CN101503337B - Technological process for methanol distillation by using fiver-tower heat integration apparatus - Google Patents
Technological process for methanol distillation by using fiver-tower heat integration apparatus Download PDFInfo
- Publication number
- CN101503337B CN101503337B CN2009100681702A CN200910068170A CN101503337B CN 101503337 B CN101503337 B CN 101503337B CN 2009100681702 A CN2009100681702 A CN 2009100681702A CN 200910068170 A CN200910068170 A CN 200910068170A CN 101503337 B CN101503337 B CN 101503337B
- Authority
- CN
- China
- Prior art keywords
- tower
- pressure
- column
- cat head
- lightness
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a technique for rectifying methanol by adopting a five-tower heat-integrated device, in particular to a method which is used for producing methanol from crude methanol through the rectifying process and saves energy. The whole methanol rectifying system at least comprises five towers which are a lightness-removing tower, a normal pressure rectifying tower, a low pressure rectifying tower, a high pressure rectifying tower and a reclaiming tower as well as other corollary equipment; wherein, heat integration is adopted among the normal pressure rectifying tower, the low pressure rectifying tower and the high pressure rectifying tower, and heat integration operation is carried out between the lightness-removing tower and the reclaiming tower; furthermore, other heat exchanging and power-saving technologies are applied in the system, the operation energy consumption is greatly reduced, the operation and control indexes of all the towers are simplified, and the operation stability of the whole rectifying system can be improved. The invention overcomes the defects of the prior art, reduces the operation energy consumption by over 30%, and has remarkable practicability and economic benefit.
Description
Technical field
The present invention relates to the rectification process of methyl alcohol, particularly a kind of process method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, it is from thick methyl alcohol, to pass through the energy-saving process method that rectifying is produced methyl alcohol.
Background technology
Methyl alcohol is a kind of important Organic Chemicals and novel energy fuel, has purposes widely in chemical industry, light industry and clean energy field.In the synthesizing methanol commercial process, the energy consumption of the treating process of thick methyl alcohol is one of key factor that influences the methanol production cost.Serious day by day along with problems such as in short supply, the environmental pollution of oil, coal, Sweet natural gas equal energy source resource and Greenhouse effect, energy-conservation, the key that consumption reduction has become Business survival and enhanced competitiveness of industries such as methyl alcohol more and more receive the attention of each side.
Fig. 1 is a kind of four towers (three towers add a tower) methanol rectification process method that extensively adopts at present, promptly adopts three towers such as preparatory tower T101, pressurizing tower T102, atmospheric tower T103 to increase a regenerating column T104 again, production GB premium grads or U.S. mark AA level methanol product.Remove light constituent by preparatory column overhead, the thick methyl alcohol 10 of prognosis obtains methanol product respectively in pressurizing tower cat head discharging 24 and atmospheric tower cat head discharging 14 after pressurizing tower and atmospheric tower rectifying, and the atmospheric tower side line is extracted fusel 42 out.Pressurizing tower cat head material gas phase 21 is given the heating of normal pressure Tata still.Atmospheric tower side line fusel 42 advances regenerating column with normal pressure tower bottoms 15, obtains reclaiming methanol product 29 by the regenerating column cat head, and the regenerating column side line is extracted potato spirit 30 out, reclaims Tata still waste discharge 33.Though this method technology maturation, production energy consumption is higher, and along with unit scale increases day by day, it is comparatively huge that its equipment scale seems.Construction, economic stability operation to the methyl alcohol product installation that maximizes day by day are unfavorable.
The process method that Chinese patent CN 200610014321.2 discloses a kind of " rectification process of high purity methanol and preparation "; Chinese patent CN 200610013269.9 discloses a kind of " double effect rectification for methanol energy-saving and water-saving system and technology "; Both core contents all are on the basis of the four tower rectifyinges that extensively adopt at present; Utilize the heat exchange of the lime set heat or the internal system cold and hot liquids of heating steam, reach purpose of energy saving.Sensible heat transfer between the obvious this material, the operation energy consumption for reducing whole rectifying system acts on very limited.
Chinese patent CN 200710067196.6 discloses " a kind of have the integrated method of refining synthetic methanol of heat "; It is characterized in that: on the basis of the four tower rectifyinges that extensively adopt at present; The pressurizing tower overhead vapours is divided into two strands, heat is provided for respectively preparatory tower and atmospheric tower.Relative Chinese patent CN 200610014321.2 and CN 200610013269.9, this process method has higher energy-saving effect.But because preparatory column overhead output methanol product not in the system, pressurizing tower is that the energy that preparatory tower provides belongs to single-action methanol rectification process.Pressurizing tower, atmospheric tower cat head output methanol product all in the system, only pressurizing tower is that the energy that atmospheric tower provides belongs to economic benefits and social benefits methanol rectification process, therefore, though this process method has certain improvement energy-saving effect, energy-saving effect is unsatisfactory.
