CN204447370U - The device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane - Google Patents
The device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane Download PDFInfo
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- CN204447370U CN204447370U CN201520046945.7U CN201520046945U CN204447370U CN 204447370 U CN204447370 U CN 204447370U CN 201520046945 U CN201520046945 U CN 201520046945U CN 204447370 U CN204447370 U CN 204447370U
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 100
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 60
- 239000001294 propane Substances 0.000 title claims abstract description 50
- 238000000926 separation method Methods 0.000 title claims abstract description 20
- 238000007701 flash-distillation Methods 0.000 title claims abstract description 14
- 238000000895 extractive distillation Methods 0.000 claims abstract description 94
- 239000000463 material Substances 0.000 claims abstract description 27
- 230000008676 import Effects 0.000 claims abstract description 14
- 238000012856 packing Methods 0.000 claims description 10
- 239000000945 filler Substances 0.000 claims description 4
- 238000000605 extraction Methods 0.000 abstract description 29
- 238000000034 method Methods 0.000 abstract description 22
- 238000005265 energy consumption Methods 0.000 abstract description 11
- 239000000203 mixture Substances 0.000 abstract description 10
- 238000001816 cooling Methods 0.000 abstract description 8
- 230000006837 decompression Effects 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 7
- 238000004821 distillation Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical group CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 30
- 238000010992 reflux Methods 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 9
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 9
- 238000011084 recovery Methods 0.000 description 9
- 239000007791 liquid phase Substances 0.000 description 8
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000012267 brine Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 5
- 239000000470 constituent Substances 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000012808 vapor phase Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- JTXAHXNXKFGXIT-UHFFFAOYSA-N propane;prop-1-ene Chemical group CCC.CC=C JTXAHXNXKFGXIT-UHFFFAOYSA-N 0.000 description 3
- 238000005336 cracking Methods 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- CYNYIHKIEHGYOZ-UHFFFAOYSA-N 1-bromopropane Chemical compound CCCBr CYNYIHKIEHGYOZ-UHFFFAOYSA-N 0.000 description 1
- RYPKRALMXUUNKS-UHFFFAOYSA-N 2-Hexene Natural products CCCC=CC RYPKRALMXUUNKS-UHFFFAOYSA-N 0.000 description 1
- PBCJIPOGFJYBJE-UHFFFAOYSA-N acetonitrile;hydrate Chemical compound O.CC#N PBCJIPOGFJYBJE-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses the device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane, the device of separation of propylene and propane, comprise extractive distillation column and flash column, described extractive distillation column top is provided with extractant import, bottom is provided with extractive distillation column material inlet, the tower top of described extractive distillation column is provided with extractive distillation column first and exports, be provided with extractive distillation column second at the bottom of tower to export, the top of described flash column is provided with flash column material inlet, the top of described flash column is provided with flash column first and exports, bottom is provided with flash column second and exports, the extractive distillation column second of described extractive distillation column exports the flash column material inlet connecting flash column, be provided with flash column second bottom described flash column and export the extractant import connecting extractive distillation column top, the utility model is by after adopting extraction and distillation technology to isolate propane to propylene and propane, mixture extractive distillation column tower reactor being contained extractant and propylene carries out decompression cooling flash distillation, reduce the energy consumption in production operation process.
Description
Technical field
The utility model relates to the device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane, and specifically, what relate to is propylene and propane extracting rectifying device and the series connection of propylene refining device, and separating-purifying propylene and propane, belong to technical field of petrochemical industry.
Background technology
Propylene is as important industrial chemicals, and demand constantly increases, and it is mainly derived from steam cracking and oil plant catalytic cracking, still has small part propylene to derive from dehydrogenating propane, olefin(e) disproportionation and methanol conversion.The propylene mixtures that these cracking and cracking obtain all needs to carry out rectification flow, and the core in process for refining is: the separation of propane propylene.
