CN107032959A - A kind of heat pump and the methanol rectification method of multiple-effect coupling - Google Patents
A kind of heat pump and the methanol rectification method of multiple-effect coupling Download PDFInfo
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- CN107032959A CN107032959A CN201710342561.3A CN201710342561A CN107032959A CN 107032959 A CN107032959 A CN 107032959A CN 201710342561 A CN201710342561 A CN 201710342561A CN 107032959 A CN107032959 A CN 107032959A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- 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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Abstract
The invention discloses a kind of methanol rectification method that heat pump and multiple-effect are coupled, raw material crude carbinol is entered in the middle part of lightness-removing column by preheating, and removes light component therein；Lightness-removing column tower reactor component enters the tower of normal pressure I, and the tower reactor component of normal pressure I enters the tower of normal pressure II, and the tower reactor component of normal pressure II enters pressurizing tower, and pressurization tower reactor component enters recovery tower；The tower of normal pressure I, the tower of normal pressure II, pressurizing tower and recovery column overhead obtain the methanol product of high-purity；The tower of normal pressure I uses heat pump distillation technology, and overhead vapours gives the heat supply of this tower reactor reboiler by compressing；Thermal coupling is carried out between the tower of normal pressure II and pressurizing tower, pressurization top gaseous phase provides institute's calorific requirement as the heat source of the tower reactor reboiler of normal pressure II for the rectifying of the tower of normal pressure II；Thermal coupling is carried out between lightness-removing column and recovery tower, top gaseous phase is reclaimed as the heat source of lightness-removing column kettle reboiler, institute's calorific requirement is provided for the rectifying of lightness-removing column.The present invention is integrated by heat pump techniques and differential pressure thermal coupled process, with the saving energy, the characteristics of reducing energy consumption.
Description
Technical field
The present invention relates to the technological process of methanol rectification, particularly a kind of methanol rectifying system of optimization belongs to chemical industry biography
Matter and the field separated.
Background technology
Methanol is a kind of important basic organic chemical raw material and novel energy fuel, and the task of methanol rectification is that removing is thick
The impurity such as the light components such as the dimethyl ether in methanol and water, ethanol, production meets the refined methanol of product requirement.With coal chemical industry
Development, the scale of methanol device is also increasing, and how energy-saving refining methanol device is turns into Business survival and raising
The key of competitiveness, also as researcher increasingly concern.
At present widely used three tower methanol rectifications (following current double-effect rectification) technique, i.e. crude carbinol order by pre-tower plus
Tower, atmospheric tower is pressed to carry out rectifying separation.Light component in crude carbinol is removed by pre-tower, prognosis crude carbinol passes through pressurizing tower and normal pressure
After tower rectifying, methanol product is obtained respectively in the discharging of pressurization column overhead and the discharging of normal pressure column overhead, the column overhead methanol that pressurizes is utilized
The condensation latent heat of steam is discharged as atmospheric tower boiling hot source again, fusel from atmospheric tower side take-off, waste water from atmospheric tower bottom of towe.This
Although kind of method technology maturation, energy consumption is higher, methanol rectification process energy consumption is about 3414.225MJ/ tons of methanol productions
Product, and as unit scale increasingly increases, total energy consumption is also dramatically increased.
In addition, also having much on the Patents that methanol rectification is saved, than more typical, there is CN101503337A《Adopt
The process of methanol rectification is carried out with fiver-tower heat integration apparatus》And CN101786940A《A kind of methanol heat-pump rectifying process》,
But two methods cut both ways.Five tower integrated approach energy-saving effects are substantially, therein to be thermally integrated atmospheric tower, lower pressure column and high pressure
The tower of tower three is integrated and lightness-removing column and recovery tower between be thermally integrated, methanol rectification process energy consumption is about 2288.41MJ/ tons of methanol
Product, although this flow is than above-mentioned three towers methanol rectification (following current double-effect rectification) energy saving technology 32.97%, it is also potential can
Dig, and the condensation of lightness-removing column and normal pressure column overhead methanol steam needs to consume more cooling water.The patent of methanol heat-pump rectifying,
Propose and saved using heat pump techniques, but because flow is only designed as pre-tower, normal pressure A towers and normal pressure B towers.On the one hand compress
The power consumption of machine is larger, and another aspect normal pressure B towers tower reactor reboiler still needs more steam to provide heat, through adjusting, its
Energy consumption is about 2347.07MJ/ tons of methanol products.
