CN205152116U - Cyclohexanone and cyclohexanol separation economizer in cyclohexanone production process - Google Patents
Cyclohexanone and cyclohexanol separation economizer in cyclohexanone production process Download PDFInfo
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- CN205152116U CN205152116U CN201520793322.6U CN201520793322U CN205152116U CN 205152116 U CN205152116 U CN 205152116U CN 201520793322 U CN201520793322 U CN 201520793322U CN 205152116 U CN205152116 U CN 205152116U
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Abstract
The utility model relates to a cyclohexanone and cyclohexanol separation economizer in cyclohexanone production process, mainly by the cyclohexanol tower, the cyclohexanone tower, cyclohexanol tower return tank, cyclohexanone tower vacuum system, cyclohexanol tower blowdown condenser, cyclohexanone tower return tank, cyclohexanol tower backwash pump, cyclohexanol tata cauldron pump, cyclohexanol tower reboiler, cyclohexanone tower blowdown condenser, the cyclohexanone overhead condenser, cyclohexanone tower backwash pump, cyclohexanone tower cauldron pump, cyclohexanone tower cauldron reboiler, cyclohexanone tower cauldron steam reboiler, cyclohexanol dehydrogenation evaporator assembly becomes, the utility model discloses a cyclohexanone separation and two tower technologies of cyclohexanol separation, can save cyclohexanone tower steam reboiler heating load 8000kw in 200, 000 tons of / year cyclohexanol devices about, about cyclohexanol dehydrogenation evaporimeter heating load 2000kw, cyclohexanol tower condenser duty 10000kw controls.
Description
Technical field
The utility model belongs to chemical technology field, relates to a kind of process of cyclohexanone production cyclohexanone and hexalin separated energy-saving device.
Background technology
Pimelinketone is a kind of important Organic Chemicals.In China, the pimelinketone of 65% is as the raw material producing hexanolactam, and the pimelinketone of 20% is as the raw material producing hexanodioic acid, and remaining pimelinketone is as relevant industrial chemicals.In addition, pimelinketone or excellent solvent, can be used as the solvent painting nitrocotton, vinyl chloride-base polymer and multipolymer.Along with developing rapidly of China's chemical fibre industry, hexanolactam, hexanodioic acid output increase year by year, and the demand of pimelinketone also day by day all increases, and exploitation prospect is wide.
At present, produce pimelinketone technique and mainly contain cyclohexane oxidation process and cyclohexene hydration method.The problems such as cyclohexane oxidation technique is domestic and international prevailing technology, but hexanaphthene method yield is only 75%-80%, there is by-product waste many, and safety requirements is high; The cyclohexene method comprehensive yield is high, hydrogen consumption is low: 99.5% benzene can be converted into product, i.e. pimelinketone and hexanaphthene, and pimelinketone accounts for more than 80%.The cyclohexene method hydrogenation reaction and hydration reaction are carried out all in the liquid phase, and energy consumption is low, except steam consumption and hexanaphthene method close to except, the power consumptions such as consumption de-salted water, electricity, Sweet natural gas are all few compared with hexanaphthene method.Cyclohexene hydration technology is adopted to produce pimelinketone, it is a kind of production line of green economy, recycling raw materials, saving resource and free of contamination technique, comprehensive resource utilization rate is high, belong to environmental type project, the model of cleaner production, meet national industrial policies, have high investment value, building up of it makes a due contribution for the technical progress of enterprise and Sustainable development; Progressively substitute traditional hexanaphthene method operational path by the cyclohexene method modern technique, make conventional industries shine new machine.
When the cyclohexene method preparing cyclohexanone, because cyclohexene hydration reaction generates hexalin low conversion rate, generally be no more than 10%, in such reaction product, tetrahydrobenzene needs carry out hydration reaction after being separated with hexalin again, that isolated hexalin is entered cyclohexanol dehydrogenation reactor through gasification in the prior art, dehydrogenation product to be separated with alcohol tower through ketone tower and to obtain pimelinketone, and the hexalin that alcohol tower is separated enters cyclohexanol dehydrogenation reactor again and carries out dehydrogenation.This technical process steam consumption is high, thus studies hexalin separating technology, develops new separating technology, reduces steam consumption and is significant.
The utility model to be separated with hexalin the pimelinketone in cyclohexanone production apparatus and to carry out heat energy coupling, effectively reduce hexalin and pimelinketone separation system with can load.Energy-conservation and economically all highly significant.
Summary of the invention
The purpose of this utility model is to provide a kind of process of cyclohexanone production cyclohexanone and hexalin tripping device, reduces energy expenditure, with save energy consumption, reduces plant running cost.