The separation of olefin/paraffin is one of most important process in petroleum chemical industry always, and industrial traditional separating technology equipment needed thereby investment is large, energy consumption is high.Because the boiling point of propylene and propane is close (differing 5 DEG C), between component, relative volatility is less, when adopting conventional distil-lation method, the tower height of design needs to reach 90m, and theoretical cam curve needs more than 200 pieces, and reflux ratio is greater than 10, also to pressurize or low-temperature operation, so energy consumption is very high.During employing high-pressure process, tower top temperature is higher than 45 DEG C, can carry out condensation by direct cooling water, but the number of plates that high-pressure process is separated needs is many, and reflux ratio is very large.Adopt low-pressure process, propylene propane relative volatility increases, and can reduce reflux ratio and number of theoretical plate, but tower top temperature is too low, condensed water can not be adopted directly to carry out condensation, need adopt other condensing agent, will increase investment and energy consumption so undoubtedly.Therefore, the isolation technics of high-efficiency and economic that needs a large amount of alkene is reclaimed and is effectively utilized.
Extraction and distillation technology is adopted rectifying and extraction to be coupled, utilize extractant and propane, propylene in the counter-current flow of extractive distillation column, in tower on High Efficient Standard Packing, the selective absorbing propylene of extractant, realize propane to be separated with the efficient of propylene, reduce number of theoretical plate and the reflux ratio of extractant recovery tower, energy consumption can also be reduced to a great extent, obtain the propylene that purity is higher.
Although extraction and distillation technology to a certain extent comparatively conventional rectification method separating-purifying propylene and propane can reduce energy consumption, at extractant exhausting section, still have employed the method for compression rectification, thus the energy consumption of whole technique is still higher.
Utility model content
Utility model object: the purpose of this utility model is in existing separation of propylene and propane technology, the defect that the energy consumption of whole technique is higher, the device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane is provided, after adopting extraction and distillation technology to isolate propane to propylene and propane, mixture extractive distillation column tower reactor being contained extractant and propylene carries out decompression cooling flash distillation, reduces the energy consumption in production operation process.
Technical scheme: the device of a kind of extracting rectifying described in the utility model and flash distillation integrated separation propylene and propane, comprise extractive distillation column and flash column, described extractive distillation column top is provided with extractant import, bottom is provided with extractive distillation column material inlet, the tower top of described extractive distillation column is provided with extractive distillation column first and exports, be provided with extractive distillation column second at the bottom of tower to export, the top of described flash column is provided with flash column material inlet, the top of described flash column is provided with flash column first and exports, bottom is provided with flash column second and exports, the extractive distillation column second of described extractive distillation column exports the flash column material inlet connecting flash column, be provided with flash column second bottom described flash column and export the extractant import connecting extractive distillation column top.
As preferably: described extractive distillation column is packed tower, and the filler in described packed tower is High Efficient Standard Packing.
Adopt the device of above-mentioned extracting rectifying and flash distillation integrated separation propylene and propane to carry out the method for separation of propylene and propane, comprise the steps:
1.1, propane and propylene mixtures and extractant are delivered in extractive distillation column from the extractant import of extractive distillation column, extractive distillation column material inlet respectively, after separation of extractive distillation, the extractive distillation column first of extracting rectifying column overhead exports extraction propane, and the extractive distillation column at the bottom of extractive distillation column tower second exports extraction extractant and propylene mixtures;
1.2, the propylene obtained in step 1.1 and the mixture of extractant enter in flash column by the flash column material inlet on flash column top, after carrying out flash separation, the flash column first at flash column top exports extraction propylene, and the flash column bottom flash column second exports extraction extractant;
1.3, the extractant exporting extraction by the flash column bottom flash column second in step 1.2 enters in extractive distillation column by the extractant import on extractive distillation column top, recycles.
Improve technique scheme further: described extractant is dimethyl formamide (DMF), 1-METHYLPYRROLIDONE (NMP), oxolane (THF), furfural or water content be 5 ~ 40% containing water-acetonitrile (ACN).
The operating pressure of described extractive distillation column is 1.2 ~ 2.4 MPa, and theoretical cam curve is 30 ~ 100, and reflux ratio is 0.1 ~ 20.