Although researcher proposes different energy-saving schemes to methanol rectifying system, still there is difference in each scheme
The problem of；In view of problem present in current flow, the present invention is integrated by heat pump techniques and differential pressure thermal coupled process, it is proposed that one
Plant the methanol rectifying system of optimization.
The content of the invention
It is an object of the invention to provide a kind of methanol rectification method that heat pump and multiple-effect are coupled, by heat pump techniques and differential pressure heat
Coupling technique is integrated, with the saving energy, the characteristics of reducing energy consumption.
The technical scheme is that：A kind of heat pump and the methanol rectification method of multiple-effect coupling, it is characterised in that：Raw material is thick
Methanol is entered in the middle part of lightness-removing column by preheating, and removes light component therein；Lightness-removing column tower reactor component enters the tower of normal pressure I, the tower of normal pressure I
Kettle component enters the tower of normal pressure II, and the tower reactor component of normal pressure II enters pressurizing tower, and pressurization tower reactor component enters recovery tower；The tower of normal pressure I, often
Press II tower, pressurizing tower and reclaim the methanol product that column overhead obtains high-purity；The tower of normal pressure I uses heat pump distillation technology, tower top
Steam gives the heat supply of this tower reactor reboiler by compressing；Thermal coupling is carried out between the tower of normal pressure II and pressurizing tower, pressurization top gaseous phase is made
For the heat source of the tower reactor reboiler of normal pressure II, institute's calorific requirement is provided for the rectifying of the tower of normal pressure II；Between lightness-removing column and recovery tower
Thermal coupling is carried out, top gaseous phase is reclaimed as the heat source of lightness-removing column kettle reboiler, the heat for needed for being provided the rectifying of lightness-removing column
Amount.
Methanol rectifying system of the present invention, is carried out between thermal coupling, the tower of normal pressure II and pressurizing tower between lightness-removing column and recovery tower
Thermal coupling is carried out, the tower of normal pressure I uses heat pump distillation technology.The integrated application of heat pump and differential pressure thermal coupled process is realized, greatly
Ground reduces energy consumption.The energy consumption of this methanol rectifying system is about 1828.94MJ/ tons of methanol, than three tower methanol rectification (following current economic benefits and social benefits
Rectifying) energy saving technology 46.4%, than simple heat pump techniques energy-conservation 22%, methanol device energy-conservation 20% is thermally integrated than five towers.
In summary, methanol rectifying system proposed by the present invention, with the saving energy, the characteristics of reducing energy consumption, therefore tool
There are larger implementary value and economic benefit.
Brief description of the drawings
Fig. 1 is the process chart of the methanol rectifying system of optimization.
Drawing reference numeral：1- preheaters；2- lightness-removing columns；3- lightness-removing column dephlegmator of top of the tower；4- lightness-removing column tower reactor reboilers；5- is normal
Press I tower；6- compressors；7- condensers；The tower tower reactor reboiler of 8- normal pressures I；The tower of 9- normal pressures II；The column overhead condenser of 10- normal pressures II；
The tower tower reactor reboiler of 11- normal pressures II；12 pressurizing towers；13- pressurizing tower tower reactor reboilers；14- recovery towers；15- recovery towers tower reactor is again
Boil device.
