CN204024737U - Distillation tower top complementary energy is converted into the device of electric energy - Google Patents
Distillation tower top complementary energy is converted into the device of electric energy Download PDFInfo
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- CN204024737U CN204024737U CN201420350983.7U CN201420350983U CN204024737U CN 204024737 U CN204024737 U CN 204024737U CN 201420350983 U CN201420350983 U CN 201420350983U CN 204024737 U CN204024737 U CN 204024737U
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- fractionating tower
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- 230000000295 complement effect Effects 0.000 title claims abstract description 25
- 238000004821 distillation Methods 0.000 title description 13
- 239000012530 fluid Substances 0.000 claims abstract description 57
- 239000012071 phase Substances 0.000 claims abstract description 50
- 230000009466 transformation Effects 0.000 claims abstract description 43
- 239000007792 gaseous phase Substances 0.000 claims abstract description 22
- 238000012546 transfer Methods 0.000 claims abstract description 21
- 230000008676 import Effects 0.000 claims abstract description 18
- 238000010992 reflux Methods 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 abstract description 22
- 238000011084 recovery Methods 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 description 15
- 238000000605 extraction Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- -1 fractionating tower Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- 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
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to and a kind ofly distills the device that tower top complementary energy is converted into electric energy; Overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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.Abundant recovery by the complementary energy of the top gaseous phase of air cooling and cooling by water, was converted into electric energy, implementation procedure energy regenerating and utilization originally.Have equipment investment lower, easy to operate, can fully reclaim the advantages such as top gaseous phase complementary energy.
Description
Technical field
The utility model relates to stripping technique and equipment field, particularly relates to a kind ofly distilling the device that tower top complementary energy is converted into electric energy.
Background technique
Still-process is one of chemical engineering unit operation that in chemical industry, energy consumption is high.Analyze from energy essence, distillation is process physics useful energy being converted into diffusion useful energy, loses in process along with the depression of order of physics useful energy.The reason of its process exergy loss is caused to be the nonreversibility of Pressure Drop of heat transfer between the mass transfer between the uneven logistics of mixed phase concentration or the mixing between variable concentrations logistics, different temperatures logistics, fluid flowing.
Still-process is evaporated by multi-stage condensing, realizes different boiling component from the separation 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 the energy of 5% is used effectively.Simultaneously again because heat transmission equipment fouling, water vapour leak, and the bad and other problems etc. that causes of device maintenance, the original very low capacity usage ratio of still-process is reduced further.
Out, major part enters condenser to distillation top gaseous phase, after being cooled to liquid phase, carries out extraction by cooling medium, or carries out the operation of backflow and product extraction.Condenser effect is only the cooling to gas phase, if gas phase potential temperature is higher carry out heat exchange with other logistics, realizes heat recovery, but the energy that the gas phase of temperature below 100 DEG C has, major part employing is air-cooled, water-cooled cools, and this part heat can not utilize substantially, is called as " complementary energy ".
If the technological means by advanced person realizes utilization and the recovery of distillation top gaseous phase " complementary energy ", really reach energy-saving and cost-reducing, reduce the object of product cost, the impetus for the development of China's oil chemical industry is then quite huge.
Summary of the invention
The utility model is with on the basis realizing top gaseous phase energy and fully reclaim, and a kind of of proposition distills the device that tower top complementary energy is converted into electric energy.
The purpose of this utility model is the gas phase complementary energy making full use of distillation tower top, by adopting the another kind of working medium heat exchange that there is heat transfer temperature difference with it, the energy required for evaporation expansion is provided to this kind of working medium, thus make its expansion work 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 utility model is converted into electrical energy devices, primarily of compositions such as 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 pumps.The feature of method of the present utility model 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, implementation procedure energy regenerating and utilization.
The technical solution of the utility model 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 feedstocks pipeline and the pipeline being connected above equipment; Overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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.
Overhead gas phase enters the hot side of phase transformation heat-exchanger, takes heat condensed fluid away and enters fractionating tower condensed fluid receiving tank, and 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 expander 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 utility model is converted into method and the device of electric energy, its advantage is can make full use of " complementary energy " that not easily reclaims of distilling top gaseous phase and having, and be mechanical energy by thermal energy and then change electric energy into, farthest can realize utilization and the recovery of rectifier unit energy.
Accompanying drawing explanation
Fig. 1 distills the device schematic diagram 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. expander 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 utility model and device are further detailed.
The utility model is achieved by the following technical solution:
Distillation tower top complementary energy of the present utility model 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 feedstocks pipeline and the pipeline being connected above equipment; It is characterized in that: overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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 utility model 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) exports liquid (S4) part as reflux liquid (S5) through fractionating tower condensed fluid transfer pump (P1), 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 expander outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and heat-obtaining logistics circulating-pump outlet logistics (S11) gets back to the cold side of phase transformation heat-exchanger (E1).