The technical solution of the utility model: a kind of process of cyclohexanone production cyclohexanone and hexalin separated energy-saving device, primarily of hexalin tower 1, pimelinketone tower 2, hexalin tower return tank 3, pimelinketone tower vacuum system 4, hexalin tower blowdown condenser 5, pimelinketone tower return tank 6, hexalin tower reflux pump 7, hexalin tower reactor pump 8, hexalin tower reboiler 9, pimelinketone tower blowdown condenser 10, pimelinketone overhead condenser 11, pimelinketone tower reflux pump 12, pimelinketone tower reactor pump 13, pimelinketone tower reactor reboiler 14, pimelinketone tower reactor Steam reboiler 15, cyclohexanol dehydrogenation vaporizer 16 forms, it is characterized in that: the hexalin and the pimelinketone material that gently heat up in a steamer tower enter in the middle part of pimelinketone tower 2, pimelinketone top of tower vapor delivery line is connected with pimelinketone overhead condenser 11, pimelinketone overhead condenser 11 liquid phase pipeline is connected with pimelinketone tower return tank 6, pimelinketone overhead condenser 11 vapor delivery line is connected with pimelinketone tower blowdown condenser 10, pimelinketone tower blowdown condenser 10 vapor delivery line is connected with pimelinketone tower vacuum system 4, pimelinketone tower blowdown condenser 10 vapor delivery line is connected with pimelinketone tower return tank 6, pimelinketone tower return tank 6 is connected with pimelinketone tower reflux pump 12, pimelinketone tower reflux pump 12 exports to be connected with pimelinketone tower top respectively and to be connected with pimelinketone product tank field, pimelinketone tower reactor is connected with pimelinketone tower reboiler 14, pimelinketone tower tower reactor Steam reboiler 15 is connected with pimelinketone tower reactor, pimelinketone tower is connected with hexalin tower fresh feed pump 13, pimelinketone tower reactor pump 13 is connected with in the middle part of hexalin tower 1, hexalin top of tower vapor delivery line is connected with pimelinketone tower reboiler 14, pimelinketone tower reboiler 14 is connected with hexalin tower return tank 3, hexalin tower return tank 3 vapor delivery line is connected with hexalin tower blowdown condenser 5, hexalin tower blowdown condenser 5 liquid phase pipeline is connected with hexalin tower return tank 3, be connected with hexalin tower reflux pump 7 bottom hexalin tower return tank 3, hexalin tower reflux pump 7 is connected with hexalin tower 1 top and cyclohexanol dehydrogenation vaporizer 16 respectively, cyclohexanol dehydrogenation vaporizer 16 connects and is connected with cyclohexanol dehydrogenation reactor, hexalin tower reactor reboiler 9 is connected with hexalin tower bottom, hexalin tower reactor pump 8 is connected with hexalin tower reactor.
Pimelinketone of the present utility model and hexalin separated energy-saving device can also in hexalin tower blowdown condenser 5 T-Ring hexanone tower vacuum systems 17 below.
In the present invention, hexalin tower has working pressure to be 40-300KPa, tower top temperature 125-250 DEG C.
A kind of process of cyclohexanone production cyclohexanone and hexalin separated energy-saving technique, enter in the middle part of pimelinketone tower from the hexalin and pimelinketone material that gently heat up in a steamer tower, pimelinketone adopts underpressure distillation, and working pressure is 5KPa(absolute pressure), tower reactor service temperature is about 100 DEG C, pimelinketone tower reactor reboiler adopts hexalin column overhead vapor condensation hotwork to be its thermal source, and pimelinketone column overhead gas phase is after the condensation of pimelinketone overhead condenser, and phlegma enters pimelinketone tower return tank, noncondensable gas cools at pimelinketone tower blowdown condenser refrigerated water, and pimelinketone tower blowdown condenser is connected with vacuum system, after the material of abundant recovery non-condensable gas entrained with, tail gas enters torch house steward, and the material of recovery enters pimelinketone tower return tank, material in pimelinketone tower return tank returns pimelinketone tower as reflux through pimelinketone tower reflux pump major part, and rest part is sent to tank field as product after the cooling of pimelinketone water cooler, pimelinketone tower bottoms is pumped in the middle part of hexalin tower through pimelinketone tower reactor, and hexalin tower adopts pressure-fired distillation, and working pressure is 110KPa(absolute pressure), tower top service temperature is about 163 DEG C, hexalin tower gas phase enters pimelinketone tower reactor reboiler shell side, be condensed as its thermal source, phlegma enters hexalin tower return tank, hexalin tower noncondensable gas blowdown condenser recirculated water proceeds cooling, after the hexalin of abundant recovery entrained with, tail gas enters torch house steward, the hexalin reclaimed also enters hexalin tower return tank, material in hexalin tower return tank returns hexalin tower as reflux through hexalin tower reflux pump major part, rest part is sent to cyclohexanol dehydrogenation vaporizer, hexalin tower reactor is the still liquid that the concentration of hexalin is less than 30%, through hexalin tower reactor pump, deliver to product tank field.
