CN206033614U - Temperature control type ionic liquid separation aromatic hydrocarbon system - Google Patents
Temperature control type ionic liquid separation aromatic hydrocarbon system Download PDFInfo
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- CN206033614U CN206033614U CN201620844725.3U CN201620844725U CN206033614U CN 206033614 U CN206033614 U CN 206033614U CN 201620844725 U CN201620844725 U CN 201620844725U CN 206033614 U CN206033614 U CN 206033614U
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- solvent
- tower
- pipeline
- aromatic hydrocarbon
- extraction
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 32
- 239000002608 ionic liquid Substances 0.000 title claims abstract description 24
- 238000000926 separation method Methods 0.000 title claims abstract description 13
- 239000002904 solvent Substances 0.000 claims abstract description 95
- 238000000605 extraction Methods 0.000 claims abstract description 33
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 239000000654 additive Substances 0.000 claims abstract description 5
- 230000000996 additive effect Effects 0.000 claims abstract description 5
- 230000008929 regeneration Effects 0.000 claims description 43
- 238000011069 regeneration method Methods 0.000 claims description 43
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000000047 product Substances 0.000 claims 2
- 239000013589 supplement Substances 0.000 claims 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 abstract description 25
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000284 extract Substances 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- FCEHBMOGCRZNNI-UHFFFAOYSA-N 1-benzothiophene Chemical compound C1=CC=C2SC=CC2=C1 FCEHBMOGCRZNNI-UHFFFAOYSA-N 0.000 description 14
- 230000006866 deterioration Effects 0.000 description 7
- 230000007797 corrosion Effects 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 238000000354 decomposition reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 150000003457 sulfones Chemical class 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 241000370738 Chlorion Species 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003797 solvolysis reaction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a temperature control type ionic liquid separation aromatic hydrocarbon system, include the extraction column of supplying with pipeline connection with the raw materials, the top of extraction column is equipped with the excess oil and extracts the pipeline, the strip tower is connected to the extraction column, the buffer tank that pipeline connection collected the aromatic hydrocarbon product is passed through at the top of strip tower, parallelly connected first, the second solvent regenerator column that sets up is introduced by the pipeline to the bottom lean solvent in the strip tower, foretell first, second solvent regenerator column all is equipped with several grades of heat exchangers, be equipped with additive replenishing pipe line at top of the tower first, the second solvent regenerator column, it is parallelly connected and through pipeline connection to extracting tower side to the extractant supply line at the bottom of the tower of first solvent regenerator column and second solvent regenerator column. The utility model discloses reduce extraction solvent separation energy consumption, effective recycling sulfolane inferior improves aromatic hydrocarbon product quality and yield, reduce cost.
Description
Technical field
The utility model belongs to ionic liquid aromatics separation technical field, more particularly to a kind of temperature control type ionic liquid
Body aromatics separation system.
Background technology
Aromatic hydrocarbons is the general name of the hydrocarbon containing benzene ring structure.Triphen (BTX in aromatic hydrocarbons：Benzene,toluene,xylene)
It is important basic material in chemical industry.With developing rapidly for organic synthesis industry, aromatic hydrocarbons demand is significantly increased, with stone
Oil becomes the main source of world's aromatic hydrocarbons for the petroleum aromatic that raw material is produced.The raw material of production aromatic hydrocarbons BTX is mainly catalytic reforming
Oil and hydrocracking gasoline, as in raw material, carbon number identical aromatic hydrocarbons is close to non-aromatics boiling point and can form azeotropic mixture, institute
So that light aromatics is isolated from both raw materials mainly using solvent extraction and extractive distillation method.
Aromatics Extractive Project system is one production unit of Aromatic Hydrocarbon United Plant heat release, and solvent extraction aromatics separation is using extraction
Selective dissolution aromatics separation of the agent to aromatic hydrocarbons and non-aromatics, the performance of solvent is to the yield of aromatic hydrocarbons, aromatic hydrocarbon product quality, public
Engineering consumption has very big impact.The basic demand that extractant need to meet is：The selectivity of solubility height, dissolving to aromatic hydrocarbons
High, evaporation latent heat and specific heat capacity it is little, and extraction feed density variation it is big, with good chemical stability and chemical stability.