Chinese patent CN 200710146369.3 discloses " a kind of pressure-reducing flow-reversing dual-purpose distillation method of refining crude methanol and equipment "; It is optimized the pressurizing tower in the four tower rectifyinges that extensively adopt at present and the operational condition and the rectifying order of atmospheric tower; The preparatory tower of process removes the thick methyl alcohol behind the light constituent; Be introduced into the rectification under vacuum tower, the rectification under vacuum tower bottoms gets into little compression rectification tower again, by the cat head acquisition methanol product of two towers.Little compression rectification column overhead gas phase is given the heating of rectification under vacuum Tata still reboiler.Though the rectification under vacuum tower is favourable for raising separation system relative volatility, the higher methanol product purity of acquisition.But because the methyl alcohol boiling point is lower, decompression operation can cause tower top temperature very low, and the overhead condenser heat transfer temperature difference significantly reduces, and not only the condensing surface area is huge, simultaneously because vacuum system possibly cause the loss of methyl alcohol to strengthen.As everyone knows, this decompression operation process will inevitably cause enlarging markedly of corresponding tower scale.For the methanol device that maximizes day by day at present, this technology can cause the very huge of tower and heat-exchange equipment scale.The essence of this technology still belongs to the double-effect rectification process of traditional three-tower rectification, therefore fails obtaining substantive breakthroughs aspect further cutting down the consumption of energy.Its operation energy consumption disregards preparatory tower and regenerating column just reaches 0.916 ton of steam/ton methanol product, if count preparatory tower and regenerating column energy consumption, operation energy consumption will be greater than 1 ton of steam/ton methanol product.
Summary of the invention
The present invention relates to a kind of process method that adopts fiver-tower heat integration apparatus to carry out methanol rectification; It is from thick methyl alcohol, to pass through the energy-saving process method that rectifying is produced methyl alcohol; Can overcome the defective of prior art; Reduce operation energy consumption more than 30%, have significant practicality and economic benefit, have a extensive future.
The step that the process method that employing fiver-tower heat integration apparatus provided by the invention carries out methanol rectification comprises:
(1) comprises five towers such as lightness-removing column T201, atmospheric distillation tower T202, low-pressure distillation tower T203, high-pressure rectification tower T204 and regenerating column T205 at least;
(2) heat is integrated between atmospheric distillation tower T202, low-pressure distillation tower T203, high-pressure rectification tower T204 three towers, and low-pressure distillation tower cat head gas phase is as atmospheric distillation Tata still heating thermal source, for the atmospheric distillation tower provides institute's heat requirement; High-pressure rectification column overhead gas phase is as low-pressure distillation Tata still heating thermal source, for low-pressure distillation tower provides institute's heat requirement;
(3) heat is integrated between lightness-removing column T201 and regenerating column T205 two towers, and regenerating column cat head gas phase is as lightness-removing column tower still heating thermal source, for lightness-removing column provides institute's heat requirement.
Process method provided by the present invention except that adopting the integrated production methyl alcohol of above-mentioned five towers heat, can also adopt the integrated production methyl alcohol of six towers heat.On the integrated basis of above-mentioned five towers heat, increase a compression rectification tower T207 again; Between said atmospheric distillation tower T202, low-pressure distillation tower T203, high-pressure rectification tower T204 three towers heat integrated; Compression rectification tower T207 cat head gas phase is as high-pressure rectification tower T204 tower still heating thermal source, for high-pressure rectification tower T204 provides institute's heat requirement.Compression rectification tower T207 and atmospheric distillation tower T202, low-pressure distillation tower T203, that high-pressure rectification tower T204 forms four tower heat is integrated, further reduces operation energy consumption.
In the process method provided by the present invention said thick methanol feedstock can with reclaim the heat exchange of Tata still waste discharge, thick methanol feedstock also can with the methanol product heat exchange, to improve the temperature that thick methyl alcohol gets into lightness-removing column, reduce operation energy consumption.
Process method provided by the present invention; The energy-saving manner (heat exchange mode) that can also select to adopt has: lightness-removing column (T201), atmospheric distillation tower (T202), low-pressure distillation tower (T203), high-pressure rectification tower (T204), compression rectification tower (T207) or regenerating column (T205) wait the charging and the heat exchange of heating steam lime set of each tower; To improve the feeding temperature of corresponding knockout tower, reduce operation energy consumption.
The exemplary embodiment of the heat exchange between this steam condensate and each the tower charging has:
Mode one:
Steam condensate elder generation and high-pressure rectification tower (T204) charging heat exchange, preheating high-pressure rectification tower (T204) charging;
Give after high-pressure rectification tower (T204) the charging heat exchange steam condensate again with low-pressure distillation tower (T203) charging heat exchange, preheating low-pressure distillation tower (T203) charging;
Give after low-pressure distillation tower (T203) the charging heat exchange steam condensate again with atmospheric distillation tower (T202) charging heat exchange, preheating atmospheric distillation tower (T202) charging;
Give after atmospheric distillation tower (T202) the charging heat exchange steam condensate again with lightness-removing column (T201) charging heat exchange, preheating lightness-removing column (T201) charging.