In above-mentioned energy-saving technique, can also change the operation of hexalin tower into rectification under vacuum, hexalin tower working pressure is 40KPa(absolute pressure), tower top service temperature is about 132 DEG C; Pimelinketone adopts underpressure distillation, and working pressure is 5KPa(absolute pressure), tower reactor service temperature is about 100 DEG C.
The utility model is by pimelinketone tower and hexalin tower efficient combination, by the change of processing parameter, achieve two tower energy effective utilizations, the gas phase hexalin produced by hexalin tower is as the thermal source of hexalin tower, so both decrease the steam consumption of pimelinketone tower, also reduce the cooling-water consumption of hexalin tower simultaneously.
At 200,000 tons/year of hexalin devices, pimelinketone tower Steam reboiler about thermal load 8000kw, cyclohexanol dehydrogenation vaporizer about thermal load 2000kw, hexalin tower condenser duty about 10000kw can be saved.The pimelinketone quality product of producing reaches the requirement of caprolactam production.
Accompanying drawing explanation
Fig. 1, hexalin rectification process pimelinketone and hexalin tripping device;
Fig. 2, former pimelinketone and hexalin tripping device.
In figure:
1-hexalin tower, 2-pimelinketone tower, 3-hexalin tower return tank, 4-pimelinketone tower vacuum system, 5-hexalin tower blowdown condenser, 6-pimelinketone tower return tank, 7-hexalin tower reflux pump, 8-hexalin tower reactor pump, 9-hexalin tower reboiler, 10-pimelinketone tower blowdown condenser), 11-pimelinketone overhead condenser, 12-pimelinketone tower reflux pump, 13-pimelinketone tower reactor pump, 14-pimelinketone tower reactor reboiler, 15-pimelinketone tower reactor Steam reboiler, 16-cyclohexanol dehydrogenation vaporizer, 17-hexalin tower vacuum system, 18-hexalin overhead condenser, WCS-recirculated water, RCS-refrigerated water, HS-high pressure steam, SCH-high pressure steam water of condensation, LS-low-pressure steam, SCL-low-pressure steam water of condensation.
Embodiment
Further illustrate the present invention below in conjunction with accompanying drawing, but do not form limitation of the invention
Embodiment 1
The pimelinketone producing 200000 tons of pimelinketone devices per year is separated with hexalin, as shown in Figure 1 technical process.
Enter in the middle part of pimelinketone tower 2 from the hexalin and pimelinketone material that gently heat up in a steamer tower, pimelinketone adopts underpressure distillation, and working pressure is 5KPa(absolute pressure), tower reactor service temperature is about 100 DEG C; Pimelinketone tower reactor reboiler 14 adopts hexalin tower 1 top gaseous phase heat of condensation as its thermal source, and pimelinketone column overhead gas phase is after pimelinketone overhead condenser 11 condensation, and phlegma enters pimelinketone tower return tank 6; Noncondensable gas cools with refrigerated water at pimelinketone tower blowdown condenser 10, and pimelinketone tower blowdown condenser 10 is connected with pimelinketone tower vacuum system 4; After the material of abundant recovery non-condensable gas entrained with, tail gas enters torch house steward, and the material of recovery enters pimelinketone tower return tank 6; Material in pimelinketone tower return tank 6 returns pimelinketone tower 2 as reflux through pimelinketone tower reflux pump 12 major part, and rest part is sent to tank field as product after the cooling of pimelinketone water cooler; Pimelinketone tower tower bottoms is delivered in the middle part of hexalin tower 1 through pimelinketone tower tower reactor pump 13, and hexalin tower 1 adopts pressure-fired rectifying, and working pressure is 110KPa(absolute pressure), tower top service temperature is about 163 DEG C; Hexalin tower 2 gas phase enters pimelinketone tower reactor reboiler 14 shell side, is condensed as its thermal source, pimelinketone tower reactor Steam reboiler 15 thermal source as a supplement; Phlegma enters hexalin tower return tank 3, hexalin tower noncondensable gas blowdown condenser 5 recirculated water proceeds cooling, after the hexalin of abundant recovery entrained with, tail gas enters torch house steward, the hexalin reclaimed also enters hexalin tower return tank 3, material in hexalin tower return tank returns hexalin tower as reflux through hexalin tower reflux pump major part, and rest part is sent to cyclohexanol dehydrogenation vaporizer 16, after evaporation, enter hexalin dealkylation reaction device; Hexalin tower reactor is the still liquid that the concentration of hexalin is less than 30%, through hexalin tower reactor pump, delivers to X oil production tank field, as X oil production.