The relative volatility of propane and propylene is close to 1, and traditional rectifying column requires that theoretical cam curve is more than 200 pieces.The utility model forms ternary system after adding extractant, increases the relative volatility of propane and propylene, decreases the theoretical cam curve of rectifying column; Adopt pressurized operation simultaneously, improve tower top temperature, avoid tower top to need to cool with cryogenic system; Keep suitable reflux ratio, what be conducive to improving propylene and propane is separated production capacity simultaneously.
As preferably: the operating pressure of described extractive distillation column is 0.2 ~ 1.0MPa, and theoretical cam curve is 60 ~ 80, and reflux ratio is 1 ~ 5.
Described flash column operating pressure is 0.01 ~ 1.0 MPa, and flash temperature is-10 ~ 50 DEG C.
Flash column equipment is simple, and without the need to loading filler in tower, save cost, flash process under low pressure completes simultaneously, and lower to equipment requirement, flash temperature can be met by brine ice.
As preferably: described flash column operating pressure is 0.2 ~ 1.0MPa, and flash temperature is 10 ~ 30 DEG C.
Compared with prior art, its beneficial effect is the utility model:
1, the utility model equipment is simple, small investment, good separating effect, extractant recycle non-secondary pollution, operating cost is low, and obtain highly purified propane and propylene after treatment, have good social benefit, achieve the efficient separation of propane propylene.
2, in the utility model, the theoretical cam curve of extractive distillation column is 30-100, and reflux ratio is 0.1-20, operating pressure is 0.2 ~ 1.0MPa, and tower top directly adopts water quench, without the need to adopting refrigerant special, and reboiler heat duty reduces, overall energy consumption reduces by more than 10%.
Accompanying drawing explanation
Fig. 1 is the structural representation of device described in embodiment 1.
Number in the figure is: 1-extractant feed pipeline, 2-propylene and propane mixture feeding line, 3-extractive distillation column, 4-High Efficient Standard Packing, 5-extractive distillation column overhead vapor phase pipeline, 6-extractive distillation column overhead condenser, 7-extractive distillation column overhead reflux pipeline, 8-bromopropane product discharging pipeline, 9-extractive distillation column tower reactor reboiler liquid phase circulation pipeline, 10-extractive distillation column tower reactor reboiler, 11-extractive distillation column tower reactor reboiler vapour phase pipeloop, 12-extractive distillation column tower reactor liquid phase extraction pipeline, 13-pressure-reducing valve, 14-flash column feeding line, 15-flash column, 16-flash column overhead vapor phase pipeline, 17-flash column tower reactor liquid phase pipeline, 18-blender feed pump, 19-blender feeding line, the fresh extractant feed pipeline of 20-, 21-extractant blender.
Detailed description of the invention
Below in conjunction with accompanying drawing, technical solutions of the utility model are described in detail, but protection domain of the present utility model is not limited to described embodiment.
embodiment 1:as shown in Figure 1, the device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane, comprises extractive distillation column 3 and flash column 15, and described extractive distillation column 3 is packed tower, and the filler in described packed tower is High Efficient Standard Packing 4.
Described extractive distillation column 3 top is provided with extractant import, bottom is provided with extractive distillation column material inlet, and described extractant import connects extractant feed pipeline 1, and described extractive distillation column material inlet connects propylene and propane mixture feeding line 2.
Described extracting rectifying column overhead is connected with extractive distillation column overhead condenser 6 by extractive distillation column overhead vapor phase pipeline 5, and the discharging opening of described extractive distillation column overhead condenser 6 is connected to extractive distillation column overhead reflux pipeline 7, bromopropane product discharging pipeline 8.
Be connected with extractive distillation column tower reactor reboiler 10 by extractive distillation column tower reactor reboiler liquid phase circulation pipeline 9 at the bottom of the tower of described extractive distillation column 3, described extractive distillation column tower reactor reboiler 10 top is connected with extractive distillation column 3 by extractive distillation column tower reactor reboiler vapour phase pipeloop 11, and described extractive distillation column tower reactor reboiler 10 bottom is connected with extractive distillation column tower reactor liquid phase extraction pipeline 12.