Adopt sulfolane for extractant arene extracting process, as sulfolane has solubility height, good stability, selection
Property it is high the advantages of, the product purity that can be is high and the rate of recovery is big, high financial profit.
But, there is substantially deficiency in Aromatics Extractive Project system as extractant in sulfolane：Extraction tower operation temperature mistake
Height causes sulfolane to decompose, and generates the water generating acid in sulfur oxide, with system, causes the selectivity of pH value decline solvent big
Width declines so that aromatics seperation efficiency is reduced, and it is that solvent goes bad that high temperature also result in sulfolane to occur polymerization in addition；Apparatus system
In when being mixed with air (vacuum be more than 1.33kPa), sulfolane solvent can occur to aoxidize with air, make solvent that deterioration, pH to occur
Value is decreased obviously；Easily there is chemical reaction with sulfolane in the chlorion in feedstock oil and system water so as to become acid Jie
Matter, and polymer is generated with alkene at high temperature, the pH value of system is declined rapidly.Above-mentioned situation causes sulfolane solvent to make
Deterioration is produced with during, pH value declines so that equipment corrosion, pipeline blockage, product quality decline to a great extent；The sulfolane of decomposition
The energy consumption and maintenance cost of solvent recovery and regenerator is increased, longtime running can cause circulating solvent deterioration serious, affect
It is normal to produce.
The content of the invention
The utility model provides one kind to solve technical problem present in known technology and can reduce extraction solvent point
From energy consumption, inferior sulfolane is effectively reclaimed, improve aromatic hydrocarbon product quality and yield, the temperature control type ionic liquid of reduces cost
Aromatics separation system.
The utility model is adopted the technical scheme that by solving technical problem present in known technology：
A kind of temperature control type ionic liquid aromatics separation system, it is characterised in that：Including being connected with raw material supply pipeline
Extraction tower, the top of extraction tower is laterally provided with extractant supply pipeline, and excess oil extracting pipeline is provided with the top of extraction tower；It is described
The bottom of extraction tower connects the side wall of stripper by pipeline, carries out solvent and separate with aromatic hydrocarbon product in stripper；The vapour
The top of stripper connects the surge tank for collecting aromatic hydrocarbon product by pipeline, and the aromatic hydrocarbon in stripper passes through pipe as rich solvent
Line is delivered in surge tank；The first solvent regeneration tower and second that stripper inner bottom part lean solvent is arranged in parallel by pipeline introducing is molten
Agent regenerator；First solvent regeneration tower and the second solvent regeneration tower are packed tower；Above-mentioned the first solvent regeneration tower and second
Solvent regeneration tower is equipped with several levels heat exchanger；Additive benefit is provided with the tower top of the first solvent regeneration tower and the second solvent regeneration tower
Fill pipeline；The bottom of towe of the first solvent regeneration tower and the second solvent regeneration tower is in parallel and is connected to extraction tower by pipeline and laterally extracts
Agent supply line.
The utility model has the advantages and positive effects that：As the utility model adopts above-mentioned technical proposal, aromatic hydrocarbons
Extracting separating technology is efficient, energy-conservation, low cost, and design compounds sulfolane solvent using benzothiophene kind ionic liquid, and adopts
The solvent regeneration tower of intermittently operated in parallel, can not only meet aromatic hydrocarbons quantity-produced demand, and effectively solve because of ring
Fourth sulfone decomposes the problem that the aromatics seperation efficiency such as the equipment corrosion that deterioration causes are reduced.
Description of the drawings
Fig. 1 is structural representation of the present utility model.
