CN101503337A - 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
- CN101503337A CN101503337A CNA2009100681702A CN200910068170A CN101503337A CN 101503337 A CN101503337 A CN 101503337A CN A2009100681702 A CNA2009100681702 A CN A2009100681702A CN 200910068170 A CN200910068170 A CN 200910068170A CN 101503337 A CN101503337 A CN 101503337A
- Authority
- CN
- China
- Prior art keywords
- tower
- pressure
- cat head
- rectification
- heat
- 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.)
- Granted
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 processing method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, it is an energy-saving process method of producing methyl alcohol from thick methyl alcohol by rectifying.
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 are subjected to the attention of each side.
Fig. 1 is a kind of four towers (three towers add a tower) methanol rectification processing method that extensively adopts at present, promptly adopts three towers such as pre-tower T101, pressurizing tower T102, atmospheric tower T103 to increase a recovery tower T104 again, production GB premium grads or U.S. mark AA level methanol product.Remove light constituent by pre-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 and normal pressure tower bottoms 15 advance recovery tower, obtain reclaiming methanol product 29 by the recovery tower cat head, and the recovery tower side line is extracted potato spirit 30 out, reclaim 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 processing 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 pre-tower and atmospheric tower.Relative Chinese patent CN 200610014321.2 and CN 200610013269.9, this processing method has higher energy-saving effect.But because pre-column overhead output methanol product not in the system, pressurizing tower belongs to single-action methanol rectification process for the energy that tower in advance provides.Pressurizing tower, atmospheric tower cat head output methanol product all in the system, only the energy that provides for atmospheric tower of pressurizing tower belongs to economic benefits and social benefits methanol rectification process, and therefore, though this processing 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 in proper order to the pressurizing tower in the four tower rectifyinges that extensively adopt at present and the operational condition and the rectifying of atmospheric tower, the pre-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 enters 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 condenser area is huge, simultaneously because vacuum system may 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 pre-tower and recovery tower just reaches 0.916 ton of steam/ton methanol product, if count pre-tower and recovery tower 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 processing method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, it is an energy-saving process method of producing methyl alcohol from thick methyl alcohol by rectifying, 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 processing 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 recovery tower 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 recovery tower T205 two towers, and recovery tower cat head gas phase is as lightness-removing column tower still heating thermal source, for lightness-removing column provides institute's heat requirement.
Processing 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 processing 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 enters lightness-removing column, reduce operation energy consumption.
Processing 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 recovery tower (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 recovery tower (T205) charging heat exchange, pre-heat recovery tower (T205) charging;
Give after recovery tower (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 certain several heat exchange mode.
Processing 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 processing 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 recovery tower T205 is 100～900kPa.
Processing 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 processing 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 processing 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 recovery tower 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 condenser, 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 condenser) are hot integrated interchanger.
Hot integrated operation between lightness-removing column, recovery tower two towers, recovery tower 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 condenser, recovery Tata still is provided with reboiler, and lightness-removing column tower still reboiler (being the recovery tower overhead condenser) is hot integrated interchanger.
Adopt processing 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 recovery tower 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 processing method provided by the invention, simplified each tower operation controlling index in energy-conservation: 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 recovery tower 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 processing 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 is described in detail as follows with reference to accompanying drawing, but for illustrative purposes only rather than the restriction the present invention.
Embodiment 1:
As 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 recovery tower T205 tower still waste water enters 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 and condenser E201 lime set 5 enter the lightness-removing column cat head as lightness-removing column phegma 9 together.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 recovery tower T205.High-pressure rectification Tata still reboiler E207 is by live steam, the conventional thermal source heating of heat conduction wet goods.
Recovery tower T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of recovery tower cat head methanol steam 26 are as recovery tower phegma 28, and another part is as 29 extraction of recovery tower cat head methanol product.Extract potato spirit 30 out by the recovery tower side line, after cooling, go out device.Reclaim tower bottoms 32 by E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several whereabouts is 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.
Recovery tower 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 recovery tower 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.
Recovery tower 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:
As 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 recovery tower T205 tower still waste water enters 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 and condenser E201 lime set 5 enter the lightness-removing column cat head as lightness-removing column phegma 9 together.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 recovery tower T205.Atmospheric distillation Tata still reboiler E205 provide heat by low-pressure distillation column overhead methanol steam 16.