Mode two:
Steam condensate elder generation and high-pressure rectification tower (T204) charging heat exchange, preheating high-pressure rectification tower (T204) charging;
Give after high-pressure rectification tower (T204) the charging heat exchange steam condensate again with low-pressure distillation tower (T203) charging heat exchange, preheating low-pressure distillation tower (T203) charging;
Give after low-pressure distillation tower (T203) the charging heat exchange steam condensate again with regenerating column (T205) charging heat exchange, preheating regenerating column (T205) charging;
Give after regenerating column (T205) the charging heat exchange steam condensate again with lightness-removing column (T201) charging heat exchange, preheating lightness-removing column (T201) charging.
Heat exchange mode between said steam condensate and each the tower charging can be listed a kind of in the aforesaid combination, or the wherein combination of a few kinds of heat exchange modes.
Process method provided by the present invention; Can be chosen on above-mentioned five tower heat integrated (or six tower heat the are integrated) basis and increase an absorption tower T206 again; Lightness-removing column T201 cat head tail gas is washed in the T206 of absorption tower and goes out device again after water absorbs; To reclaim methyl alcohol wherein, improve the methanol product yield, reduce to discharge pollutant load in the non-condensable gas.
The cat head working pressure of said lightness-removing column T201 is 20～300kPa in the process method provided by the present invention; The cat head working pressure of atmospheric distillation tower T202 is 25～190kPa; The cat head working pressure of low-pressure distillation tower T203 is 150～900kPa, and the cat head working pressure of high-pressure rectification tower T204 is 300～1500kPa; The cat head working pressure of regenerating column T205 is 100～900kPa.
Process method provided by the present invention, the discharging of lightness-removing column T201 tower still can be introduced into atmospheric distillation tower T202 or be introduced into low-pressure distillation tower T203 or be introduced into high-pressure rectification tower T204 or be introduced into compression rectification tower T207.
The process method that employing fiver-tower heat integration apparatus provided by the invention carries out methanol rectification can be used for production GB premium grads methyl alcohol, U.S. mark AA level methanol product, or the methanol product of other specification.
Employing fiver-tower heat integration apparatus provided by the invention carries out the process method of methanol rectification, and whole methanol rectifying system comprises five towers such as lightness-removing column T201, atmospheric distillation tower T202, low-pressure distillation tower T203, high-pressure rectification tower T204 and regenerating column T205 and support equipment composition thereof at least.Hot integrated operation between atmospheric distillation tower, low-pressure distillation tower, high-pressure rectification tower three towers, low-pressure distillation tower cat head gas phase is as atmospheric distillation Tata still heating thermal source, for atmospheric distillation Tata still reboiler provides institute's heat requirement; High-pressure rectification column overhead gas phase is as low-pressure distillation Tata still heating thermal source, for low-pressure distillation Tata still reboiler provides institute's heat requirement.Three methanol rectification column overhead difference extraction methanol product; Only the atmospheric distillation column overhead is provided with condensing surface, high-pressure rectification Tata still is provided with reboiler, and atmospheric distillation Tata still reboiler (being the low-pressure distillation tower overhead condenser), low-pressure distillation Tata still reboiler (being high-pressure rectification column overhead condensing surface) are hot integrated interchanger.
Hot integrated operation between lightness-removing column, regenerating column two towers, regenerating column cat head gas phase is as lightness-removing column tower still heating thermal source, for lightness-removing column tower still reboiler provides institute's heat requirement.Only the lightness-removing column cat head is provided with condensing surface, recovery Tata still is provided with reboiler, and lightness-removing column tower still reboiler (being the regenerating column overhead condenser) is hot integrated interchanger.
Adopt process method provided by the invention, adopt above-mentioned two groups of hot integrated technologies, add the application of other heat exchange, power-saving technology in the system, greatly reduced the operation energy consumption of whole rectifying system.
Atmospheric distillation tower and regenerating column all need be controlled cat head and tower still methanol concentration simultaneously in the conventional four tower methanol rectification technical process, and operation easier is bigger, is difficult for stable operation.Adopt process method provided by the invention; In energy-conservation, simplified each tower and controled index: three methanol rectifying towers such as atmospheric distillation tower, low-pressure distillation tower, high-pressure rectification tower all only need to guarantee the overhead product index; Above-mentioned three Tata stills need be controlled hardly, and only regenerating column need be controlled cat head and tower still methanol concentration.Greatly improved the operational stability of whole methanol rectifying system.The present invention has overcome the shortcoming of prior art, reduces operation energy consumption more than 30%, has significant practicality and economic benefit, has a extensive future.
Description of drawings
Fig. 1 is the schema of four towers (three towers add a tower) the methanol rectification process method of prior art employing.
Fig. 2 is the process flow sheet that a kind of typical fiver-tower heat integration apparatus provided by the invention (adding the lightness-removing column tail gas absorber) carries out methanol rectification.