Embodiment
Technical scheme is further detailed below in conjunction with the accompanying drawings：
As shown in figure 1, a kind of methanol rectifying system of optimization, the tower top of lightness-removing column 2 is segregated by pipeline and lightness-removing column tower top
Device 3 is connected, and bottom of towe is connected by pipeline with lightness-removing column tower reactor reboiler 4 and the middle part of I tower of normal pressure 5；The described tower top of I tower of normal pressure 5
It is connected by pipeline with compressor 6, bottom of towe is connected by pipeline with tower reactor reboiler 8 and the middle part of II tower of normal pressure 9, and compressor 6 leads to
Pipeline is crossed with the tower tower reactor reboiler 8 of normal pressure I to be connected；The described tower top of II tower of normal pressure 9 is connected by pipeline with overhead condenser 10,
Bottom of towe is connected by pipeline with tower reactor reboiler 11 and the middle part of pressurizing tower 12；The described tower top of pressurizing tower 12 passes through pipeline and normal pressure
II tower tower reactor reboiler 11 is connected, and bottom of towe is connected by pipeline with tower reactor reboiler 13 and the middle part of recovery tower 14；Described recovery
The tower top of tower 14 is connected by pipeline with lightness-removing column tower reactor reboiler 4, and bottom of towe passes through pipeline and tower reactor reboiler 15 and raw material preheating
Device 1 is connected.
Clear in order to describe, the equipment and condition that the present embodiment is used describe in detail as follows：
Crude carbinol enters the middle part of lightness-removing column 2 after being preheated by preheater 1；Described lightness-removing column 2 pressure be 101~
Operated under 150kPa, tower top temperature is：64 DEG C~75 DEG C, column bottom temperature is 70 DEG C~85 DEG C；The top gaseous phase of lightness-removing column 2 passes through tower
Push up after the condensation of segregator 3, light component extraction；Lightness-removing column bottom of towe Partial Liquid Phase enters reboiler 4 after overheat, returns in tower；It is de-
Light tower tower reactor component enters the middle part of I tower of normal pressure 5.
The described tower 5 of normal pressure I is operated in the case where pressure is 101~150kPa, and tower top temperature is：64 DEG C~75 DEG C, bottom of towe temperature
Spend for 75 DEG C~90 DEG C；The top gaseous phase of I tower of normal pressure 5 to tower reactor reboiler 8 after the compression heating of compressor 6 by providing heat；For
The stream thigh that reboiler 8 is provided after heat is allocated as producing for product, and the condensed device 7 in part is used as backflow after cooling down；The tower tower of normal pressure I
Bottom Partial Liquid Phase, which enters after reboiler 8 is heated, to be returned in tower；The tower tower reactor component of normal pressure I enters the middle part of II tower of normal pressure 9.
The described tower 9 of normal pressure II is operated in the case where pressure is 101~150kPa, and tower top temperature is：64 DEG C~75 DEG C, bottom of towe temperature
Spend for 75 DEG C~95 DEG C；The top gaseous phase of II tower of normal pressure 9 condenses rear portion by overhead condenser 10 and is allocated as producing for product, and part is returned
Flow into tower；The tower bottom of towe Partial Liquid Phase of normal pressure II is returned in tower into reboiler 11 after overheat；The tower tower reactor component of normal pressure II enters
The middle part of pressurizing tower 12.
Described pressurizing tower 12 is operated in the case where pressure is 300~450kPa, and tower top temperature is：94 DEG C~105 DEG C, bottom of towe temperature
Spend for 105 DEG C~125 DEG C；The top gaseous phase of pressurizing tower 12, as the heat source of the tower tower reactor reboiler 13 of normal pressure II, is reboiler
Stream thigh after 13 offer heats is allocated as producing for product, is partly used as and passes back into tower；Pressurization tower bottom point liquid phase enters boils again
Device 13 is returned in tower after heating；Tower reactor of pressurizeing component enters the middle part of recovery tower 14.