In the flow process of this utility model, the thermal load of cyclohexanol dehydrogenation vaporizer is 5371kw, and the thermal load of pimelinketone tower reactor Steam reboiler is 1347.6kw.
In prior art, the thermal load of cyclohexanol dehydrogenation vaporizer is 7613kw, and hexalin overhead condenser duty is 10128kw; The thermal load of pimelinketone tower reboiler is 9412.6kw.
Embodiment 2
As shown in Figure 1, enter in the middle part of pimelinketone tower 2 from the hexalin and pimelinketone material gently heating up in a steamer tower, pimelinketone adopts underpressure distillation, and working pressure is 5KPa(absolute pressure), tower reactor service temperature is about 100 DEG C; Pimelinketone tower reactor reboiler 14 adopts hexalin tower 1 top gaseous phase heat of condensation as its thermal source, and pimelinketone column overhead gas phase is after pimelinketone overhead condenser 11 condensation, and phlegma enters pimelinketone tower return tank 6; Noncondensable gas cools with refrigerated water at pimelinketone tower blowdown condenser 10, and pimelinketone tower blowdown condenser 10 is connected with pimelinketone tower vacuum system 4; After the material of abundant recovery non-condensable gas entrained with, tail gas enters torch house steward, and the material of recovery enters pimelinketone tower return tank 6; Material in pimelinketone tower return tank 6 returns pimelinketone tower 2 as reflux through pimelinketone tower reflux pump 12 major part, and rest part is sent to tank field as product after the cooling of pimelinketone water cooler; Pimelinketone tower bottoms is delivered in the middle part of hexalin tower 1 through pimelinketone tower reactor pump 13, and hexalin tower 1 adopts pressure-fired rectifying, and working pressure is 40KPa(absolute pressure), tower top service temperature is about 132 DEG C; Hexalin tower 2 gas phase enters pimelinketone tower tower reactor reboiler 14 shell side, is condensed as its thermal source, pimelinketone tower reactor Steam reboiler 15 thermal source as a supplement; Phlegma enters hexalin tower return tank 3, hexalin tower noncondensable gas blowdown condenser 5 recirculated water proceeds cooling, after the hexalin of abundant recovery entrained with, tail gas enters pimelinketone tower vacuum system 17, the hexalin reclaimed also enters hexalin tower return tank 3, material in hexalin tower return tank returns hexalin tower as reflux through hexalin tower reflux pump major part, and rest part is sent to cyclohexanol dehydrogenation vaporizer 16, after evaporation, enter hexalin dealkylation reaction device; Hexalin tower tower reactor is the still liquid that the concentration of hexalin is less than 30%, through hexalin tower reactor pump, delivers to X oil production tank field, as X oil production.
In the flow process of this utility model, the thermal load of hexalin vaporizer is 6238kw, and the thermal load of pimelinketone tower reactor Steam reboiler is 620.6kw.
In prior art, the thermal load of hexalin vaporizer is 7613kw, and hexalin overhead condenser duty is 10128kw; The thermal load of pimelinketone tower reboiler is 9412.6kw.