Fig. 3 is the process flow sheet that the typical fiver-tower heat integration apparatus of another kind provided by the invention (adding the lightness-removing column tail gas absorber) carries out methanol rectification.
Fig. 4 is the process flow sheet that a kind of typical six tower heat integration devices provided by the invention (adding the lightness-removing column tail gas absorber) carry out methanol rectification.
Embodiment
Specific embodiments of the present invention specifies as follows with reference to accompanying drawing, but for illustrative purposes only rather than limit the present invention.
Embodiment 1:
Like Fig. 2, Fig. 2 is the process flow sheet that a kind of typical fiver-tower heat integration apparatus provided by the invention (adding the lightness-removing column tail gas absorber) carries out methanol rectification.Lightness-removing column T201 tower still material 10 advanced atmospheric distillation tower T202.The thick methyl alcohol of raw material 1 elder generation and 32 heat exchange of regenerating column T205 tower still waste water gets into lightness-removing column T201 top again with after mixing methanol product 37 heat exchange.Lightness-removing column cat head gas phase 4 is after overhead condenser E201 condensation, and tail gas advances absorption tower T206, and after washing water 35 washings, non-condensable gas 7 goes out device.Absorption tower T206 tower still washings 8 gets into the lightness-removing column cat head as lightness-removing column phegma 9 together with condensing surface E201 lime set 5.Absorption tower T206 tower still oil phase 40 dischargers.
Lightness-removing column tower bottoms 10 removes atmospheric distillation tower T202.Atmospheric distillation column overhead gas phase 11 is after the E204 condensation, and lime set 12 parts are as atmospheric distillation tower phegma 13, and another part is as 14 extraction of atmospheric distillation column overhead methanol product.Atmospheric distillation tower bottoms 15 removes low-pressure distillation tower T203.Atmospheric distillation Tata still reboiler E205 provide heat by low-pressure distillation column overhead methanol steam 16.
Lime set 17 parts of low-pressure distillation tower T203 cat head methanol steam 16 are as low-pressure distillation tower phegma 18, and another part is as 19 extraction of low-pressure distillation column overhead methanol product.Low-pressure distillation tower bottoms 20 removes high-pressure rectification tower T204.Low-pressure distillation Tata still reboiler E206 provide heat by high-pressure rectification column overhead methanol steam 21.
Lime set 22 parts of high-pressure rectification tower T204 cat head methanol steam 21 are as high-pressure rectification tower phegma 23, and another part is as 24 extraction of high-pressure rectification column overhead methanol product.High-pressure rectification tower bottoms 25 removes regenerating column T205.High-pressure rectification Tata still reboiler E207 is by live steam, the conventional thermal source heating of heat conduction wet goods.
Regenerating column T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of regenerating column cat head methanol steam 26 are as regenerating column phegma 28, and another part is as 29 extraction of regenerating column cat head methanol product.Extract potato spirit 30 out by the regenerating column side line, after cooling, go out device.Reclaim tower bottoms 32 through E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several kinds of whereabouts are arranged then:,, perhaps go out device as system's waste water 36 as lightness-removing column extraction water 41 as absorption tower T206 washing water 35.
Regenerating column T205 tower still reboiler E203 is by live steam, the conventional thermal source heating of heat conduction wet goods.
Atmospheric distillation column overhead methanol product 14, low-pressure distillation column overhead methanol product 19, high-pressure rectification column overhead methanol product 24 and regenerating column cat head methanol product 29 mix; After E209 and thick methyl alcohol 2 heat exchange of raw material, after the E210 cooling, obtain refined methanol product 39 again.
Below provided a kind of typical operation conditions (working pressure not specified otherwise all refers to absolute pressure) of embodiment 1 each major equipment:
Lightness-removing column cat head working pressure 130kPa, the cat head service temperature is 73 ℃, 79 ℃ of tower still service temperatures.
Regenerating column cat head working pressure 350kPa, 99 ℃ of cat head service temperatures, 141 ℃ of tower still service temperatures.
Atmospheric distillation column overhead working pressure 130kPa, 71 ℃ of cat head service temperatures, 78 ℃ of tower still service temperatures.
Low-pressure distillation column overhead working pressure 320kPa, 96 ℃ of cat head service temperatures, 105 ℃ of tower still service temperatures.
High-pressure rectification column overhead working pressure 750kPa, 125 ℃ of cat head service temperatures, 141 ℃ of tower still service temperatures.
Absorption tower cat head working pressure 120kPa, 39 ℃ of cat head service temperatures, 46 ℃ of tower still service temperatures.
Embodiment 2:
Like Fig. 3, Fig. 3 is the process flow sheet that the typical fiver-tower heat integration apparatus of another kind provided by the invention (adding the lightness-removing column tail gas absorber) carries out methanol rectification.Lightness-removing column T201 tower still material 10 advanced high-pressure rectification tower T204.