The top of described flash column 15 is provided with flash column material inlet, and described flash column material inlet is connected with flash column feeding line 14, and described extractive distillation column tower reactor liquid phase extraction pipeline 12 is connected with flash column feeding line 14 by pressure-reducing valve 13.
Described flash column 15 top is provided with flash column first and exports, described flash column first is connected with flash column overhead vapor phase pipeline 16 on exporting, be provided with flash column second bottom flash column to export, flash column second is connected with flash column tower reactor liquid phase pipeline 17 on exporting, flash column tower reactor liquid phase pipeline 17 is connected 19 by blender feed pump 18 with blender feeding line, blender feeding line 19 is connected with extractant blender 21, extractant blender 21 is also connected with fresh extractant feed pipeline 20, the discharging opening of extractant blender 21 is connected with extractant feed pipeline 1.
The present embodiment, be the catalytically cracked material gas (de-frivolous heavy constituent) of certain refinery, be characterized as propane 30%, propylene is 70%(mass fraction), extractant is dimethyl formamide (DMF).Extractive distillation column 3 in the present embodiment loads High Efficient Standard Packing 4, number of theoretical plate 76 pieces, reflux ratio 14, operating pressure 1.8MPa, and the mass ratio of extractant and raw material is 4.0; Operating pressure 0.08 MPa of flash column, temperature 30 DEG C.
Catalytically cracked material gas is entered from extractive distillation column material inlet with the speed of 1500kg/h, extractant is dimethyl formamide (DMF), add from the import of extractive distillation column 3 extractant with the speed of 6000kg/h, extractant feed is the 4th block of plate, propane and propylene feed position are the 60th piece of theoretical plate, extractive distillation column 3 overhead extraction mass fraction is the propane of 97%, the extractant being rich in propylene then enters flash column 15, through decompression cooling, light component propylene with the purity of mass fraction 98.5% from the extraction of flash column top, the mass fraction of extraction bottom flash column is be extractant feed after mixing with fresh extractant after the extractant of 98.5%.In extractive distillation column 3, the rate of recovery of propane is 98.8%, and the propylene recovery rate of flash column extraction is 95.2%.In this technical process, extractive distillation column bottom temperature 148.25 DEG C, the thermic load of required reboiler is 1093.56 kW, extracting rectifying column overhead temperatures 51.68 DEG C, and thermic load needed for condenser is-510.46 kW; Flash column in cooling decompression process, chilling temperature 30 DEG C, required condensed water heat exchange load-455.98 kW.Therefore the total heat duties of reboiler is 1093.56 kW, required heating steam is low-pressure steam; Condenser total heat duties-966.44 kW, required condensed water is normal temperature condensation water or brine ice.
embodiment 2:the device of the extracting rectifying adopted in the present embodiment and flash distillation integrated separation propane and propylene, identical with embodiment 1.
The present embodiment, be the catalytically cracked material gas (de-frivolous heavy constituent) of certain refinery, be characterized as propane 20%, propylene is 80%(mass fraction), extractant is 1-METHYLPYRROLIDONE (NMP).Extractive distillation column 3 in the present embodiment loads High Efficient Standard Packing 4, number of theoretical plate 82 pieces, reflux ratio 5.5, operating pressure 1.8 MPa, and the mass ratio of extractant and raw material is 8.0; Operating pressure 0.02 MPa of flash column, temperature 30 DEG C.