In figure：1st, raw material supply pipeline；2nd, extraction tower；3rd, extractant supply pipeline；4th, excess oil extracting pipeline；5th, strip
Tower；6th, surge tank；7th, the first solvent regeneration tower；8th, the second solvent regeneration tower；9th, heat exchanger；10th, additive makes up line.
Specific embodiment
For the content of the invention of the present utility model, feature and effect can be further appreciated that, following examples are hereby enumerated, and is coordinated
Accompanying drawing describes in detail as follows：
Refer to Fig. 1, a kind of temperature control type ionic liquid aromatics separation system, including being connected with raw material supply pipeline 1
Extraction tower 2, the top of extraction tower is laterally provided with extractant supply pipeline 3, and excess oil extracting pipeline 4 is provided with the top of extraction tower；
The bottom of the extraction tower connects the side wall of stripper 5 by pipeline, carries out solvent and separate with aromatic hydrocarbon product in stripper；Institute
State the top of stripper 5 and connect the surge tank 6 for collecting aromatic hydrocarbon product by pipeline, the aromatic hydrocarbon in the stripper is used as rich solvent
By in pipelined to surge tank；5 inner bottom part lean solvent of stripper is introduced the first solvent regeneration tower 7 being arranged in parallel by pipeline
With the second solvent regeneration tower 8；First solvent regeneration tower 7 and the second solvent regeneration tower 8 are packed tower；The first above-mentioned solvent is again
Raw tower and the second solvent regeneration tower are equipped with several levels heat exchanger 9；In the first solvent regeneration tower and the tower top of the second solvent regeneration tower
It is provided with additive and makes up line 10；The bottom of towe of the first solvent regeneration tower and the second solvent regeneration tower is in parallel and is connected to by pipeline
The lateral extractant supply line of extraction tower 3.
General principle：Raw material enters extraction tower, raw material and the extractant by extraction tower top side entry feed after pretreatment
Liquid-liquid extraction removing non-aromatics is carried out, extraction tower top products obtain non-aromatic hydrocarbon product, extraction tower bottom to raffinate oil Jing after processing
Portion's material is carried out solvent into stripper and is separated with aromatic hydrocarbon product, and aromatic hydrocarbon product is produced from stripper top as rich solvent,
The lean solvent of bottom of towe introduces the first solvent regeneration tower of solvent in parallel or the second solvent regeneration tower by pipeline, and solvent is returned after regeneration
The recycling of extraction tower top-side is flowed, the solvent containing inferior sulfolane in regenerator carries out next after discharging by the road
The process of step.
Concrete grammar, first check for temperature control type ionic liquid aromatics separation system junction with the presence or absence of leakage or
Whether gas leakage, the packed tower in the first solvent regeneration tower and the second solvent regeneration tower are sufficient；Then, into extraction tower, supply is former
Material, while it is extractant in 10 DEG C～85 DEG C to add solid-liquid phase change temperature spot；The extractant is sulfolane and benzo thiophene
The complex solvent of fen class ionic liquid mixing；Sulfolane and benzothiophene kind ionic liquid mass fraction 0.1%～10%；
In one solvent regeneration tower and the second solvent regeneration tower, temperature in tower is reduced by heat exchanger, tower top temperature is 160 DEG C～200 DEG C, often
Level heat exchanger heat-exchange temperature declines 30 DEG C～50 DEG C, and column bottom temperature is down to environment temperature (5～30 DEG C) so that be dissolved with decomposition bad
Change the ionic liquid solidification of sulfolane, and adsorb on the surface of solid packing, fresh sulfolane complex solvent is recycled to extracting
Tower；The alternation of both the first above-mentioned solvent regeneration tower and the second solvent regeneration tower, treats the filler in the first solvent regeneration tower
Adsorption saturation, switches to the second solvent regeneration tower, carries out identical solvent reclamation, and at the same time, the first solvent regeneration tower is by again
Boiling device heating so that the ionic liquid of solidification melts, will be dissolved with the ionic liquid for decomposing deterioration sulfolane from the first solvent again
Raw tower bottom extraction, is further processed to the ionic liquid.
