CN104047650A - Method and device for converting surplus energy on distillation tower top into electric energy - Google Patents
Method and device for converting surplus energy on distillation tower top into electric energy Download PDFInfo
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- CN104047650A CN104047650A CN201410298819.0A CN201410298819A CN104047650A CN 104047650 A CN104047650 A CN 104047650A CN 201410298819 A CN201410298819 A CN 201410298819A CN 104047650 A CN104047650 A CN 104047650A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
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Abstract
The invention relates to a method and device for converting surplus energy on the distillation tower top into electric energy. The gas-phase surplus energy on the distillation tower top is made full use of, another working medium having heat transfer temperature difference with the gas-phase surplus energy is adopted for heat transfer, and energy needed for evaporation and expansion is provided for the working medium. The device is mainly composed of a distillation tower, a phase-change heat removal device, a heat removal material flow condenser, a heat removal material flow circulation pump, a generator, a distillation tower condensate receiving tank, a distillation tower condensate conveying pump and the like. The gas-phase surplus energy on the distillation tower top cooled by air and water originally is fully recycled and converted into electric energy, and energy recovery and utilization are achieved in the process. According to the method and device, the gas-phase surplus energy which can not be recycled easily on the distillation tower top can be made full use of, heat energy is converted into mechanical energy and then is converted into electric energy, and the energy of a distillation device can be utilized and recycled to the maximum extent. The method and device have the advantages of being simple in technological process, low in equipment investment, convenient to operate and capable of fully recycling the gas-phase surplus energy on the tower top.
Description
Technical field
The present invention relates to stripping technique and equipment field, particularly relate to a kind of method and device that tower top complementary energy is converted into electric energy that distill.
Background technique
Still-process is one of chemical engineering unit operation that in chemical industry, energy consumption is high.From energy essence, analyze, distillation is the process of diffusion useful energy that physics useful energy is converted into, and is accompanied by the depression of order loss of physics useful energy in process.The reason that causes its process exergy loss is the nonreversibility of mixing the mobile Pressure Drop of mass transfer between the uneven logistics of phase concentration or the mixing between variable concentrations logistics, heat transfer, fluid between different temperatures logistics.
Still-process evaporates by multi-stage condensing, realizes the separation of different boiling component from mixed solution.In general fractionating tower, the energy of reboiler 95% is taken away by the cooling water in overhead condenser or cooling-air, and only 5% energy is used effectively.Simultaneously again because heat transmission equipment fouling, water vapour leak, and device maintenance is bad and the other problems that causes etc. further reduce the original very low capacity usage ratio of still-process.
Out, major part enters condenser to distillation top gaseous phase, by cooling medium, is cooled to after liquid phase, carries out extraction, or the operation refluxing with product extraction.Condenser effect is only cooling to gas phase, if gas phase potential temperature is higher, with other logistics, carries out heat exchange, realizes heat recovery, but the energy that temperature has in the gas phase below 100 ℃, most of to adopt air-cooled, water-cooled to carry out cooling, and this part heat can not utilize substantially, is called as " complementary energy ".
If can realize utilization and the recovery of distillation top gaseous phase " complementary energy " by advanced technological means, the object that really reach energy-saving and cost-reducing, reduces product cost, the impetus developing for China's oil chemical industry is quite huge.
Summary of the invention
The present invention is with on the basis of realizing top gaseous phase energy and fully reclaiming, and proposition a kind of distills method and the device that tower top complementary energy is converted into electric energy.
The object of the invention is to make full use of the gas phase complementary energy of distillation tower top, by adopting the another kind of working medium heat exchange that has heat transfer temperature difference with it, provide evaporation expansion needed energy to this kind of working medium, thereby make its acting of expanding that complementary energy is converted into electric energy, have that technological process is simple, equipment investment is lower, easy to operate, can fully reclaim the advantages such as top gaseous phase complementary energy.
Distillation tower top complementary energy of the present invention is converted into electrical energy devices, mainly fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump etc., consists of.The feature of method of the present invention and device is fully to reclaim originally by the complementary energy of the top gaseous phase of air cooling and cooling by water, is converted into electric energy, and implementation procedure energy reclaims and utilizes.
Technological scheme of the present invention is as follows:
A kind ofly distill the device that tower top complementary energy is converted into electric energy; Comprise fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump and relevant feeding line and the pipeline that is connected above equipment; The outlet of fractionating tower top gaseous phase is connected to phase transformation heat-exchanger, and the hot side outlet of phase transformation heat-exchanger is connected to fractionating tower condensed fluid receiving tank, and the outlet of condensed fluid receiving tank is connected to the import of fractionating tower condensed fluid transfer pump, and pump discharge is connected to fractionating tower refluxing opening and products export; Heat-obtaining logistics recycle pump is connected to the cold side import of phase transformation heat-exchanger, the cold mouth of measuring of phase transformation heat-exchanger is connected to the expander inlet that drives generator, decompressor outlet is connected to the import of heat-obtaining logistics condenser, and heat-obtaining logistics condensator outlet is connected to heat-obtaining logistics pump entry.