Catalytically cracked material gas is entered from extractive distillation column material inlet with the speed of 1500kg/h, extractant is 1-METHYLPYRROLIDONE (NMP), mixed extractant adds from the import of extractive distillation column 3 extractant with the speed of 12000kg/h, extractant feed is the 6th block of plate, propane and propylene feed position are the 40th piece of theoretical plate, extractive distillation column 3 overhead extraction mass fraction is the propane of 96.9%, the extractant being rich in propylene then enters flash column 15, through decompression cooling, light component propylene with the purity of mass fraction 98.8% from the extraction of flash column top, the mass fraction of extraction bottom flash column is mix extractant feed the most with fresh extractant after the extractant of 99.5%.In extractive distillation column 3, the rate of recovery of propane is 99.0%, and the propylene recovery rate of flash column extraction is 96.4%.In this technical process, extractive distillation column bottom temperature 283.39 DEG C, the thermic load of required reboiler is 2197.01 kW, extracting rectifying column overhead temperatures 51.66 DEG C, and thermic load needed for condenser is-234.35 kW; Flash column in cooling decompression process, chilling temperature 30 DEG C, required condensed water heat exchange load-1827.80 kW.Therefore the total heat duties of reboiler is 2197.01 kW, required heating steam is low-pressure steam; Condenser total heat duties-2062.15 kW, required condensed water is normal temperature condensation water or brine ice.
embodiment 3:the device of the extracting rectifying adopted in the present embodiment and flash distillation integrated separation propane and propylene, identical with embodiment 1.
The present embodiment, be the catalytically cracked material gas (de-frivolous heavy constituent) of certain refinery, be characterized as propane 25%, propylene is 75%(mass fraction), extractant is oxolane (THF).Extractive distillation column 3 in the present embodiment loads High Efficient Standard Packing 4, number of theoretical plate 90 pieces, reflux ratio 1.72, operating pressure 1.8 MPa, and the mass ratio of extractant and raw material is 9.0; Operating pressure 0.015 MPa of flash column, temperature 30 DEG C.
Catalytically cracked material gas is entered from extractive distillation column material inlet with the speed of 1500 kg/h, extractant is oxolane (THF), mixed extractant adds from the import of extractive distillation column 3 extractant with the speed of 13500 kg/h, extractant feed is the 4th block of plate, propane and propylene feed position are the 45th piece of theoretical plate, extractive distillation column 3 overhead extraction mass fraction is the propane of 97.2%, the extractant being rich in propylene then enters flash column 15, through decompression cooling, light component propylene with the purity of mass fraction 98.7% from the extraction of flash column top, the mass fraction of extraction bottom flash column is mix extractant feed the most with fresh extractant after the extractant of 99.7%.In extractive distillation column 3, the rate of recovery of propane is 99.4%, and the propylene recovery rate of flash column extraction is 96.0%.In this technical process, extractive distillation column bottom temperature 294.69 DEG C, the thermic load of required reboiler is 2400.46 kW, extracting rectifying column overhead temperatures 51.72 DEG C, and thermic load needed for condenser is-97.82 kW; Flash column in cooling decompression process, chilling temperature 30 DEG C, required condensed water heat exchange load-2163.93 kW.Therefore the total heat duties of reboiler is 2400.46 kW, required heating steam is low-pressure steam; Condenser total heat duties-2261.75 kW, required condensed water is normal temperature condensation water or brine ice.
comparative example:
The catalytically cracked material gas (de-frivolous heavy constituent) of certain refinery, be characterized as propane 30%, propylene is 70%, and extractant is dimethyl formamide (DMF).Extractive distillation column 3 in the present embodiment loads High Efficient Standard Packing 4, number of theoretical plate 76 pieces, reflux ratio 14, operating pressure 1.8 MPa, and the mass ratio of extractant and raw material is 4.0; Extractant reclaims rectifying column inside installing High Efficient Standard Packing 4, number of theoretical plate 30 pieces, reflux ratio 0.9, operating pressure 1.6 MPa.