Described recovery tower 14 is operated in the case where pressure is 250~400kPa, and tower top temperature is：85 DEG C~105 DEG C, bottom of towe temperature
Spend for 130 DEG C~150 DEG C；The top gaseous phase of recovery tower 14, as the heat source of lightness-removing column tower reactor reboiler 4, is that reboiler 4 is carried
Stream thigh after heating load is allocated as producing for product, is partly used as and passes back into tower；Reclaim tower bottom point liquid phase and enter reboiler 15
Returned after heating in tower；Reclaim after tower reactor component is cooled down in preheater 1 and send out, fusel is produced from the middle part of recovery tower 14.
A kind of methanol rectifying system of optimization disclosed by the invention, differential pressure thermal coupled process and heat pump techniques are collected
Into the energy consumption of this methanol rectifying system is about 1828.94MJ/ tons of methanol, than three tower methanol rectifications (following current double-effect rectification) technique
Energy-conservation 46.4%, than simple heat pump techniques energy-conservation 22%, methanol device energy-conservation 20% is thermally integrated than five towers, with significant warp
Ji benefit, has a extensive future.
The present invention discloses a kind of methanol rectifying system of optimization.Those skilled in the art can by using for reference present invention,
Appropriate to change technological parameter, the link such as structure design is realized, the order, the operating parameter of each tower such as each tower.The present invention is logical
Cross preferred embodiment to be described, person skilled can substantially not depart from core concept of the present invention, scope and content
It is interior that relevant flow is carried out suitably to change or combine, to realize the technology of the present invention, in addition, all similar replacements and change pair
It is it will be apparent that they are considered as being included in core spirit of the present invention, scope and content for those skilled in the art.
Claims (6)
1. a kind of heat pump and the methanol rectification method of multiple-effect coupling, it is characterised in that：Raw material crude carbinol enters de- light by preheating
In the middle part of tower (2), light component therein is removed；Lightness-removing column tower reactor component enters the tower of normal pressure I (5), and the tower of normal pressure I (5) tower reactor component is entered
Enter the tower of normal pressure II (9), the tower of normal pressure II (9) tower reactor component enters pressurizing tower (12), and pressurizing tower (12) tower reactor component enters recovery tower
(14)；The tower of normal pressure I (5), the tower of normal pressure II (9), pressurizing tower (12) and recovery tower (14) tower top obtain the methanol product of high-purity；
The tower of normal pressure I (5) uses heat pump distillation technology, and overhead vapours gives the tower of normal pressure I (5) tower reactor reboiler (8) heat supply by compressing；Normal pressure
Thermal coupling is carried out between II tower (9) and pressurizing tower (12), pressurizing tower (12) top gaseous phase is used as the tower of normal pressure II (9) tower reactor reboiler
(11) heat source, institute's calorific requirement is provided for the rectifying of the tower of normal pressure II (9)；Carried out between lightness-removing column (2) and recovery tower (14)
Thermal coupling, recovery tower (14) top gaseous phase, as the heat source of lightness-removing column (2) tower reactor reboiler (4), is the essence of lightness-removing column (2)
Offer institute calorific requirement is provided.
2. heat pump as claimed in claim 1 and the methanol rectification method of multiple-effect coupling, it is characterised in that：The lightness-removing column (2)
Operated in the case where pressure is 101~150kPa, tower top temperature is：64 DEG C~75 DEG C, column bottom temperature is 70 DEG C~85 DEG C.
3. heat pump as claimed in claim 1 and the methanol rectification method of multiple-effect coupling, it is characterised in that：The tower of normal pressure I (5)
Operated in the case where pressure is 101~150kPa, tower top temperature is：64 DEG C~75 DEG C, column bottom temperature is 75 DEG C~90 DEG C.
4. heat pump as claimed in claim 1 and the methanol rectification method of multiple-effect coupling, it is characterised in that：The tower of normal pressure II
(9) operated in the case where pressure is 101~150kPa, tower top temperature is：64 DEG C~75 DEG C, column bottom temperature is 75 DEG C~95 DEG C.