Recovery tower T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of recovery tower cat head methanol steam 26 are as recovery tower phegma 28, and another part is as 29 extraction of recovery tower cat head methanol product.Extract potato spirit 30 out by the recovery tower side line, after cooling, go out device.Reclaim tower bottoms 32 by E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several whereabouts is 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 recovery tower 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:
As 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 recovery tower T205 tower still waste water enters 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 and condenser E201 lime set 5 enter the lightness-removing column cat head as lightness-removing column phegma 9 together.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 recovery tower T205.Compression rectification Tata still reboiler E213 is by being heated by live steam, the conventional thermal source of heat conduction wet goods.
Recovery tower T205 cat head methanol steam 26 provides heat to lightness-removing column tower still reboiler E202.Lime set 27 parts of recovery tower cat head methanol steam 26 are as recovery tower phegma 28, and another part is as 29 extraction of recovery tower cat head methanol product.Extract potato spirit 30 out by the recovery tower side line, after cooling, go out device.Reclaim tower bottoms 32 by E208 and thick methyl alcohol 1 heat exchange of raw material, after water cooler E212 cooling, following several whereabouts is 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.
Recovery tower 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 recovery tower 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 processing method of methanol rectification and extensively adopt four tower methanol rectification technologies to carry out the operation energy consumption contrast at present as follows by employing fiver-tower heat integration apparatus provided by the invention:
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 processing 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 processing method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, have extremely distinct economic.Specified in conjunction with the embodiments, the personnel of association area can suitably change or change and make up fully according to method provided by the invention, realize this technology.Of particular note, all these are by 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, a kind of processing method that adopts fiver-tower heat integration apparatus to carry out methanol rectification, this processing method is to produce methyl alcohol from thick methanol feedstock by rectifying, it is characterized in that this processing method comprises:
1) comprises lightness-removing column (T201), atmospheric distillation tower (T202), low-pressure distillation tower (T203), high-pressure rectification tower (T204) and recovery tower (T205) Wu Taita 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 recovery tower (T205) two towers, and recovery tower (T205) cat head gas phase is as lightness-removing column (T201) tower still heating thermal source, for lightness-removing column (T201) provides institute's heat requirement.
2, according to the said processing method of claim 1, it is characterized in that this processing method can also adopt the integrated production methyl alcohol of six towers heat, between said atmospheric distillation tower (T202), low-pressure distillation tower (T203) and high-pressure rectification tower (T204) three towers heat integrated outside, 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) is integrated with atmospheric distillation tower (T202), low-pressure distillation tower (T203) and high-pressure rectification tower (T204) formation four tower heat.
3, according to the said processing method of claim 1, it is characterized in that said thick methanol feedstock and the heat exchange of recovery tower (T205) tower still waste discharge, perhaps thick methanol feedstock and methanol product heat exchange to improve the temperature that thick methyl alcohol enters lightness-removing column, reduce operation energy consumption.
4, according to claim 1 or 2 said processing methodes, it is characterized in that the energy-saving manner that adopts is: the charging and the heat exchange of heating steam lime set of lightness-removing column (T201), atmospheric distillation tower (T202), low-pressure distillation tower (T203), high-pressure rectification tower (T204), compression rectification tower (T207) or each tower of recovery tower (T205).
5, according to claim 1 or 2 said processing methodes, it is characterized in that: increase an absorption tower (T206) again on or the basis that six towers heat is integrated integrated in above-mentioned five towers heat, lightness-removing column (T201) cat head tail gas is washed in absorption tower (T206) 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 claim 1 or 2 said processing methodes, it is characterized in that: the discharging of lightness-removing column (T201) tower still can be introduced into atmospheric distillation tower (T202), is introduced into low-pressure distillation tower (T203), is introduced into high-pressure rectification tower (T204) or is introduced into compression rectification tower (T207).
7, according to the said processing method of claim 1, the cat head working pressure that it is characterized in that said lightness-removing column (T201) is 20～300kPa; 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; The cat head working pressure of high-pressure rectification tower (T204) is 300～1500kPa; The cat head working pressure of recovery tower (T205) is 100～900kPa.