The thick methyl alcohol of raw material 1 elder generation and 32 heat exchange of regenerating column T205 tower still waste water gets into lightness-removing column T201 top again with after mixing methanol product 37 heat exchange.Lightness-removing column cat head gas phase 4 is after overhead condenser E201 condensation, and tail gas advances absorption tower T206, and after washing water 35 washings, non-condensable gas 7 goes out device.Absorption tower T206 tower still washings 8 gets into the lightness-removing column cat head as lightness-removing column phegma 9 together with condensing surface E201 lime set 5.Absorption tower T206 tower still oil phase 40 dischargers.
Lightness-removing column tower bottoms 10 removes high-pressure rectification tower T204.High-pressure rectification column overhead gas phase 21 is after the E204 condensation, and lime set 22 parts are as high-pressure rectification tower phegma 23, and another part is as 24 extraction of high-pressure rectification column overhead methanol product.High-pressure rectification tower bottoms 25 removes low-pressure distillation tower T203.High-pressure rectification Tata still reboiler E207 is by live steam, the conventional thermal source heating of heat conduction wet goods.
Lime set 17 parts of low-pressure distillation column overhead methanol steam 16 are as low-pressure distillation tower phegma 18, and another part is as 19 extraction of low-pressure distillation column overhead methanol product.Low-pressure distillation tower bottoms 20 removes atmospheric distillation tower T202.Low-pressure distillation Tata still reboiler E206 provide heat by high-pressure rectification column overhead methanol steam 21.
Lime set 12 parts of atmospheric distillation column overhead methanol steam 11 are as atmospheric distillation tower phegma 13, and another part is as 14 extraction of atmospheric distillation column overhead methanol product.Atmospheric distillation tower bottoms 15 removes regenerating column T205.Atmospheric distillation Tata still reboiler E205 provide heat by low-pressure distillation column overhead methanol steam 16.
Regenerating column T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of regenerating column cat head methanol steam 26 are as regenerating column phegma 28, and another part is as 29 extraction of regenerating column cat head methanol product.Extract potato spirit 30 out by the regenerating column side line, after cooling, go out device.Reclaim tower bottoms 32 through E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several kinds of whereabouts are arranged then:,, perhaps go out device as system's waste water 36 as lightness-removing column extraction water 41 as absorption tower T206 washing water 35.
Reclaim Tata still reboiler E203 by live steam, the conventional thermal source heating of heat conduction wet goods.
Atmospheric distillation column overhead methanol product 14, low-pressure distillation column overhead methanol product 19, high-pressure rectification column overhead methanol product 24 and regenerating column cat head methanol product 29 mix; After E209 and thick methyl alcohol 2 heat exchange of raw material, after the E210 cooling, obtain refined methanol product 39 again.
Embodiment 3:
Like Fig. 4, Fig. 4 is the process flow sheet that a kind of typical six tower heat integration devices provided by the invention (adding the lightness-removing column tail gas absorber) carry out methanol rectification.Compare with the technical process that Fig. 2 provides, increased a compression rectification tower T207, it is integrated that atmospheric distillation tower T202, low-pressure distillation tower T203, high-pressure rectification tower T204 and compression rectification tower T207 form four tower heat, further reduces operation energy consumption.
The thick methyl alcohol of raw material 1 elder generation and 32 heat exchange of regenerating column T205 tower still waste water gets into lightness-removing column T201 top again with after mixing methanol product 37 heat exchange.Lightness-removing column cat head gas phase 4 is after overhead condenser E201 condensation, and tail gas advances absorption tower T206, and after washing water 35 washings, non-condensable gas 7 goes out device.Absorption tower T206 tower still washings 8 gets into the lightness-removing column cat head as lightness-removing column phegma 9 together with condensing surface E201 lime set 5.Absorption tower T206 tower still oil phase 40 dischargers.
Lightness-removing column tower bottoms 10 removes atmospheric distillation tower T202.Atmospheric distillation column overhead gas phase 11 is after the E204 condensation, and lime set 12 parts are as atmospheric distillation tower phegma 13, and another part is as 14 extraction of atmospheric distillation column overhead methanol product.Atmospheric distillation tower bottoms 15 removes low-pressure distillation tower T203.Atmospheric distillation Tata still reboiler E205 provide heat by low-pressure distillation column overhead methanol steam 16.
Lime set 17 parts of low-pressure distillation tower T203 cat head methanol steam 16 are as low-pressure distillation tower phegma 18, and another part is as 19 extraction of low-pressure distillation column overhead methanol product.Low-pressure distillation tower bottoms 20 removes high-pressure rectification tower T204.Low-pressure distillation Tata still reboiler E206 provide heat by high-pressure rectification column overhead methanol steam 21.
Lime set 22 parts of high-pressure rectification tower T204 cat head methanol steam 21 are as high-pressure rectification tower phegma 23, and another part is as 24 extraction of high-pressure rectification column overhead methanol product.High-pressure rectification tower bottoms 25 removes compression rectification tower T207.High-pressure rectification Tata still reboiler E207 provides heat by compression rectification tower T207 cat head methanol steam 43.