Distillation tower top complementary energy of the present invention is converted into the operating method of electric energy, fractionating tower top gaseous phase enters the hot side of phase transformation heat-exchanger, take heat condensed fluid away and enter fractionating tower condensed fluid receiving tank, receiving tank extraction condensed fluid is through a fractionating tower condensed fluid transfer pump outlet liquid part as reflux liquid, and a part is as product Produced Liquid; After the outlet heat-obtaining of phase transformation heat-exchanger cold side, logistics enters the decompressor with generator, the heat-obtaining logistics condensed fluid of decompressor outlet heat-obtaining logistics after heat-obtaining logistics condenser enters heat-obtaining logistics recycle pump, and the cold side of phase transformation heat-exchanger is got back in the logistics of heat-obtaining logistics circulating-pump outlet.
Distillation tower top complementary energy of the present invention is converted into method and the device of electric energy, its advantage is to make full use of " complementary energy " of the difficult recovery that distillation top gaseous phase has, and heat energy is converted into mechanical energy and then changes electric energy into, can farthest realize utilization and the recovery of rectifier unit energy.
Accompanying drawing explanation
Fig. 1 distills the schematic flow sheet that tower top complementary energy is converted into electric energy.
Equipment: T1. fractionating tower, E1. phase transformation heat-exchanger, E2. heat-obtaining logistics condenser, C1. fractionating tower condensed fluid receiving tank, P1. fractionating tower condensed fluid transfer pump, P2. heat-obtaining logistics recycle pump, F1. decompressor, D1. generator
Logistics: S1. distills top gaseous phase, S2. condensed fluid, S3. receiving tank extraction condensed fluid, S4. condensed fluid transfer pump outlet liquid, S5. reflux liquid, S6. product Produced Liquid, S7. discharging at the bottom of fractionating tower, logistics after S8. heat-obtaining, the logistics of S9. decompressor outlet heat-obtaining, S10. heat-obtaining logistics condensed fluid, the logistics of S11. heat-obtaining logistics circulating-pump outlet
Embodiment
Below in conjunction with accompanying drawing, method provided by the present invention and device are further detailed.
The present invention is achieved through the following technical solutions:
Distillation tower top complementary energy of the present invention is converted into the device of electric energy, comprises fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump and relevant feeding line and the pipeline that is connected above equipment; It is characterized in that: the outlet of fractionating tower top gaseous phase is connected to phase transformation heat-exchanger, the hot side outlet of phase transformation heat-exchanger is connected to fractionating tower condensed fluid receiving tank, the outlet of condensed fluid receiving tank is connected to the import of fractionating tower condensed fluid transfer pump, and pump discharge is connected to fractionating tower refluxing opening and products export; Heat-obtaining logistics recycle pump is connected to the cold side import of phase transformation heat-exchanger, the cold mouth of measuring of phase transformation heat-exchanger is connected to the expander inlet that drives generator, decompressor outlet is connected to the import of heat-obtaining logistics condenser, and heat-obtaining logistics condensator outlet is connected to heat-obtaining logistics pump entry.
The operating method that distillation tower top complementary energy of the present invention is converted into the device of electric energy is: fractionating tower (T1) top gaseous phase (S1) enters the hot side of phase transformation heat-exchanger (E1), take heat condensed fluid (S2) away and enter fractionating tower condensed fluid receiving tank (C1), receiving tank extraction condensed fluid (S3) is through fractionating tower condensed fluid transfer pump (P1) outlet liquid (S4) part as reflux liquid (S5), and a part is as product Produced Liquid (S6); After the outlet heat-obtaining of phase transformation heat-exchanger cold side, logistics (S8) enters the decompressor (F1) with generator (D1), the heat-obtaining logistics condensed fluid (S10) of decompressor outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and the cold side of phase transformation heat-exchanger (E1) is got back in heat-obtaining logistics circulating-pump outlet logistics (S11).
Technology and equipment of the present invention can be widely used in distilling the callback course of top gaseous phase complementary energy, in order to illustrate that better the present invention is in the advantage aspect product purity and yield, choosing wherein two application examples is illustrated, but therefore do not limit the Applicable scope of this technology and equipment, accompanying drawing, for explanation the present invention draws, is not construed as limiting concrete application form of the present invention.
