CN105175302A - Unrelated tower differential pressure thermal coupling energy saving method of DCP (dicumyl peroxide) device - Google Patents
Unrelated tower differential pressure thermal coupling energy saving method of DCP (dicumyl peroxide) device Download PDFInfo
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Abstract
The invention relates to an unrelated tower differential pressure thermal coupling energy saving method of a DCP device and mainly solves the problem that the energy consumption is higher in the prior art. With the adoption of the unrelated tower differential pressure thermal coupling energy saving method of the DCP device, a material to recycle cumene in the DCP device enters a cumene recycling tower for recycling the cumene, a tower kettle solution is a heavy component by-product, a tower top gas phase material is divided into two streams, a first stream of the tower top gas phase material enters to a cumene recycling tower top middle tank, a second stream of the tower top gas phase material enters a benzyl alcohol tower reboiler as a benzyl alcohol tower kettle reboiler heating medium and cools and condenses after providing heat, and the second stream material and the first condensed stream material enter the cumene recycling tower top middle tank. With the adoption of the technical scheme, the problem can be well solved, and the method can be used in the DCP device.
Description
Technical field
The present invention relates to a kind of dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method.
Background technology
Rectifying is one of topmost separation method during petrochemical complex is produced, and traditional rectifying separation technical process exists the defects such as separating energy consumption is high, facility investment is large.At present, the tower reactor that dicumyl peroxide DCP device returns different tower and benzylalcohol tower needs extraneous steam source to provide heat respectively, and tower top needs extraneous recirculated cooling water low-temperature receiver to provide cold respectively.Although this technical process is simple, the energy of whole process unit can not be fully used, and thermodynamic(al) efficiency is lower, and energy consumption is higher thus.Number of patent application is novel method prepared by the thermal coupling of CN200410049923.2 ionic liquid, this invention describes the coupling between two or more ionic liquid synthesising reacting heats of comprehensive utilization, two or more ionic liquids can be prepared simultaneously, can Simplified flowsheet and equipment, reduce energy consumption, reduce production cost.Number of patent application is CN201410128451.3 sulfur oxychloride differential pressure heat coupling rectification method and apparatus, the invention provides the energy-saving technique that a kind of sulfur oxychloride is purified, adopt differential pressure heat coupling technique by thermal coupling at the bottom of weight-removing column tower top and lightness-removing column tower, compared with common process, reduce a considerable amount of energy consumption of rectifying separation process, save the input of outside energy.
Number of patent application CN200410049923.2 of the prior art is only the thermal coupling of reaction mass inside, does not relate to the rectifying separation of process unit material component, cannot apply on dicumyl peroxide DCP device.Although number of patent application CN201410128451.3 discloses the method for material rectifying separation, also need chemical reactor to add, have certain limitation, the isopropyl benzene purification or the benzylalcohol that also do not relate to dicumyl peroxide DCP device are refined.Thus, above-mentioned prior art exists cannot in the isopropyl benzene recovery system of dicumyl peroxide DCP device and the application of benzylalcohol refining system, Hui Yita and benzylalcohol tower are respectively with low-pressure steam heating and circulating cooling water condensation, and the thermal load of the material that boils again and the thermal load of condensation material such as cannot to match at the problem.
The present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that in prior art, energy consumption is higher, provides a kind of new dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method.The method is used for, in dicumyl peroxide DCP device, having the advantage that energy consumption is lower.
For solving the problem, the technical solution used in the present invention is as follows: a kind of dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method, in dicumyl peroxide DCP device, the material of isopropyl benzene to be recycled enters isopropyl benzene recovery tower and reclaims isopropyl benzene, tower bottoms is the heavy constituent by product comprising phenol tar, top gaseous phase material is divided into two strands, after first stock-traders' know-how returns different overhead condenser cooling condensation, enter back different tower top tundish, second strand enters benzylalcohol tower reboiler as benzylalcohol tower reactor reboiler heating medium material, after heat is provided, self is cooling condensation also, converge with first strand of material through condensation and enter back different tower top tundish, return the material of discharging in different tower top tundish and be divided into two strands after returning different trim the top of column pump, first strand returns isopropyl benzene recovery tower as phegma, second strand enters follow-up flow process as product separation.
