CN1160293C - Heat pump azeotropic rectification process and equipment for fuel ethanol - Google Patents
Heat pump azeotropic rectification process and equipment for fuel ethanol Download PDFInfo
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- CN1160293C CN1160293C CNB021455031A CN02145503A CN1160293C CN 1160293 C CN1160293 C CN 1160293C CN B021455031 A CNB021455031 A CN B021455031A CN 02145503 A CN02145503 A CN 02145503A CN 1160293 C CN1160293 C CN 1160293C
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- ethanol dehydration
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Abstract
The present invention relates to an azeotropic rectification process of a fuel ethanol heat pump and a device thereof. The device comprises an alcohol dewatering tower, an entrainer recovery tower and an alcohol recovery tower. Steam on the top parts of the three towers is pressurized to rise in temperature, and is directly used as a heat source of reboilers at the bottom of the three towers. Condensers do not need to be arranged at the top parts of the three towers, and the public work of a boiler heating system, a circulation pump, etc. do not need. The whole logistics system is fully sealed to be operated, so the production cost is greatly reduced, the gross project investment is reduced, and the moisture of the ethanol as the raw material can be produced as a byproduct. Zero release is realized and the triple benefits of economy, saving and environmental protection are obtained.
Description
One, technical field
The present invention relates to a kind of dehydrated alcohol distil process and device, particularly a kind of alcohol fuel heat pump sequence of constant boiling and rectification technology and device.
Two, background technology
According to State Standard of the People's Republic of China's " denatured fuel ethanol " (GB18350-2001) and " vehicle-use alcohol gasoline " regulation (GB18351-2001), alcohol fuel be with denaturing agent, can be used as the dehydrated alcohol that fuel is used.Denatured fuel ethanol is to be raw material with starch, saccharic, makes ethanol through fermentation, distillation, after the dehydration, adds the denaturing agent modification again and gets.With the alcohol fuel and the allotment of gasoline blend component oil of sex change, produce vehicle-use alcohol gasoline.
Promote the use of ethanol petrol, reduce gasoline on the one hand, also be the consumption of oil, on the other hand, because the alcohol fuel combustion processes mainly produces water vapour and amounts of carbon dioxide, can not produce obnoxious flavour, this gasohol is not leaded simultaneously, with improving the atmospheric environment and the vapor content in city, alleviate air pollution.The vehicle-use alcohol gasoline technology still is the new technology of a Sustainable development, because the raw material of alcohol fuel comes from grain, and grain is constantly regenerated as farm crop.
Abroad, country such as the U.S., Brazil promoted the new technology of vehicle-use alcohol gasoline as automobile fuel since 1978.Up to the present, the usage quantity of Brazil accounts for 43% of gasoline total amount, reaches 1,500 ten thousand tons/year (40% uses 192 ° of international standard alcoholic strength alcohol, and 60% uses the gasoline/alcohol mixt of 78/22 ratio), U.S.'s consumption reaches 6,000,000 tons/year, and Canada is 500,000 tons/year.
Though vehicle-use alcohol gasoline is successfully promoted the use of abroad, still be a brand-new job in China.For vehicle-use alcohol gasoline, the alcohol fuel of sex change or alcohol fuel are the bases, and the cost of material of alcohol fuel, production cost are related to the price of whole vehicle-use alcohol gasoline and the complexity of popularization, and wherein production cost is a key content.Generally speaking, the grain cost of China makes that than higher alcohol after the fermentation is on the high side, adds the distillation production cost, and the price of alcohol fuel is compared with regular gasoline, does not have competitive power at present.Therefore, under the situation that the grain cost can not obviously descend, reduce the distilling producing process cost and just seem particularly important.
The production of fuel ethanol method is a lot of at present, comprise unslaked lime evaporation, dehydration of salt method, (dissolved salt) extractive distillation method, molecular sieve preparing process, vacuum distillation method, starch absorption method, ion-exchange-resin process, sequence of constant boiling and rectification method etc., wherein, sequence of constant boiling and rectification, extractive distillation and three kinds of methods of modern molecular sieve are mainly adopted in the scale operation of alcohol fuel, and these three kinds of large scale production methods cut both ways.Traditional sequence of constant boiling and rectification fuel ethanol production technology, output is big, quality good, production is stable, technology maturation, though the molecular sieve preparing process that its energy consumption is lower than the extractive distillation method and applies at present, but it is still too high that its shortcoming is an energy consumption, and entrainment agent can not cause environmental pollution at that time in production operation.