Embodiment 1
Still-process by the inventive method for the separation of ethanol water, as shown in Figure 1, comprise fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump and relevant feeding line and the pipeline that is connected above equipment; The outlet of fractionating tower top gaseous phase is connected to phase transformation heat-exchanger, and the hot side outlet of phase transformation heat-exchanger is connected to fractionating tower condensed fluid receiving tank, and the outlet of condensed fluid receiving tank is connected to the import of fractionating tower condensed fluid transfer pump, and pump discharge is connected to fractionating tower refluxing opening and products export; Heat-obtaining logistics recycle pump is connected to the cold side import of phase transformation heat-exchanger, the cold mouth of measuring of phase transformation heat-exchanger is connected to the expander inlet that drives generator, decompressor outlet is connected to the import of heat-obtaining logistics condenser, and heat-obtaining logistics condensator outlet is connected to heat-obtaining logistics pump entry.
Fractionating tower (T1) atmospheric operation, top gaseous phase (S1) is the azeotropic mixture of ethanol water, temperature is 78 ℃, flow is 300kg/h, enter the hot side of phase transformation heat-exchanger (E1), adopting temperature is that to take heat away be 73kW for the working medium of 40 ℃, top gaseous phase is all condensed into liquid phase, condensed fluid (S2) enters fractionating tower condensed fluid receiving tank (C1), receiving tank extraction condensed fluid (S3) is through fractionating tower condensed fluid transfer pump (P1) outlet liquid (S4) part as reflux liquid (S5), and a part is as product Produced Liquid (S6); After the outlet heat-obtaining of phase transformation heat-exchanger cold side, logistics (S8) enters the decompressor (F1) with generator (D1), the heat-obtaining logistics condensed fluid (S10) of decompressor outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and the cold side of phase transformation heat-exchanger (E1) is got back in heat-obtaining logistics circulating-pump outlet logistics (S11).
Make full use of the complementary energy of the middle low temperature of the difficult recovery that has of distillation top gaseous phase, and heat is converted into mechanical energy and then changes electric energy into, can farthest realize utilization and the recovery of rectifier unit energy.This installs final generated energy is 2.9kW.
Embodiment 2
The inventive method is used for to the cyelohexanone still-process separated with cyclohexanol, as shown in Figure 1, comprise fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump and relevant feeding line and the pipeline that is connected above equipment; The outlet of fractionating tower top gaseous phase is connected to phase transformation heat-exchanger, and the hot side outlet of phase transformation heat-exchanger is connected to fractionating tower condensed fluid receiving tank, and the outlet of condensed fluid receiving tank is connected to the import of fractionating tower condensed fluid transfer pump, and pump discharge is connected to fractionating tower refluxing opening and products export; Heat-obtaining logistics recycle pump is connected to the cold side import of phase transformation heat-exchanger, the cold mouth of measuring of phase transformation heat-exchanger is connected to the expander inlet that drives generator, decompressor outlet is connected to the import of heat-obtaining logistics condenser, and heat-obtaining logistics condensator outlet is connected to heat-obtaining logistics pump entry.
Fractionating tower (T1) operation pressure is 53kPa, the cyelohexanone that top gaseous phase (S1) is 99%, temperature is 123.7 ℃, flow is 1200kg/h, enter the hot side of phase transformation heat-exchanger (E1), adopting temperature is that to take heat away be 159.78kW for the working medium of 60 ℃, gas phase is all condensed into liquid phase, condensed fluid (S2) enters fractionating tower condensed fluid receiving tank (C1), receiving tank extraction condensed fluid (S3) is through fractionating tower condensed fluid transfer pump (P1) outlet liquid (S4) part as reflux liquid (S5), and a part is as product Produced Liquid (S6); After the outlet heat-obtaining of phase transformation heat-exchanger cold side, logistics (S8) enters the decompressor (F1) with generator (D1), the heat-obtaining logistics condensed fluid (S10) of decompressor outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and the cold side of phase transformation heat-exchanger (E1) is got back in heat-obtaining logistics circulating-pump outlet logistics (S11).
Make full use of the middle low temperature complementary energy of the difficult recovery that has of distillation top gaseous phase, and heat is converted into mechanical energy and then changes electric energy into, can farthest realize utilization and the recovery of rectifier unit energy.This installs final generated energy is 8.01kW.
The distillation tower top complementary energy that the present invention proposes is converted into method and the device of electric energy, by preferred embodiment, be described, person skilled obviously can be changed equipment and process flow process as herein described or suitably change and combination within not departing from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is, all similar replacements and change apparent to those skilled in the artly, they are deemed to be included in spirit of the present invention, scope and content.