Lime set 44 parts of compression rectification tower T207 cat head methanol steam 43 are as compression rectification tower phegma 45, and another part is as 46 extraction of compression rectification column overhead methanol product.Compression rectification tower bottoms 47 removes regenerating column T205.Compression rectification Tata still reboiler E213 is by being heated by live steam, the conventional thermal source of heat conduction wet goods.
Regenerating column T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of regenerating column cat head methanol steam 26 are as regenerating column phegma 28, and another part is as 29 extraction of regenerating column cat head methanol product.Extract potato spirit 30 out by the regenerating column side line, after cooling, go out device.Reclaim tower bottoms 32 through E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several kinds of whereabouts are arranged then:,, perhaps go out device as system's waste water 36 as lightness-removing column extraction water 41 as absorption tower T206 washing water 35.
Regenerating column T205 tower still reboiler E203 is by live steam, the conventional thermal source heating of heat conduction wet goods.
Atmospheric distillation column overhead methanol product 14, low-pressure distillation column overhead methanol product 19, high-pressure rectification column overhead methanol product 24, compression rectification column overhead methanol product 46 and regenerating column cat head methanol product 29 mix; After E209 and thick methyl alcohol 2 heat exchange of raw material, after the E210 cooling, obtain refined methanol product 39 again.
Carry out the process method of methanol rectification by employing fiver-tower heat integration apparatus provided by the invention and carried out the operation energy consumption contrast as follows with extensively adopting four tower methanol rectification technologies at present:
With 600,000 tons of/year methanol devices is example, produces U.S. mark AA level methanol product, and by extensively adopting four tower methanol rectification technologies at present, the minimum steam consumption quantity of methanol rectification process is 1 ton of steam/ton methanol product.
Adopt employing fiver-tower heat integration apparatus provided by the invention to carry out the process method of methanol rectification, methanol rectification process steam consumption quantity is lower than 0.7 ton of steam/ton methanol product.
Calculate by 600,000 tons of/year methanol product:
(1-0.7) ton/ton * 600,000 ton/year=180,000 ton/year
Can save about 180,000 tons of steam every year.
By 150 yuan of calculating of steam per ton, can save the steam expense every year:
180,000 tons/year * 150 yuan/ton=2,700 ten thousand yuan/year.
The invention provides a kind of process method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, have extremely distinct economic.Specify in conjunction with embodiment, the personnel of association area can suitably change or change and make up fully according to method provided by the invention, and realizing should technology.What need special instruction is that all these are through technical process provided by the invention being carried out similar change or change and being reconfigured, and are apparent to those skilled in the art, all are regarded as in spirit of the present invention, scope and content.
Claims (8)
1. process method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, this process method are to produce methyl alcohol from thick methanol feedstock through rectifying, it is characterized in that this process method comprises:
1) comprises lightness-removing column, atmospheric distillation tower, low-pressure distillation tower, high-pressure rectification tower and five towers of regenerating column at least;
2) heat is integrated between atmospheric distillation tower, low-pressure distillation tower, high-pressure rectification tower three towers, and low-pressure distillation tower cat head gas phase is as atmospheric distillation Tata still heating thermal source, for the atmospheric distillation tower provides institute's heat requirement; High-pressure rectification column overhead gas phase is as low-pressure distillation Tata still heating thermal source, for low-pressure distillation tower provides institute's heat requirement;
3) heat is integrated between lightness-removing column and regenerating column two towers, and regenerating column cat head gas phase is as lightness-removing column tower still heating thermal source, for lightness-removing column provides institute's heat requirement;
The cat head working pressure of said low-pressure distillation tower is 150～900kPa; The cat head working pressure of high-pressure rectification tower is 300～1500kPa;
Its process is following: the advanced atmospheric distillation tower of lightness-removing column tower still material, and the thick methyl alcohol of raw material elder generation and recovery Tata still wastewater heat exchange get into lightness-removing column top again with after mixing the methanol product heat exchange; Lightness-removing column cat head gas phase is after the overhead condenser condensation, and tail gas enters the absorption tower, and after the washing water washing, non-condensable gas goes out device; Absorb Tata still washings and condensing surface lime set and get into the lightness-removing column cat head as the lightness-removing column phegma together, absorb Tata still oil phase discharger;
The lightness-removing column tower bottoms removes the atmospheric distillation tower, and atmospheric distillation column overhead gas phase is after condensation, and a lime set part is as atmospheric distillation tower phegma, and another part is as the extraction of atmospheric distillation column overhead methanol product; The atmospheric distillation tower bottoms removes low-pressure distillation tower, and atmospheric distillation Tata still reboiler provides heat by low-pressure distillation column overhead methanol steam;
The lime set part of low-pressure distillation column overhead methanol steam is as the low-pressure distillation tower phegma; Another part is as the extraction of low-pressure distillation column overhead methanol product; The low-pressure distillation tower bottoms removes the high-pressure rectification tower, and low-pressure distillation Tata still reboiler provides heat by high-pressure rectification column overhead methanol steam;
The lime set part of high-pressure rectification column overhead methanol steam is as high-pressure rectification tower phegma, and another part is as the extraction of high-pressure rectification column overhead methanol product, and the high-pressure rectification tower bottoms removes regenerating column; High-pressure rectification Tata still reboiler is by live steam, the conventional thermal source heating of thermal oil;
Regenerating column cat head methanol steam provides heat to lightness-removing column tower still reboiler; The lime set part of regenerating column cat head methanol steam is as the regenerating column phegma, and another part is as the extraction of regenerating column cat head methanol product; Extract potato spirit out by the regenerating column side line, after cooling, go out device; Reclaim tower bottoms and the thick methyl alcohol heat exchange of raw material, after the water cooler cooling, following several kinds of whereabouts are arranged then:,, perhaps go out device as system's waste water as the lightness-removing column extraction water as the absorption tower washing water;
Reclaim Tata still reboiler by live steam, the conventional thermal source heating of thermal oil;
Atmospheric distillation column overhead methanol product, low-pressure distillation column overhead methanol product, high-pressure rectification column overhead methanol product and regenerating column cat head methanol product mix, and after the thick methyl alcohol heat exchange of raw material, after cooling, obtain the refined methanol product again.
