulating gas through the condenser 7, the separated target product enters the subsequent rectification system 11 after heat exchange, the circulating gas is used as a carrier and enters the circulating gas compressor 10 for compression, and the circulating gas enters the gas stripping evaporator 3 for continuous circulation after being heated by the heat exchanger 6.
After the two cold materials are heated by the multi-stream heat exchanger 9, the temperature of the raw materials can be increased by about 45 ℃, the raw materials are heated to be beneficial to reboiling evaporation and gas stripping of the gas stripping evaporator 3, the steam consumption of a reboiler can be reduced, and the same evaporation and gas stripping effects are achieved. The heating of the target product can be increased by about 50 ℃, and the target product enters the subsequent rectification system 11 after being heated, and the steam consumption is also reduced.
The multi-flow heat exchanger 9 integrates multiple fluids, can simultaneously realize heat exchange among the multiple fluids, can realize the function of the two-flow heat exchanger 6 network, has the advantages of compact structure, high heat exchange efficiency, low equipment investment cost and the like which are not possessed by the two-flow heat exchanger 6 network, and is widely applied to the industrial fields of low temperature, petrochemical industry, aviation, vehicles, power machinery, electronics, atomic energy, space navigation and the like at present.
The plate-type and plate-fin heat exchangers 6 in the high-efficiency heat exchanger 6 can be arranged into a plurality of flow heat exchangers 9 with different channel arrangements according to requirements, and one or more cold (hot) fluids can simultaneously cool (heat) other one or more hot (cold) fluids, so that the plate-type and plate-fin heat exchangers 6 play a role of a plurality of two-flow heat exchangers 6 or a heat exchange network.
Comparative example
As shown in fig. 2, the octenal gas phase hydrogenation reaction apparatus comprises a hydrogen input pipeline 1, a hydrogen heater 2, a stripping evaporator 3, a heater 4, a hydrogenation converter 5, a heat exchanger 6, a condenser 7 and a gas-liquid separator 8 which are connected in sequence;
the hydrogenation converter 5 is connected with a heat source inlet of a heat exchanger 6, and a heat source outlet of the heat exchanger 6 is connected with an inlet of a condenser 7; a circulating gas outlet of the gas-liquid separator 8 is connected with an inlet of a circulating gas compressor 10, an outlet of the circulating gas compressor 10 is connected with a cold source inlet of the heat exchanger 6, and a cold source outlet of the heat exchanger 6 is connected with a circulating gas inlet of the air stripping evaporator 3;
the product outlet of the gas-liquid separator 8 is connected with a rectification system 11;
the feed line 12 is connected to the feed inlet of the stripping evaporator 3.
The hydrogenation system is a closed circulation system and mainly comprises evaporation, reaction, condensation, pressurization and the like, and hydrogen is used as a raw material and a carrier to circulate in a loop. The system can continuously supplement hydrogen through a hydrogen input pipeline 1, the hydrogen is heated to about 138 ℃ through a hydrogen heater 2, the heated hydrogen and circulating gas enter a gas stripping evaporator 3, the hot circulating gas and raw materials are evaporated and stripped in the gas stripping evaporator 3, the raw materials are taken out as entrained effective components, the raw materials are heated to about 155 ℃ through an outlet heater 4, the gas is ensured not to carry liquid, the gas enters a hydrogenation converter 5, and the hydrogen and the raw materials react under the action of a catalyst to produce a target product. The hot spot temperature of the hydrogenation converter 5 is about 270 ℃, and the heat quantity is large. Part of the heat generated by the reaction is taken away by a steam drum at the shell side of the hydrogenation converter 5 to generate low-pressure steam which is merged into a steam pipe network; the other part is carried away by the recycle gas. The heat taken away by the circulating gas is partially taken out through heat exchange of the heat exchanger 6, the circulating gas at the outlet of the heat exchanger 6 can be reduced by about 30 ℃, the taken-out heat is used for heating the circulating gas at the outlet of the circulating gas compressor 10, the circulating gas can be approximately raised by about 25 ℃, the circulating gas at the outlet of the heat exchanger 6 at about 120 ℃ enters the condenser 7 for condensation, the circulating gas is separated by condensing the liquid through the condenser 7, the separated target product enters the subsequent rectification system 11, the circulating gas is used as a carrier and enters the circulating gas compressor 10 for compression, and the circulating gas enters the gas stripping evaporator 3 for continuous circulation after being heated through the heat exchanger 6.