5. heat pump as claimed in claim 1 and the methanol rectification method of multiple-effect coupling, it is characterised in that：The pressurizing tower (12)
Operated in the case where pressure is 300~450kPa, tower top temperature is：94 DEG C~105 DEG C, column bottom temperature is 105 DEG C~125 DEG C.
6. heat pump as claimed in claim 1 and the methanol rectification method of multiple-effect coupling, it is characterised in that：The recovery tower (14)
Operated in the case where pressure is 250~400kPa, tower top temperature is：85 DEG C~105 DEG C, column bottom temperature is 130 DEG C~150 DEG C.
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| CN201710342561.3A CN107032959A (en) | 2017-05-16 | 2017-05-16 | A kind of heat pump and the methanol rectification method of multiple-effect coupling |
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| CN201710342561.3A CN107032959A (en) | 2017-05-16 | 2017-05-16 | A kind of heat pump and the methanol rectification method of multiple-effect coupling |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109761751A (en) * | 2017-11-09 | 2019-05-17 | 赵婷婷 | A kind of methanol thermal coupling multi-effect distillation method and device |
| CN110143850A (en) * | 2019-05-28 | 2019-08-20 | 天津大学 | The not energy-saving methanol multi-effect distillation method of the single column steam drive of by-product fusel oil |
| CN110280034A (en) * | 2019-07-02 | 2019-09-27 | 中国天辰工程有限公司 | A kind of methanol fractionation system and technique |
| CN111548243A (en) * | 2020-05-06 | 2020-08-18 | 天津市汇筑恒升科技有限公司 | Heat integration energy-saving process in device for synthesizing cyclohexanone by cyclohexene method |
| CN111574374A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl methacrylate crude product |
| CN111995499A (en) * | 2020-08-26 | 2020-11-27 | 吴嘉 | Methanol heat pump rectification method and device |
| CN114621056A (en) * | 2022-04-19 | 2022-06-14 | 烟台国邦化工机械科技有限公司 | Process for separating dimethyl carbonate and methanol azeotrope |
| CN114681942A (en) * | 2020-12-28 | 2022-07-01 | 天津市华瑞奕博化工科技有限公司 | Tert-butyl alcohol recovery complete variable-voltage coupling rectification device and rectification method |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109761751A (en) * | 2017-11-09 | 2019-05-17 | 赵婷婷 | A kind of methanol thermal coupling multi-effect distillation method and device |
| CN110143850A (en) * | 2019-05-28 | 2019-08-20 | 天津大学 | The not energy-saving methanol multi-effect distillation method of the single column steam drive of by-product fusel oil |
| CN110280034A (en) * | 2019-07-02 | 2019-09-27 | 中国天辰工程有限公司 | A kind of methanol fractionation system and technique |
| CN111548243A (en) * | 2020-05-06 | 2020-08-18 | 天津市汇筑恒升科技有限公司 | Heat integration energy-saving process in device for synthesizing cyclohexanone by cyclohexene method |
| CN111574374A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl methacrylate crude product |
| CN111574374B (en) * | 2020-06-22 | 2022-08-23 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl methacrylate crude product |
| CN111995499A (en) * | 2020-08-26 | 2020-11-27 | 吴嘉 | Methanol heat pump rectification method and device |
| CN114681942A (en) * | 2020-12-28 | 2022-07-01 | 天津市华瑞奕博化工科技有限公司 | Tert-butyl alcohol recovery complete variable-voltage coupling rectification device and rectification method |
| CN114681942B (en) * | 2020-12-28 | 2023-07-07 | 天津市华瑞奕博化工科技有限公司 | Complete pressure swing coupling rectification device and rectification method for tertiary butanol recovery |
| CN114621056A (en) * | 2022-04-19 | 2022-06-14 | 烟台国邦化工机械科技有限公司 | Process for separating dimethyl carbonate and methanol azeotrope |
| CN114621056B (en) * | 2022-04-19 | 2023-10-27 | 烟台国邦化工机械科技有限公司 | Process method for separating dimethyl carbonate and methanol azeotrope |
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