2. according to the said process method of claim 1; It is characterized in that this process method can also adopt the integrated production methyl alcohol of six towers heat; Between said atmospheric distillation tower, low-pressure distillation tower and high-pressure rectification tower three towers heat integrated outside; Also have the compression rectification tower, compression rectification column overhead gas phase is as high-pressure rectification Tata still heating thermal source, for the high-pressure rectification tower provides institute's heat requirement; It is integrated that compression rectification tower and atmospheric distillation tower, low-pressure distillation tower and high-pressure rectification tower form four tower heat.
3. according to the said process method of claim 1, it is characterized in that said thick methanol feedstock and reclaim the heat exchange of Tata still waste discharge that perhaps thick methanol feedstock and methanol product heat exchange to improve the temperature that thick methyl alcohol gets into lightness-removing column, reduce operation energy consumption.
4. according to the said process method of claim 2, it is characterized in that the energy-saving manner that adopts is: the charging of lightness-removing column, atmospheric distillation tower, low-pressure distillation tower, high-pressure rectification tower, compression rectification tower or each tower of regenerating column and the heat exchange of heating steam lime set.
5. according to claim 1 or 2 said process methodes; It is characterized in that: increase an absorption tower again on or the basis that six towers heat is integrated integrated in above-mentioned five towers heat; Lightness-removing column cat head tail gas is washed in newly-increased absorption tower and goes out device again after water absorbs; To reclaim methyl alcohol wherein, improve the methanol product yield, reduce to discharge pollutant load in the non-condensable gas.
6. according to the said process method of claim 2, it is characterized in that: the discharging of lightness-removing column tower still is introduced into the atmospheric distillation tower, is introduced into low-pressure distillation tower, is introduced into the high-pressure rectification tower or is introduced into the compression rectification tower.
7. according to the said process method of claim 1, the cat head working pressure that it is characterized in that said lightness-removing column is 20～300kPa; The cat head working pressure of atmospheric distillation tower is 25～190kPa; The cat head working pressure of low-pressure distillation tower is 150～900kPa; The cat head working pressure of high-pressure rectification tower is 300～1500kPa; The cat head working pressure of regenerating column is 100～900kPa.
8. according to the said process method of claim 1, it is characterized in that:
Lightness-removing column cat head working pressure 130kPa, the cat head service temperature is 73 ℃, 79 ℃ of tower still service temperatures;
Regenerating column cat head working pressure 350kPa, 99 ℃ of cat head service temperatures, 141 ℃ of tower still service temperatures;
Atmospheric distillation column overhead working pressure 130kPa, 71 ℃ of cat head service temperatures, 78 ℃ of tower still service temperatures;
Low-pressure distillation column overhead working pressure 320kPa, 96 ℃ of cat head service temperatures, 105 ℃ of tower still service temperatures;
High-pressure rectification column overhead working pressure 750kPa, 125 ℃ of cat head service temperatures, 141 ℃ of tower still service temperatures.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100681702A CN101503337B (en) | 2009-03-19 | 2009-03-19 | Technological process for methanol distillation by using fiver-tower heat integration apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100681702A CN101503337B (en) | 2009-03-19 | 2009-03-19 | Technological process for methanol distillation by using fiver-tower heat integration apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101503337A CN101503337A (en) | 2009-08-12 |
| CN101503337B true CN101503337B (en) | 2012-06-06 |
Family
ID=40975730
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009100681702A Active CN101503337B (en) | 2009-03-19 | 2009-03-19 | Technological process for methanol distillation by using fiver-tower heat integration apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101503337B (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040472B (en) * | 2010-11-17 | 2013-07-10 | 蓝仁水 | Energy-saving process for rectifying alcohol by adopting heat integration of three rectifying columns |
| CN102039058B (en) * | 2010-11-26 | 2012-12-26 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN106748653B (en) * | 2017-02-09 | 2023-05-02 | 天津市新天进科技开发有限公司 | Energy-saving process method and device for by-product monohydric alcohol from dehydration of dihydric alcohol aqueous solution |