Three, summary of the invention
The objective of the invention is to overcome the weak point of traditional sequence of constant boiling and rectification technology, sequence of constant boiling and rectification and two kinds of proven technique of heat pump techniques are organically combined, the alcohol fuel heat pump sequence of constant boiling and rectification technology and the device of a kind of energy-saving and environmental protection and minimizing facility investment is provided.
For achieving the above object, the technical solution used in the present invention is: comprise the ethanol dehydration tower, the cat head of the cat head of ethanol dehydration tower and entrainment agent recovery tower is connected with the suction side of compressor through pipeline respectively, the exhaust side of compressor is connected with the inlet end of tower still reboiler 9 and the inlet end of tower still reboiler 7 through pipeline respectively, the exit end of the exit end of tower still reboiler 9 and tower still reboiler 7 is connected through the inlet end of pipeline with the lime set quantizer, the upper strata exit end of lime set quantizer is connected with the trim the top of column end of ethanol dehydration tower through pipeline, lower floor's exit end is connected with the middle inlet end of entrainment agent recovery tower through pipeline, entrainment agent recovery tower outlet at bottom end is connected with the middle inlet end of alcohol distillation column through pipeline, ethanol dehydration tower bottom exit end is connected with the high temperature side of interchanger through pipeline, and the low temperature side of interchanger is connected with the middle inlet end of feed ethanol pipeline and ethanol dehydration tower respectively.
The cat head of alcohol distillation column of the present invention is connected with the suction side of compressor through pipeline, the exhaust side of compressor is connected through the inlet end of pipeline with tower still reboiler 8, and the outlet of tower still reboiler 8 is connected with the trim the top of column end of alcohol distillation column and the middle inlet end of ethanol dehydration tower through pipeline respectively; Compressor is the heat pump vapour compressor.
The technology of employing of the present invention is: the ternary azeotrope steam of ethanol dehydration column overhead directly heats up by the pressurization of heat pump vapour compressor, and as the solution in the thermal source heating tower still reboiler of tower still reboiler;
Phlegma after the compression of heat pump vapour compressor flows into elevated lime set quantizer through pipeline;
In the lime set quantizer, the rich benzene on upper strata refluxes as the ethanol dehydration column overhead and enters the ethanol dehydration tower, and lower floor's water-rich phase flows into the entrainment agent recovery tower and reclaims entrainment agent, and the solution of entrainment agent recovery tower bottom second alcohol and water is sent into alcohol distillation column again;
Alcohol distillation column cat head alcohol-water binary azeotrope steam is heated up as the thermal source of tower still reboiler by the pressurization of heat pump vapour compressor, its phlegma part enters alcohol distillation column as backflow alcohol distillation column trim the top of column liquid, all the other feed ethanol as raw material alcohol and the preheating of process interchanger together enter the ethanol dehydration tower, and high-temperature product is alcohol fuel at the bottom of the tower of ethanol dehydration tower.
One of its component of ternary azeotrope steam of ethanol dehydration column overhead of the present invention is called entrainment agent, and entrainment agent can be a benzene, also can be pentane, ethylene glycol, cyclohexane etc.
Because the whole logistics system totally closed operation of the present invention, do not need overhead condenser, do not need general facilitiess such as boiler heating system and recycle pump yet, production cost reduces greatly, the total investment of engineering expense reduces, the moisture of all right by-product feed ethanol, ordinary production does not have any product refuse and environmental pollution.
Four, description of drawings
Accompanying drawing 1 is a technical process schematic diagram of the present invention.
Five, embodiment
Below in conjunction with accompanying drawing the present invention is described in further detail.
Referring to Fig. 1, the present invention includes ethanol dehydration tower 1, the cat head of ethanol dehydration tower 1 is connected through the suction side of pipeline with heat pump vapour compressor 5, the exhaust side of heat pump vapour compressor 5 is connected with the inlet end of tower still reboiler 9 and the inlet end of tower still reboiler 7 through pipeline respectively, the exit end of the exit end of tower still reboiler 9 and tower still reboiler 7 together is connected through the inlet end of pipeline with lime set quantizer 4, in lime set quantizer 4, the exit end on upper strata is connected with the trim the top of column end of ethanol dehydration tower 1 through pipeline, the exit end of lower floor is connected with the middle inlet end of entrainment agent recovery tower 2 through pipeline, the cat head of entrainment agent recovery tower 2 is connected through the suction side of pipeline with heat pump vapour compressor 5, entrainment agent recovery tower 2 outlet at bottom ends are connected with the middle inlet end of alcohol distillation column 3 through pipeline, the cat head of alcohol distillation column 3 is connected through the suction side of pipeline with heat pump vapour compressor 6, the exhaust side of heat pump vapour compressor 6 is connected through the inlet end of pipeline with the tower still reboiler 8 of alcohol distillation column 3, the outlet of tower still reboiler 8 is connected with the trim the top of column end of alcohol distillation column 3 and the middle inlet end of ethanol dehydration tower 1 through pipeline respectively, and alcohol distillation column 3 outlet at bottom ends remove aqua storage tank through pipeline.Ethanol dehydration tower 1 outlet at bottom end is connected with the high temperature side entrance end of interchanger 10 through pipeline, the high temperature side exit end of interchanger 10 removes product library through pipeline, the low temperature side entrance end of interchanger 10 is connected with the feed ethanol pipeline, and the low temperature side exit end of interchanger 10 is connected with the middle inlet end of ethanol dehydration tower 1 through pipeline.