Technology and equipment of the present utility model can be widely used in the callback course of distilling top gaseous phase complementary energy, in order to the advantage of the utility model in product purity and yield is described better, choose wherein two methods example to be illustrated, but therefore do not limit the Applicable scope of this technology and equipment, accompanying drawing, for illustrating that the utility model is drawn, is not construed as limiting embody rule form of the present utility model.
Embodiment 1
The utility model method is used for the still-process of second alcohol-water separation, as shown in Figure 1, 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 feedstocks pipeline and the pipeline being connected above equipment is comprised; Overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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, the azeotropic mixture that top gaseous phase (S1) is ethanol water, temperature is 78 DEG C, flow is 300kg/h, enter the hot side of phase transformation heat-exchanger (E1), temperature is adopted to be that to take heat away be 73kW for the working medium of 40 DEG C, 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) exports liquid (S4) part as reflux liquid (S5) through fractionating tower condensed fluid transfer pump (P1), 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 expander outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and heat-obtaining logistics circulating-pump outlet logistics (S11) gets back to the cold side of phase transformation heat-exchanger (E1).
Make full use of the complementary energy of the middle low temperature not easily reclaimed that distillation top gaseous phase has, and be mechanical energy by converting heat and then change electric energy into, farthest can realize utilization and the recovery of rectifier unit energy.The final generated energy of this device is 2.9kW.
Embodiment 2
The utility model method is used for the still-process that cyelohexanone is separated with cyclohexanol, as shown in Figure 1, 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 feedstocks pipeline and the pipeline being connected above equipment is comprised; Overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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, top gaseous phase (S1) is the cyelohexanone of 99%, temperature is 123.7 DEG C, flow is 1200kg/h, enter the hot side of phase transformation heat-exchanger (E1), temperature is adopted to be that to take heat away be 159.78kW for the working medium of 60 DEG C, 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) exports liquid (S4) part as reflux liquid (S5) through fractionating tower condensed fluid transfer pump (P1), 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 expander outlet heat-obtaining logistics (S9) after heat-obtaining logistics condenser (E2) enters heat-obtaining logistics recycle pump (P2), and heat-obtaining logistics circulating-pump outlet logistics (S11) gets back to the cold side of phase transformation heat-exchanger (E1).
Make full use of the middle low temperature complementary energy not easily reclaimed that has of distillation top gaseous phase, and be mechanical energy by converting heat and then change electric energy into, farthest can realize utilization and the recovery of rectifier unit energy.The final generated energy of this device is 8.01kW.
The distillation tower top complementary energy that the utility model proposes is converted into method and the device of electric energy, be described by preferred embodiment, person skilled obviously can not depart from the utility model content, spirit and scope equipment and process flow process as herein described is changed or suitably change with combination, realize the utility model technology.Special needs to be pointed out is, all similar replacements and change apparent to those skilled in the art, they are deemed to be included in the utility model spirit, scope and content.
Claims (1)
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 feedstocks pipeline and the pipeline being connected above equipment; It is characterized in that: overhead gaseous phase outlet 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, phase transformation heat-exchanger is cold measures the expander inlet that mouth is connected to drive electrical generators, expander 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420350983.7U CN204024737U (en) | 2014-06-26 | 2014-06-26 | Distillation tower top complementary energy is converted into the device of electric energy |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420350983.7U CN204024737U (en) | 2014-06-26 | 2014-06-26 | Distillation tower top complementary energy is converted into the device of electric energy |
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| Publication Number | Publication Date |
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| CN204024737U true CN204024737U (en) | 2014-12-17 |
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| CN201420350983.7U Expired - Lifetime CN204024737U (en) | 2014-06-26 | 2014-06-26 | Distillation tower top complementary energy is converted into the device of electric energy |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104047650A (en) * | 2014-06-26 | 2014-09-17 | 天津大学 | Method and device for converting surplus energy on distillation tower top into electric energy |
| CN107023990A (en) * | 2017-04-24 | 2017-08-08 | 南通博泰美术图案设计有限公司 | Circulate pumping thermal |
-
2014
- 2014-06-26 CN CN201420350983.7U patent/CN204024737U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104047650A (en) * | 2014-06-26 | 2014-09-17 | 天津大学 | Method and device for converting surplus energy on distillation tower top into electric energy |
| CN107023990A (en) * | 2017-04-24 | 2017-08-08 | 南通博泰美术图案设计有限公司 | Circulate pumping thermal |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20141217 |
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| CX01 | Expiry of patent term |