In technique scheme, the operational condition of isopropyl benzene recovery tower is: tower top service temperature is 105 ~ 140 DEG C, and preferable range is 110 ~ 135 DEG C, and more preferably scope is 115 ~ 130 DEG C; Working pressure is 10 ~ 60kPaA, and preferable range is 15 ~ 55kPaA, and more preferably scope is 20 ~ 50kPaA.Tower reactor service temperature is 145 ~ 185 DEG C, and preferable range is 150 ~ 180 DEG C, and more preferably scope is 160 ~ 170 DEG C; Working pressure is 15 ~ 65kPaA, and preferable range is 20 ~ 60kPaA, and more preferably scope is 25 ~ 55kPaA.The operational condition of benzylalcohol tower is: tower top service temperature is 35 ~ 75 DEG C, and preferable range is 40 ~ 70 DEG C, and more preferably scope is 45 ~ 65 DEG C; Working pressure is 1 ~ 10kPaA, and preferable range is 2 ~ 8kPaA, and more preferably scope is 3 ~ 6kPaA.Tower reactor service temperature is 95 ~ 135 DEG C, and preferable range is 105 ~ 125 DEG C, and more preferably scope is 110 ~ 120 DEG C; Working pressure is 3 ~ 12kPaA, and preferable range is 4 ~ 10kPaA, and more preferably scope is 5 ~ 8kPaA.
In technique scheme, preferably, described isopropyl benzene recovery tower top gaseous phase material is divided into two strands, and first strand is 1.05 ~ 1.45:1 with the ratio of the mass rate of second strand.
In technique scheme, preferably, the material of discharging in described time different tower top tundish is divided into two strands after returning different trim the top of column pump, and first strand is 5.5 ~ 7.5:1 with the ratio of the mass rate of second strand.
The present invention is by optimizing back the operational condition of different tower and benzylalcohol tower, different column overhead material will be returned and benzylalcohol tower kettle material carries out heat exchange, benzylalcohol tower tower reactor reboiler does not need to consume low-pressure steam, return different column overhead condenser circulating cooling water consumption and reduce about 50%, thus, take full advantage of condensation material and the energy of the material that boils again, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1, isopropyl benzene recovery tower (be called for short Hui Yita); 2, benzylalcohol tower; 3, different overhead condenser is returned; 4, benzylalcohol tower reactor reboiler; 5, different tower top tundish are returned; 6, different trim the top of column pump is returned; 7, different top gaseous phase discharging is returned; 8, the discharging of different tower top liquid phase is returned; 9, different tower charging is returned; 10, the discharging of different tower reactor liquid phase is returned; 11, benzylalcohol tower top liquid phase discharging; 12, benzylalcohol tower charging; 13, benzylalcohol tower reactor liquid phase discharging.
In dicumyl peroxide DCP device, the material of isopropyl benzene to be recycled enters isopropyl benzene recovery tower (1) and reclaims isopropyl benzene, and tower bottoms is the heavy constituent by products such as phenol tar.Returning different top gaseous phase material (7) is divided into after two strands: one stock-traders' know-how returns different overhead condenser (3) cooling condensation, enter back different tower top tundish (5), another stock enters benzylalcohol tower reboiler (4) as benzylalcohol bottom reboiler heating medium material, after heat is provided, self is cooling condensation also, converges enter back different tower top tundish (5) with anterior divisions material.Converge after rear material leaves back different tower top tundish (5), two strands are divided into: one returns Hui Yita (1) as phegma through returning different trim the top of column pump (6), another stock returns different tower top liquid phase discharging (8) as product separation, enters follow-up flow process.Benzylalcohol tower (2) is provided with charging (12), and benzylalcohol tower (2) top is provided with liquid phase discharging (11), and bottom is provided with tower reactor liquid phase discharging (13).
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[comparative example 1]
Be 200 tons/year of DCP devices for industrial scale, the mass fraction that Hui Yita and benzylalcohol tower pass in and out material is as follows:
Hui Yita and benzylalcohol tower carry out overhead condensation by recirculated cooling water and low-pressure steam respectively and tower reactor is boiled again, its thermal load is respectively: return different column overhead condenser 10.55KW, return different tower tower reactor reboiler 10.24KW, benzylalcohol column overhead condenser 4.34KW, benzylalcohol tower tower reactor reboiler 4.40KW.