Principle of work of the present invention is as follows:
Its phlegma part of alcohol distillation column cat head alcohol-water binary azeotrope steam (78 ℃) is as refluxing, and all the other get back to the ethanol dehydration tower as raw material alcohol.
The overhead vapours of the overhead vapours of ethanol dehydration tower 1 and entrainment agent recovery tower 2, be connected through the suction side of pipeline with heat pump vapour compressor 5, after being compressed, steam is divided into two-way, one the tunnel enters the tower still reboiler 9 of ethanol dehydration tower 1 through pipeline, another road enters the tower still reboiler 7 of entrainment agent recovery tower 2 through pipeline, the ternary azeotrope steam of ethanol dehydration tower 1 cat head (as: benzene-ethanol-water azeotropic point is 64.6 ℃), without condensation, directly heat up by 5 pressurizations of heat pump vapour compressor, and as tower still reboiler 7,9 thermal source, heating tower's still reboiler 7 respectively, solution in 9, steam is condensed into liquid, together flow into elevated lime set quantizer 4 through pipeline again, in lime set quantizer 4, the rich benzene on upper strata is as the trim the top of column liquid of ethanol dehydration tower 1, enter ethanol dehydration tower 1, lower floor's water-rich phase is by self liquid level difference, flow into entrainment agent recovery tower 2 and reclaim entrainment agent, the overhead vapours of entrainment agent recovery tower 2, be connected through the suction side of pipeline with heat pump vapour compressor 5, the solution of entrainment agent recovery tower 2 bottom second alcohol and waters is sent into alcohol distillation column 3 again, alcohol distillation column 3 cat head alcohol-water binary azeotrope steam are equally without condensation, heat up as the thermal source of alcohol distillation column 3 tower still reboilers 8 by 6 pressurizations of heat pump vapour compressor, enter tower still reboiler 8 through pipeline, solution in heating tower's still, steam is condensed into liquid, a phlegma part is as the trim the top of column liquid of alcohol distillation column 3, all the other feed ethanol of getting back to ethanol dehydration tower 1 and 10 preheatings of process interchanger as raw material alcohol together enter ethanol dehydration tower 1, the bottom product of ethanol dehydration tower 1 is the pyritous alcohol fuel, as thermal source preheating material ethanol in interchanger 10, cooled alcohol fuel removes product library through pipeline, the bottom product of alcohol distillation column 3 is a water, removes aqua storage tank through pipeline.
Claims (5)
1, a kind of alcohol fuel heat pump sequence of constant boiling and rectification device, it is characterized in that: comprise ethanol dehydration tower [1], the cat head of the cat head of ethanol dehydration tower [1] and entrainment agent recovery tower [2] is connected through the suction side of pipeline with compressor [5] respectively, the exhaust side of compressor [5] is connected with the inlet end of tower still reboiler [9] and the inlet end of tower still reboiler [7] through pipeline respectively, the exit end of the exit end of tower still reboiler [9] and tower still reboiler [7] is connected through the inlet end of pipeline with lime set quantizer [4], the upper strata exit end of lime set quantizer [4] is connected through the trim the top of column end of pipeline with ethanol dehydration tower [1], lower floor's exit end is connected through the middle inlet end of pipeline with entrainment agent recovery tower [2], entrainment agent recovery tower [2] outlet at bottom end is connected through the middle inlet end of pipeline with alcohol distillation column [3], ethanol dehydration tower [1] outlet at bottom end is connected through the high temperature side of pipeline with interchanger [10], and the low temperature side of interchanger [10] is connected with the middle inlet end of feed ethanol pipeline and ethanol dehydration tower [1] respectively.