Claims (2)
1. one kind is distilled the device that tower top complementary energy is converted into electric energy; Comprise fractionating tower, phase transformation heat-exchanger, heat-obtaining logistics condenser, heat-obtaining logistics recycle pump, generator, fractionating tower condensed fluid receiving tank, fractionating tower condensed fluid transfer pump and relevant feeding line and the pipeline that is connected above equipment; It is characterized in that: the outlet of fractionating tower top gaseous phase is connected to phase transformation heat-exchanger, the hot side outlet of phase transformation heat-exchanger is connected to fractionating tower condensed fluid receiving tank, the outlet of condensed fluid receiving tank is connected to the import of fractionating tower condensed fluid transfer pump, and pump discharge is connected to fractionating tower refluxing opening and products export; Heat-obtaining logistics recycle pump is connected to the cold side import of phase transformation heat-exchanger, the cold mouth of measuring of phase transformation heat-exchanger is connected to the expander inlet that drives generator, decompressor outlet is connected to the import of heat-obtaining logistics condenser, and heat-obtaining logistics condensator outlet is connected to heat-obtaining logistics pump entry.
2. the distillation tower top complementary energy of claim 1 is converted into the operating method of electric energy, it is characterized in that fractionating tower top gaseous phase enters the hot side of phase transformation heat-exchanger, take heat condensed fluid away and enter fractionating tower condensed fluid receiving tank, receiving tank extraction condensed fluid is through a fractionating tower condensed fluid transfer pump outlet liquid part as reflux liquid, and a part is as product Produced Liquid; After the outlet heat-obtaining of phase transformation heat-exchanger cold side, logistics enters the decompressor with generator, the heat-obtaining logistics condensed fluid of decompressor outlet heat-obtaining logistics after heat-obtaining logistics condenser enters heat-obtaining logistics recycle pump, and the cold side of phase transformation heat-exchanger is got back in the logistics of heat-obtaining logistics circulating-pump outlet.
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| CN201410298819.0A CN104047650A (en) | 2014-06-26 | 2014-06-26 | Method and device for converting surplus energy on distillation tower top into electric energy |
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| CN201410298819.0A CN104047650A (en) | 2014-06-26 | 2014-06-26 | Method and device for converting surplus energy on distillation tower top into electric energy |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106492496A (en) * | 2016-11-28 | 2017-03-15 | 南京航空航天大学 | Generating rectifying integral system and method for work |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4149940A (en) * | 1976-12-22 | 1979-04-17 | Imperial Chemical Industries Limited | Methanol |
| US4382366A (en) * | 1981-12-07 | 1983-05-10 | Air Products And Chemicals, Inc. | Air separation process with single distillation column for combined gas turbine system |
| CN101709661A (en) * | 2009-12-11 | 2010-05-19 | 中冶京诚工程技术有限公司 | Waste heat power generation system and power generation method |
| US20120031096A1 (en) * | 2010-08-09 | 2012-02-09 | Uop Llc | Low Grade Heat Recovery from Process Streams for Power Generation |
| TW201211375A (en) * | 2010-08-27 | 2012-03-16 | Uop Llc | Energy conversion using RANKINE cycle system |
| CN204024737U (en) * | 2014-06-26 | 2014-12-17 | 天津大学 | Distillation tower top complementary energy is converted into the device of electric energy |
-
2014
- 2014-06-26 CN CN201410298819.0A patent/CN104047650A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4149940A (en) * | 1976-12-22 | 1979-04-17 | Imperial Chemical Industries Limited | Methanol |
| US4382366A (en) * | 1981-12-07 | 1983-05-10 | Air Products And Chemicals, Inc. | Air separation process with single distillation column for combined gas turbine system |
| JPS58115277A (en) * | 1981-12-07 | 1983-07-08 | エア−・プロダクツ・アンド・ケミカルス・インコ−ポレ−テツド | Method of separating high-purity oxygen from air |
| CN101709661A (en) * | 2009-12-11 | 2010-05-19 | 中冶京诚工程技术有限公司 | Waste heat power generation system and power generation method |
| US20120031096A1 (en) * | 2010-08-09 | 2012-02-09 | Uop Llc | Low Grade Heat Recovery from Process Streams for Power Generation |
| TW201211375A (en) * | 2010-08-27 | 2012-03-16 | Uop Llc | Energy conversion using RANKINE cycle system |
| CN204024737U (en) * | 2014-06-26 | 2014-12-17 | 天津大学 | Distillation tower top complementary energy is converted into the device of electric energy |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106492496A (en) * | 2016-11-28 | 2017-03-15 | 南京航空航天大学 | Generating rectifying integral system and method for work |
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Application publication date: 20140917 |