According to the design parameters of the device, in order to protect the circulating gas compressor 10, the temperature of the circulating gas is required to be below 50 ℃ as much as possible after the material is condensed by the gas-liquid separator 8, so as to protect the impeller of the circulating gas compressor 10 from cavitation erosion. The recycle gas as carrier is pressurized by the recycle gas compressor 10 and then starts to circulate, the recycle gas amount is controlled to be about 27000kg/h, and the recycle gas is circulated in a closed loop. The system can continuously supplement hydrogen, the temperature of the heated hydrogen is controlled to be about 138 ℃, and the hydrogen amount is 7000NM2/h。
The test is carried out by adopting the devices of the examples and the comparative examples respectively, and the comparison condition of the product quality of the production process is shown in the table 1. Table 1 table comparing the quality of the examples with the quality of the comparative products.
| Inspection index | Comparative example Process parameters | Example Process parameters |
| Evaporator steam usage | 3300kg/h | 2500kg/h |
| Amount of distillation steam | 3350kg/h | 2700kg/h |
| Temperature after condensation (3 months) | 48℃ | 39℃ |
| Condenser circulating water hand valve opening | 100％ | 20％ |
Claims (2)
1. A gas phase hydrogenation reaction device for octenal is characterized in that: the device comprises a hydrogen input pipeline (1), a hydrogen heater (2), a gas stripping evaporator (3), a heater (4), a hydrogenation converter (5), a heat exchanger (6), a condenser (7) and a gas-liquid separator (8) which are sequentially connected, wherein a multi-flow heat exchanger (9) is arranged between the heat exchanger (6) and the condenser (7), and the multi-flow heat exchanger (9) comprises a heat source inlet, a heat source outlet, two cold source inlets a and b and two cold source outlets a and b;
the hydrogenation converter (5) is connected with a heat source inlet of the heat exchanger (6), a heat source outlet of the heat exchanger (6) is connected with a heat source inlet of the multi-stream heat exchanger (9), and a heat source outlet of the multi-stream heat exchanger (9) is connected with an inlet of the condenser (7); a circulating gas outlet of the gas-liquid separator (8) is connected with an inlet of a circulating gas compressor (10), an outlet of the circulating gas compressor (10) is connected with a cold source inlet of the heat exchanger (6), and a cold source outlet of the heat exchanger (6) is connected with a circulating gas inlet of the air stripping evaporator (3);
a product outlet of the gas-liquid separator (8) is connected with a cold source inlet a of the multi-stream heat exchanger (9), and a cold source outlet a of the multi-stream heat exchanger (9) is connected with the rectification system (11);
and a cold source inlet b of the multi-flow heat exchanger (9) is connected with the feeding pipeline (12), and a cold source outlet b of the multi-flow heat exchanger (9) is connected with a feeding hole of the air stripping evaporator (3).
2. The octenal gas-phase hydrogenation reaction unit according to claim 1, characterized in that: the multi-stream heat exchanger (9) is a novel spiral tube heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921389012.2U CN210367490U (en) | 2019-08-23 | 2019-08-23 | Gas phase hydrogenation reaction device for octenal |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921389012.2U CN210367490U (en) | 2019-08-23 | 2019-08-23 | Gas phase hydrogenation reaction device for octenal |
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| CN210367490U true CN210367490U (en) | 2020-04-21 |
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| CN201921389012.2U Active CN210367490U (en) | 2019-08-23 | 2019-08-23 | Gas phase hydrogenation reaction device for octenal |
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