2, alcohol fuel heat pump sequence of constant boiling and rectification device according to claim 1, it is characterized in that: the cat head of said alcohol distillation column [3] is connected through the suction side of pipeline with compressor [6], the exhaust side of compressor [6] is connected through the inlet end of pipeline with tower still reboiler [8], and the outlet of tower still reboiler [8] is connected with the trim the top of column end of alcohol distillation column [3] and the middle inlet end of ethanol dehydration tower [1] through pipeline respectively.
3, alcohol fuel heat pump sequence of constant boiling and rectification device according to claim 1, it is characterized in that: said compressor [5], compressor [6] are the heat pump vapour compressor.
4, a kind of alcohol fuel heat pump sequence of constant boiling and rectification technology of using the described alcohol fuel heat pump of claim 1 sequence of constant boiling and rectification device, it is characterized in that: the ternary azeotrope steam of ethanol dehydration tower [1] cat head directly heats up by heat pump vapour compressor [5] pressurization, and as the solution in the thermal source heating tower still reboiler [7,9] of tower still reboiler [7,9];
Phlegma after heat pump vapour compressor [5] compression flows into elevated lime set quantizer [4] through pipeline;
In lime set quantizer [4], the rich benzene on upper strata refluxes as the ethanol dehydration column overhead and enters ethanol dehydration tower [1], lower floor's water-rich phase flows into entrainment agent recovery tower [2] and reclaims entrainment agent, and the solution of entrainment agent recovery tower [2] bottom second alcohol and water is sent into alcohol distillation column [3] again;
Alcohol distillation column [3] cat head alcohol-water binary azeotrope steam is heated up as the thermal source of tower still reboiler [8] by heat pump vapour compressor [6] pressurization, its phlegma part enters alcohol distillation column [3] as backflow alcohol distillation column [3] trim the top of column liquid, all the other feed ethanol as raw material alcohol and the preheating of process interchanger [10] together enter ethanol dehydration tower [1], and high-temperature product is alcohol fuel at the bottom of the tower of ethanol dehydration tower [1].
5, alcohol fuel heat pump sequence of constant boiling and rectification technology according to claim 4, it is characterized in that: one of its component of ternary azeotrope steam of said ethanol dehydration tower [1] cat head is called entrainment agent, entrainment agent can be a benzene, also can be pentane, ethylene glycol, cyclohexane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021455031A CN1160293C (en) | 2002-12-10 | 2002-12-10 | Heat pump azeotropic rectification process and equipment for fuel ethanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021455031A CN1160293C (en) | 2002-12-10 | 2002-12-10 | Heat pump azeotropic rectification process and equipment for fuel ethanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1417182A CN1417182A (en) | 2003-05-14 |
| CN1160293C true CN1160293C (en) | 2004-08-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB021455031A Expired - Fee Related CN1160293C (en) | 2002-12-10 | 2002-12-10 | Heat pump azeotropic rectification process and equipment for fuel ethanol |
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| CN (1) | CN1160293C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100412051C (en) * | 2006-02-28 | 2008-08-20 | 华南理工大学 | Heat pump rectifying prodn. process and plant for n-butyl acetate |
| CN101381279B (en) * | 2008-10-15 | 2011-06-01 | 天津大学 | Fuel ethanol dehydration apparatus and method |
| CN101525272B (en) * | 2009-04-07 | 2012-05-30 | 天津大学 | Ethanol distillation dehydration energy saving technique and device |
| CN102661654B (en) * | 2012-05-02 | 2014-04-30 | 北京华宇同方化工科技开发有限公司 | Method and system for preparing high purity gas by rectification method |
| CN102719282A (en) * | 2012-07-03 | 2012-10-10 | 华东理工大学 | Ethanol-water separation method based on automotive fuel and with methyl tertiary butyl ether (MTBE) serving as entrainer |
| CN103058909B (en) * | 2012-12-13 | 2016-01-20 | 中国电器科学研究院有限公司 | A kind of recovery process of N-Methyl pyrrolidone |
| CN108543324A (en) * | 2018-04-25 | 2018-09-18 | 四川子仁制药有限公司 | Andrographolide production alcohol recycle recycling equipment and its application method |
| CN109678668B (en) * | 2018-11-23 | 2021-12-17 | 滨州学院 | Ethanol-tert-butanol-water refining fractionation method |
| CN111018925A (en) * | 2019-12-18 | 2020-04-17 | 广西浦北制药厂 | Steam system working process in trinosin production |
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2002
- 2002-12-10 CN CNB021455031A patent/CN1160293C/en not_active Expired - Fee Related
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| CN1417182A (en) | 2003-05-14 |
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Granted publication date: 20040804 Termination date: 20101210 |