Claims (2)
1. a process of cyclohexanone production cyclohexanone and hexalin separated energy-saving device, primarily of hexalin tower (1), pimelinketone tower (2), hexalin tower return tank (3), pimelinketone tower vacuum system (4), hexalin tower blowdown condenser (5), pimelinketone tower return tank (6), hexalin tower reflux pump (7), hexalin tower tower reactor pump (8), hexalin tower reboiler (9), pimelinketone tower blowdown condenser (10), pimelinketone overhead condenser (11), pimelinketone tower reflux pump (12), pimelinketone tower reactor pump (13), pimelinketone tower reactor reboiler (14), pimelinketone tower reactor Steam reboiler (15), cyclohexanol dehydrogenation vaporizer (16) forms, it is characterized in that: the hexalin and the pimelinketone material that gently heat up in a steamer tower enter pimelinketone tower (2) middle part, pimelinketone top of tower vapor delivery line is connected with pimelinketone overhead condenser (11), pimelinketone overhead condenser (11) liquid phase pipeline is connected with pimelinketone tower return tank (6), pimelinketone overhead condenser (11) vapor delivery line is connected with pimelinketone tower blowdown condenser (10), pimelinketone tower blowdown condenser (10) vapor delivery line is connected with pimelinketone tower vacuum system (4), pimelinketone tower blowdown condenser (10) vapor delivery line is connected with pimelinketone tower return tank (6), pimelinketone tower return tank (6) is connected with pimelinketone tower reflux pump (12), pimelinketone tower reflux pump (12) outlet is connected with pimelinketone tower top respectively and is connected with pimelinketone product tank field, pimelinketone tower reactor is connected with pimelinketone tower reboiler (14), pimelinketone tower reactor Steam reboiler (15) is connected with pimelinketone tower reactor, pimelinketone tower is connected with hexalin tower fresh feed pump (13), pimelinketone tower reactor pump (13) is connected with hexalin tower (1) middle part, hexalin top of tower vapor delivery line is connected with pimelinketone tower reboiler (14), pimelinketone tower reboiler (14) is connected with hexalin tower return tank (3), hexalin tower return tank (3) vapor delivery line is connected with hexalin tower blowdown condenser (5), hexalin tower blowdown condenser (5) liquid phase pipeline is connected with hexalin tower return tank (3), hexalin tower return tank (3) bottom is connected with hexalin tower reflux pump (7), hexalin tower reflux pump (7) is connected with hexalin tower (1) top and cyclohexanol dehydrogenation vaporizer (16) respectively, cyclohexanol dehydrogenation vaporizer (16) connects and is connected with cyclohexanol dehydrogenation reactor, hexalin tower reactor reboiler (9) is connected with hexalin tower bottom, hexalin tower reactor pump (8) is connected with hexalin tower reactor.
2. process of cyclohexanone production cyclohexanone according to claim 1 and hexalin separated energy-saving device, is characterized in that at hexalin tower blowdown condenser (5) T-Ring hexanone tower vacuum system (17) below.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106083544A (en) * | 2016-06-02 | 2016-11-09 | 中国化学赛鼎宁波工程有限公司 | Cyclohexanone is refined and cyclohexanol recoverying and utilizing method and system |
| CN108484379A (en) * | 2018-05-02 | 2018-09-04 | 山东亚科环保科技有限公司 | A kind of Processes and apparatus detaching cyclohexanone, cyclohexanol, DMAC N,N' dimethyl acetamide mixture |
| CN108558629A (en) * | 2018-06-01 | 2018-09-21 | 李洪震 | A kind of production system and production method of refined cyclohexanone |
| CN114763318A (en) * | 2021-01-13 | 2022-07-19 | 中国石油化工股份有限公司 | Method and device for preparing cyclohexanone from crude cyclohexanol obtained by esterification hydrogenation method |
| CN115212600A (en) * | 2022-08-22 | 2022-10-21 | 福建永荣科技有限公司 | Energy-conserving high-efficient type cyclohexanone refined system |
-
2015
- 2015-10-15 CN CN201520793322.6U patent/CN205152116U/en active Active
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106083544A (en) * | 2016-06-02 | 2016-11-09 | 中国化学赛鼎宁波工程有限公司 | Cyclohexanone is refined and cyclohexanol recoverying and utilizing method and system |
| CN106083544B (en) * | 2016-06-02 | 2018-05-18 | 中国化学赛鼎宁波工程有限公司 | Cyclohexanone refines and cyclohexanol recoverying and utilizing method and system |
| CN108484379A (en) * | 2018-05-02 | 2018-09-04 | 山东亚科环保科技有限公司 | A kind of Processes and apparatus detaching cyclohexanone, cyclohexanol, DMAC N,N' dimethyl acetamide mixture |
| CN108558629A (en) * | 2018-06-01 | 2018-09-21 | 李洪震 | A kind of production system and production method of refined cyclohexanone |
| CN114763318A (en) * | 2021-01-13 | 2022-07-19 | 中国石油化工股份有限公司 | Method and device for preparing cyclohexanone from crude cyclohexanol obtained by esterification hydrogenation method |
| CN114763318B (en) * | 2021-01-13 | 2023-12-29 | 中国石油化工股份有限公司 | Method and device for preparing cyclohexanone from crude cyclohexanol obtained by esterification hydrogenation method |
| CN115212600A (en) * | 2022-08-22 | 2022-10-21 | 福建永荣科技有限公司 | Energy-conserving high-efficient type cyclohexanone refined system |
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