Catalytically cracked material gas is entered from extractive distillation column material inlet with the speed of 1500kg/h, extractant is dimethyl formamide (DMF), mixed extractant adds from the import of extractive distillation column 3 extractant with the speed of 6000kg/h, extractant feed is the 4th block of plate, propane and propylene feed position are the 60th piece of theoretical plate, extractive distillation column 3 overhead extraction mass fraction is the propane of 97%, the extractant being rich in propylene then enters extractant and reclaims rectifying column, feed entrance point is the 8th block of plate, it is the propylene of 98.5% that extractant reclaims rectifying tower top extraction mass fraction, extractant mixes extractant feed the most with fresh extractant after reclaiming the extractant of the cleaning of extraction at the bottom of rectifying column.In extractive distillation column 3, the rate of recovery of propane is 98.8%, and the propylene recovery rate that extractant reclaims rectifying column overhead extraction is 98.6%.In this technical process, extractive distillation column bottom temperature 148.25 DEG C, the thermic load of required reboiler is 1093.56 kW, extracting rectifying column overhead temperatures 51.68 DEG C, and required condenser heat load is-510.46 kW; Extractant reclaims tower bottom of rectifying tower temperature 294.36 DEG C, and the thermic load of required reboiler is 755.03 kW, and extractant reclaims rectifying column tower top temperature 38.30 DEG C, and required condenser heat load is-169.15 kW.Therefore the total heat duties of reboiler is 1848.59kW, required heating steam is low-pressure steam (1093.56 kW) and high steam (755.03 kW); Condenser total heat duties-679.61 kW, required condensed water is normal temperature condensation water or brine ice.
Embodiment 1 and comparative example are compared, in embodiment 1, reboiler heat duty reduces by 40.84%, and condenser heat load increases 29.7%, and overall energy consumption reduces by more than 10%.And needed for the reboiler increased in comparative example, heating steam is high steam, further increases cost.
As mentioned above, although represented with reference to specific preferred embodiment and described the utility model, it shall not be construed as the restriction to the utility model self.Under the spirit and scope prerequisite of the present utility model not departing from claims definition, various change can be made in the form and details to it.
Claims (2)
1. the device of an extracting rectifying and flash distillation integrated separation propylene and propane, it is characterized in that: comprise extractive distillation column and flash column, described extractive distillation column top is provided with extractant import, bottom is provided with extractive distillation column material inlet, the tower top of described extractive distillation column is provided with extractive distillation column first and exports, be provided with extractive distillation column second at the bottom of tower to export, the top of described flash column is provided with flash column material inlet, the top of described flash column is provided with flash column first and exports, bottom is provided with flash column second and exports, the extractive distillation column second of described extractive distillation column exports the flash column material inlet connecting flash column, be provided with flash column second bottom described flash column and export the extractant import connecting extractive distillation column top.
2. the device of a kind of extracting rectifying according to claim 1 and flash distillation integrated separation propylene and propane, is characterized in that: described extractive distillation column is packed tower, and the filler in described packed tower is High Efficient Standard Packing.
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| CN201520046945.7U CN204447370U (en) | 2015-01-22 | 2015-01-22 | The device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane |
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| CN201520046945.7U CN204447370U (en) | 2015-01-22 | 2015-01-22 | The device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104606911A (en) * | 2015-01-22 | 2015-05-13 | 中建安装工程有限公司 | Device and method for coupled separation of propylene and propane by extractive distillation and flash evaporation |
| CN107029447A (en) * | 2017-05-27 | 2017-08-11 | 江苏华洋尼龙有限公司 | A kind of nylon chips extraction equipment and production line |
| WO2019019034A1 (en) * | 2017-07-26 | 2019-01-31 | 深圳市宏事达能源科技有限公司 | Gas fractionation device |
-
2015
- 2015-01-22 CN CN201520046945.7U patent/CN204447370U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104606911A (en) * | 2015-01-22 | 2015-05-13 | 中建安装工程有限公司 | Device and method for coupled separation of propylene and propane by extractive distillation and flash evaporation |
| CN107029447A (en) * | 2017-05-27 | 2017-08-11 | 江苏华洋尼龙有限公司 | A kind of nylon chips extraction equipment and production line |
| WO2019019034A1 (en) * | 2017-07-26 | 2019-01-31 | 深圳市宏事达能源科技有限公司 | Gas fractionation device |
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