8, according to the said processing method of claim 1, it is characterized in that:
Lightness-removing column (T201) cat head working pressure 130kPa, the cat head service temperature is 73 ℃, 79 ℃ of tower still service temperatures;
Recovery tower (T205) cat head working pressure 350kPa, 99 ℃ of cat head service temperatures, 141 ℃ of tower still service temperatures;
Atmospheric distillation tower (T202) cat head working pressure 130kPa, 71 ℃ of cat head service temperatures, 78 ℃ of tower still service temperatures;
Low-pressure distillation tower (T203) cat head working pressure 320kPa, 96 ℃ of cat head service temperatures, 105 ℃ of tower still service temperatures;
High-pressure rectification tower (T204) cat head 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 true CN101503337A (en) | 2009-08-12 |
| CN101503337B 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) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN102040472A (en) * | 2010-11-17 | 2011-05-04 | 蓝仁水 | Energy-saving process for rectifying alcohol by adopting heat integration of three rectifying columns |
| CN106748653A (en) * | 2017-02-09 | 2017-05-31 | 天津市新天进科技开发有限公司 | The energy-saving process method and device of dihydroxylic alcohols aqueous solution dehydration by-product monohydric alcohol |
| CN108101748A (en) * | 2018-02-01 | 2018-06-01 | 天津市新天进科技开发有限公司 | Four tower triple effect methanol rectification energy-saving process methods and device |
| CN109438185A (en) * | 2018-09-04 | 2019-03-08 | 北洋国家精馏技术工程发展有限公司 | A kind of 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 |
| CN111116317A (en) * | 2019-12-31 | 2020-05-08 | 天津市创举科技股份有限公司 | Five-tower four-effect methanol rectification process and equipment |
| CN113233960A (en) * | 2021-06-16 | 2021-08-10 | 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 |
Family Cites Families (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 |
| CN101186557B (en) * | 2006-11-16 | 2011-07-27 | 洛阳隆华传热科技股份有限公司 | 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 |
-
2009
- 2009-03-19 CN CN2009100681702A patent/CN101503337B/en active Active
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040472A (en) * | 2010-11-17 | 2011-05-04 | 蓝仁水 | Energy-saving process for rectifying alcohol by adopting heat integration of three rectifying columns |
| CN102039058A (en) * | 2010-11-26 | 2011-05-04 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN102039058B (en) * | 2010-11-26 | 2012-12-26 | 天津大学 | Large-scale methanol multi-effect energy-saving rectifying device and process |
| CN106748653A (en) * | 2017-02-09 | 2017-05-31 | 天津市新天进科技开发有限公司 | The energy-saving process method and device of dihydroxylic alcohols aqueous solution dehydration by-product monohydric alcohol |
| 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 |
| CN108101748A (en) * | 2018-02-01 | 2018-06-01 | 天津市新天进科技开发有限公司 | Four tower triple effect methanol rectification energy-saving process methods and device |
| 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 |
| CN109438185A (en) * | 2018-09-04 | 2019-03-08 | 北洋国家精馏技术工程发展有限公司 | A kind of 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 |
| CN111116317A (en) * | 2019-12-31 | 2020-05-08 | 天津市创举科技股份有限公司 | Five-tower four-effect methanol rectification process and equipment |
| CN113233960A (en) * | 2021-06-16 | 2021-08-10 | 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 |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101503337B (en) | 2012-06-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101503337B (en) | Technological process for methanol distillation by using fiver-tower heat integration apparatus | |
| CN101570466B (en) | Multi-effect rectifying process of methanol | |
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN100526274C (en) | Method for rectifying ethanol by three-tower heat integration device | |
| 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 | |
| CN1760164A (en) | Energy saving equipment of double effect rectification for methanol, and method | |
| CN101786940B (en) | Methanol heat-pump rectifying process | |
| CN101693645A (en) | Methanol multitower rectifying process and rectifying equipment | |
| 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 | |
| CN110143850A (en) | The not energy-saving methanol multi-effect distillation method of the single column steam drive of by-product fusel oil | |
| CN105130760B (en) | A kind of technique of high-purity MTBE | |
| CN109438185A (en) | A kind of vacuum thermal coupling methanol rectification method and device | |
| CN110804486B (en) | Method and system for regenerating waste lubricating oil | |
| 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 | |
| CN109646980A (en) | Without the tower-coupled methanol multi-effect distillation energy saver in fusel oil next door and method | |
| CN101357879A (en) | Methanol three-tower rectification system and technique | |
| 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 | |
| CN101597091B (en) | Method for tower bottom heating of acidic water stripping device | |
| CN208008696U (en) | Four tower triple effect methanol rectification energy saving technique devices |
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 |