[embodiment 1]
Be 200 tons/year of DCP devices for industrial scale, the mass fraction that Hui Yita and benzylalcohol tower pass in and out material is as follows with the operational condition of comparative example 1, Hui Yita and benzylalcohol tower:
| Return different column overhead temperatures (DEG C) | 130 | Benzylalcohol column overhead temperatures (DEG C) | 65 |
| Return different column overhead pressure (kPaA) | 50 | Benzylalcohol column overhead pressure (kPaA) | 6 |
| Return different tower bottom temperature (DEG C) | 170 | Benzylalcohol tower bottom temperature (DEG C) | 120 |
| Return different tower tower reactor pressure (kPaA) | 55 | Benzylalcohol tower tower reactor pressure (kPaA) | 8 |
In addition, isopropyl benzene recovery tower top gaseous phase material is divided into two strands, and first strand is 1.20:1 with the ratio of the mass rate of second strand; Return the material of discharging in different tower top tundish and be divided into two strands after returning different trim the top of column pump, first strand is 6.0:1 with the ratio of the mass rate of second strand.
Different tower will be returned make differential thermal coupled with no pressure with benzylalcohol tower and be connected, benzylalcohol tower tower reactor reboiler does not need out-of-bounds low-pressure steam input, the energy returning a part of condensation of different column overhead condenser does not need recirculated cooling water, its thermal load is respectively: return different column overhead condenser 5.20KW, return different tower tower reactor reboiler 10.31KW, benzylalcohol column overhead condenser 4.34KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 45.83% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
[comparative example 2]
Be 1000 tons/year of DCP devices for industrial scale, Hui Yita and benzylalcohol tower pass in and out the mass fraction of material with comparative example 1, Hui Yita and benzylalcohol tower carry out overhead condensation by recirculated cooling water and low-pressure steam respectively and tower reactor is boiled again, its thermal load is respectively: return different column overhead condenser 52.77KW, return different tower tower reactor reboiler 51.22KW, benzylalcohol column overhead condenser 21.68KW, benzylalcohol tower tower reactor reboiler 21.99KW.
[embodiment 2]
Be 1000 tons/year of DCP devices for industrial scale, the mass fraction that Hui Yita and benzylalcohol tower pass in and out material with the operational condition of comparative example 1, Hui Yita and benzylalcohol tower with embodiment 1.To return different tower to make differential thermal coupled with no pressure with benzylalcohol tower and be connected, its thermal load is respectively: return different column overhead condenser 25.99KW, returns different tower tower reactor reboiler 51.56KW, benzylalcohol column overhead condenser 21.68KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 45.83% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
[comparative example 3]
Be 20,000 tons/year of DCP devices for industrial scale, Hui Yita and benzylalcohol tower pass in and out the mass fraction of material with comparative example 1, Hui Yita and benzylalcohol tower carry out overhead condensation by recirculated cooling water and low-pressure steam respectively and tower reactor is boiled again, its thermal load is respectively: return different column overhead condenser 1055.40KW, return different tower tower reactor reboiler 1024.45KW, benzylalcohol column overhead condenser 433.62KW, benzylalcohol tower tower reactor reboiler 439.85KW.
[embodiment 3]
Be 20,000 tons/year of DCP devices for industrial scale, the mass fraction that Hui Yita and benzylalcohol tower pass in and out material with the operational condition of comparative example 1, Hui Yita and benzylalcohol tower with embodiment 1.To return different tower to make differential thermal coupled with no pressure with benzylalcohol tower and be connected, its thermal load is respectively: return different column overhead condenser 519.83KW, returns different tower tower reactor reboiler 1031.22KW, benzylalcohol column overhead condenser 433.62KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 45.83% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
[comparative example 4]
Be 60,000 tons/year of DCP devices for industrial scale, Hui Yita and benzylalcohol tower pass in and out the mass fraction of material with comparative example 1, Hui Yita and benzylalcohol tower carry out overhead condensation by recirculated cooling water and low-pressure steam respectively and tower reactor is boiled again, its thermal load is respectively: return different column overhead condenser 3166.19KW, return different tower tower reactor reboiler 3073.36KW, benzylalcohol column overhead condenser 1300.86KW, benzylalcohol tower tower reactor reboiler 1319.56KW.
[embodiment 4]
Be 60,000 tons/year of DCP devices for industrial scale, the mass fraction that Hui Yita and benzylalcohol tower pass in and out material with the operational condition of comparative example 1, Hui Yita and benzylalcohol tower with embodiment 1.To return different tower to make differential thermal coupled with no pressure with benzylalcohol tower and be connected, its thermal load is respectively: return different column overhead condenser 1559.49KW, returns different tower tower reactor reboiler 3093.67KW, benzylalcohol column overhead condenser 1300.86KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 45.83% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
[comparative example 5]
According to the condition of comparative example 3, industrial scale is 20,000 tons/year of DCP devices.