| CN108101748B (en) * | 2018-02-01 | 2024-05-07 | 天津市新天进科技开发有限公司 | Four-tower three-effect methanol rectification energy-saving process method and device |
| CN109438185B (en) * | 2018-09-04 | 2021-12-24 | 北洋国家精馏技术工程发展有限公司 | Vacuum thermal coupling methanol rectification 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 |
| CN110483249A (en) * | 2019-08-14 | 2019-11-22 | 天津大学 | A kind of six tower quadruple effect rectificating method of single column steam drive type methanol of not by-product fusel oil |
| CN111116317B (en) * | 2019-12-31 | 2022-12-20 | 天津市创举科技股份有限公司 | Five-tower four-effect methanol rectification process and equipment |
| CN113233960B (en) * | 2021-06-16 | 2024-05-17 | 天津市新天进科技开发有限公司 | Multi-effect methanol rectification process method and device for avoiding ethanol accumulation |
| CN113620783A (en) * | 2021-08-18 | 2021-11-09 | 天津大学 | Reverse-forward mixed five-tower three-effect methanol rectification method using pre-rectifying tower as hot hydrazine |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817835A (en) * | 2006-01-13 | 2006-08-16 | 天津大学 | Double-efficient energy-saving methanol rectifying apparatus and method |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | Method of refining synthetic methanol with heat integration |
| CN101186557A (en) * | 2006-11-16 | 2008-05-28 | 洛阳隆华制冷设备有限公司 | Tower outside heat exchange device for menthol producing technique |
-
2009
- 2009-03-19 CN CN2009100681702A patent/CN101503337B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817835A (en) * | 2006-01-13 | 2006-08-16 | 天津大学 | Double-efficient energy-saving methanol rectifying apparatus and method |
| CN101186557A (en) * | 2006-11-16 | 2008-05-28 | 洛阳隆华制冷设备有限公司 | Tower outside heat exchange device for menthol producing technique |
| CN101012150A (en) * | 2007-02-07 | 2007-08-08 | 浙江大学 | Method of refining synthetic methanol with heat integration |
Non-Patent Citations (1)
| Title |
|---|
| 刘保柱等.节能型甲醇精馏工艺研究.《化工进展》.2007,第26卷(第5期),739-742. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101503337A (en) | 2009-08-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101503337B (en) | Technological process for methanol distillation by using fiver-tower heat integration apparatus | |
| CN1317248C (en) | Energy saving equipment of double effect rectification for methanol, and method | |
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN100526274C (en) | Method for rectifying ethanol by three-tower heat integration device | |
| CN101570466B (en) | Multi-effect rectifying process of methanol | |
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN101130484B (en) | Pressure-reducing flow-reversing dual-purpose distillation method and apparatus for refining crude methanol | |
| CN1817835A (en) | Double-efficient energy-saving methanol rectifying apparatus and method | |
| CN103555377B (en) | A kind of de-benzene method of decompression | |
| CN101786940B (en) | Methanol heat-pump rectifying process | |
| CN101693645A (en) | Methanol multitower rectifying process and rectifying equipment | |
| CN110143850A (en) | The not energy-saving methanol multi-effect distillation method of the single column steam drive of by-product fusel oil | |
| CN203007175U (en) | Heat integration device for methanol synthesis and rectification | |
| CN101602641B (en) | Double-effect rectification method and system thereof for finely separating hybrid pentane isomer | |
| CN109438185A (en) | A kind of vacuum thermal coupling methanol rectification method and device | |
| CN113233960B (en) | Multi-effect methanol rectification process method and device for avoiding ethanol accumulation | |
| CN101274881A (en) | Energy-saving method for producing dimethy ether by boiler with residual heat | |
| CN110804486A (en) | Method and system for regenerating waste lubricating oil | |
| CN101712592B (en) | Process for producing absolute ethanol through low-grade heat source | |
| CN215906119U (en) | Multi-effect methanol rectification process method device for avoiding ethanol accumulation | |
| CN102351634B (en) | New energy saving technology for benzene separation through double effect rectification and heat integration | |
| CN104744195A (en) | Post-etherification C4 purification dimethyl ether removal tower energy-saving technique | |
| CN210765075U (en) | Condensate utilization system of butadiene extraction unit | |
| CN101597091B (en) | Method for tower bottom heating of acidic water stripping device | |
| CN212152190U (en) | Coal tar three-tower continuous deep processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20090812 Assignee: Tianjin New Tianjin Technology and Development Co., Ltd. Assignor: Lan Renshui| Huang Guiming Contract record no.: 2012120000068 Denomination of invention: Technological process for methanol distillation by using fiver-tower heat integration apparatus Granted publication date: 20120606 License type: Exclusive License Record date: 20121113 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model |