[embodiment 5]
According to the condition of embodiment 3, be 20,000 tons/year of DCP devices for industrial scale, Hui Yita and benzylalcohol tower pass in and out the mass fraction of material with comparative example 1, and just operational condition changes, and the operational condition of Hui Yita and benzylalcohol tower is as follows:
| Return different column overhead temperatures (DEG C) | 105 | Benzylalcohol column overhead temperatures (DEG C) | 35 |
| Return different column overhead pressure (kPaA) | 10 | Benzylalcohol column overhead pressure (kPaA) | 1 |
| Return different tower bottom temperature (DEG C) | 145 | Benzylalcohol tower bottom temperature (DEG C) | 95 |
| Return different tower tower reactor pressure (kPaA) | 15 | Benzylalcohol tower tower reactor pressure (kPaA) | 3 |
In addition, isopropyl benzene recovery tower top gaseous phase material is divided into two strands, and first strand is 1.05:1 with the ratio of the mass rate of second strand; Return the material of discharging in different tower top tundish and be divided into two strands after returning different trim the top of column pump, first strand is 5.5:1 with the ratio of the mass rate of second strand.
To return different tower to make differential thermal coupled with no pressure with benzylalcohol tower and be connected, its thermal load is respectively: return different column overhead condenser 567.82KW, returns different tower tower reactor reboiler 1026.07KW, benzylalcohol column overhead condenser 429.28KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 43.65% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
[comparative example 6]
According to the condition of comparative example 3, be 20,000 tons/year of DCP devices for industrial scale.
[embodiment 6]
According to the condition of embodiment 3, be 20,000 tons/year of DCP devices for industrial scale, Hui Yita and benzylalcohol tower pass in and out the mass fraction of material with comparative example 1, and just operational condition changes, and the operational condition of Hui Yita and benzylalcohol tower is as follows:
| Return different column overhead temperatures (DEG C) | 140 | Benzylalcohol column overhead temperatures (DEG C) | 75 |
| Return different column overhead pressure (kPaA) | 60 | Benzylalcohol column overhead pressure (kPaA) | 10 |
| Return different tower bottom temperature (DEG C) | 185 | Benzylalcohol tower bottom temperature (DEG C) | 135 |
| Return different tower tower reactor pressure (kPaA) | 65 | Benzylalcohol tower tower reactor pressure (kPaA) | 12 |
In addition, isopropyl benzene recovery tower top gaseous phase material is divided into two strands, and first strand is 1.45:1 with the ratio of the mass rate of second strand; Return the material of discharging in different tower top tundish and be divided into two strands after returning different trim the top of column pump, first strand is 7.5:1 with the ratio of the mass rate of second strand.
To return different tower to make differential thermal coupled with no pressure with benzylalcohol tower and be connected, its thermal load is respectively: return different column overhead condenser 510.23KW, returns different tower tower reactor reboiler 1036.38KW, benzylalcohol column overhead condenser 437.96KW, benzylalcohol tower tower reactor reboiler 0.00KW; Thus, different column overhead condenser fractional energy savings 46.30% is returned, benzylalcohol tower tower reactor reboiler fractional energy savings 100.00%.
Claims (6)
1. a dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method, in dicumyl peroxide DCP device, the material of isopropyl benzene to be recycled enters isopropyl benzene recovery tower and reclaims isopropyl benzene, tower bottoms is the heavy constituent by product comprising phenol tar, top gaseous phase material is divided into two strands, after first stock-traders' know-how returns different overhead condenser cooling condensation, enter back different tower top tundish, second strand enters benzylalcohol tower reboiler as benzylalcohol tower reactor reboiler heating medium material, after heat is provided, self is cooling condensation also, converge with first strand of material through condensation and enter back different tower top tundish, return the material of discharging in different tower top tundish and be divided into two strands after returning different trim the top of column pump, first strand returns isopropyl benzene recovery tower as phegma, second strand enters follow-up flow process as product separation.
2. dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method according to claim 1, it is characterized in that the operational condition of described isopropyl benzene recovery tower is: tower top service temperature is 105 ~ 140 DEG C, working pressure is 10 ~ 60kPaA, tower reactor service temperature is 145 ~ 185 DEG C, and working pressure is 15 ~ 65kPaA; The operational condition of benzylalcohol tower is: tower top service temperature is 35 ~ 75 DEG C, and working pressure is 1 ~ 10kPaA, and tower reactor service temperature is 95 ~ 135 DEG C, and working pressure is 3 ~ 12kPaA.
3. dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method according to claim 2, it is characterized in that the operational condition of described isopropyl benzene recovery tower is: tower top service temperature is 110 ~ 135 DEG C, working pressure is 15 ~ 55kPaA, tower reactor service temperature is 150 ~ 180 DEG C, and working pressure is 20 ~ 60kPaA; The operational condition of benzylalcohol tower is: tower top service temperature is 40 ~ 70 DEG C, and working pressure is 2 ~ 8kPaA, and tower reactor service temperature is 105 ~ 125 DEG C, and working pressure is 4 ~ 10kPaA.
4. dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method according to claim 3, it is characterized in that the operational condition of described isopropyl benzene recovery tower is: tower top service temperature is 115 ~ 130 DEG C, working pressure is 20 ~ 50kPaA, tower reactor service temperature is 160 ~ 170 DEG C, and working pressure is 25 ~ 55kPaA; The operational condition of benzylalcohol tower is: tower top service temperature is 45 ~ 65 DEG C, and working pressure is 3 ~ 6kPaA, and tower reactor service temperature is 110 ~ 120 DEG C, and working pressure is 5 ~ 8kPaA.
5. dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method according to claim 1, it is characterized in that described isopropyl benzene recovery tower top gaseous phase material is divided into two strands, first strand is 1.05 ~ 1.45:1 with the ratio of the mass rate of second strand.
6. dicumyl peroxide DCP device onrelevant tower differential pressure heat coupling energy-saving method according to claim 1, it is characterized in that the described material of discharging in different tower top tundish that returns is divided into two strands after returning different trim the top of column pump, first strand is 5.5 ~ 7.5:1 with the ratio of the mass rate of second strand.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316792A (en) * | 2016-08-09 | 2017-01-11 | 天津大学 | Device and method for recovery of methyl alcohol and ethanol from the hydrocracking product of stalk sugar |
| CN109369488A (en) * | 2018-12-07 | 2019-02-22 | 石化盈科信息技术有限责任公司 | A kind of cumyl peroxide DCP device heat integrated utilization method |
| CN109912480A (en) * | 2019-04-01 | 2019-06-21 | 江苏道明化学有限公司 | A kind of DCP rectification working process process |
| CN114681943A (en) * | 2022-03-16 | 2022-07-01 | 中国石油化工股份有限公司 | Method for heating cumene recovery tower |
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| CN102675093A (en) * | 2012-02-25 | 2012-09-19 | 中国石油大学(华东) | Process for synthesizing n-butyl acetate |
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| CN104844493A (en) * | 2015-04-01 | 2015-08-19 | 中石化上海工程有限公司 | Dicumyl peroxide (DCP) and propylene oxied (CHPPO) coproduction method |
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| CN101239247A (en) * | 2007-11-20 | 2008-08-13 | 天津大学 | Differential pressure low-energy-consumption distillation method and equipment |
| CN102675093A (en) * | 2012-02-25 | 2012-09-19 | 中国石油大学(华东) | Process for synthesizing n-butyl acetate |
| CN103950936A (en) * | 2014-03-31 | 2014-07-30 | 中国恩菲工程技术有限公司 | Method for purifying chlorosilane through non-relevant tower differential pressure thermal coupling |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316792A (en) * | 2016-08-09 | 2017-01-11 | 天津大学 | Device and method for recovery of methyl alcohol and ethanol from the hydrocracking product of stalk sugar |
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| CN109369488A (en) * | 2018-12-07 | 2019-02-22 | 石化盈科信息技术有限责任公司 | A kind of cumyl peroxide DCP device heat integrated utilization method |
| CN109369488B (en) * | 2018-12-07 | 2020-11-10 | 石化盈科信息技术有限责任公司 | Heat integrated utilization method of dicumyl peroxide (DCP) device |
| CN109912480A (en) * | 2019-04-01 | 2019-06-21 | 江苏道明化学有限公司 | A kind of DCP rectification working process process |
| CN114681943A (en) * | 2022-03-16 | 2022-07-01 | 中国石油化工股份有限公司 | Method for heating cumene recovery tower |
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| CN105175302B (en) | 2017-06-23 |
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