As the ionic liquid for compounding is plucked out of, a certain amount of benzothiophene kind ionic liquid is supplemented in the charging aperture of stripper
Body, the ionic liquid can effectively improve the decomposition degradation temperatures of sulfolane solvent, slow down the speed of solvolysis deterioration, reduce
The generation of acidic materials, the pH value in controllable container are 7 or so, reduce the extent of corrosion of equipment, reduce the investment of equipment
And maintenance cost.
Secondary solvent of the benzothiophene kind ionic liquid as extraction solvent in the utility model, the secondary solvent is to ring fourth
Sulfone has good Compositional type, and double solvents is selective while having highly dissoluble substantially to be increased.Double solvents heat endurance
Strengthen so that the decomposition temperature of sulfolane solvent improves 10%～30%, it is effective in the range of arene extracting process process temperature
The decomposition rate of ageing for reducing sulfolane solvent, extend the service life of solvent.The double solvents effectively can dissolve
Organic compounds containing sulfur in extracting raw material, the pH value for maintaining solvent is 7 or so, efficiently solves the problems, such as equipment corrosion.This reality
It is a kind of temperature control type ionic liquid with the benzothiophene kind ionic liquid in new, in certain temperature range (10 DEG C～
85 DEG C) phase-state change quickly can occur, so as to the aging sulfolane dissolved in more rapidly and effectively separating ionic liquid is molten
Agent and sulfur-containing organic compound.
The first solvent regeneration tower and the second solvent regeneration tower described in the utility model connects intermittently operated side by side, described
Regenerator lower end has the function of reclaiming the sulfolane solvent degraded, and operation temperature is 20～200 DEG C, and operating pressure is absolute
0.05～0.1MPa of pressure.
It is packed tower that regenerator bottom is designed in the utility model, using new arch bridge arc filler, is furnished with reinforcing mass transfer
The liquid re-distributor and packing support plate of heat transfer, and cooling heat exchanger is set.This design using above-mentioned benzothiophene kind from
Sub- liquid aids in extraction solvent, can efficiently separate out the sulfolane solvent of deterioration, improves the service life cycle of extraction solvent,
The quality of extract product is improved, reduces the corrosion impact produced because sulfolane is deteriorated and to equipment, reduced the maintenance of equipment time, prolong
Long service life of equipment.
The above is only, to preferred embodiment of the present utility model, not to make any formal to the utility model
Restriction, it is every according to technical spirit of the present utility model to any simple modification made for any of the above embodiments, equivalent variations with
Modification, belongs in the range of technical solutions of the utility model.
Claims (1)
1. a kind of temperature control type ionic liquid aromatics separation system, it is characterised in that：Including what is be connected with raw material supply pipeline
Extraction tower, the top of extraction tower are laterally provided with extractant supply pipeline, and excess oil extracting pipeline is provided with the top of extraction tower；It is described to take out
The bottom of stripper connects the side wall of stripper by pipeline, carries out solvent and separate with aromatic hydrocarbon product in stripper；The stripping
The top of tower connects the surge tank for collecting aromatic hydrocarbon product by pipeline, and the aromatic hydrocarbon in stripper passes through pipeline as rich solvent
It is delivered in surge tank；Stripper inner bottom part lean solvent is introduced the first solvent regeneration tower and the second solvent being arranged in parallel by pipeline
Regenerator；First solvent regeneration tower and the second solvent regeneration tower are packed tower；The first above-mentioned solvent regeneration tower and second molten
Agent regenerator is equipped with several levels heat exchanger；Additive supplement is provided with the tower top of the first solvent regeneration tower and the second solvent regeneration tower
Pipeline；The bottom of towe of the first solvent regeneration tower and the second solvent regeneration tower is in parallel and is connected to the lateral extractant of extraction tower by pipeline
Supply line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620844725.3U CN206033614U (en) | 2016-08-05 | 2016-08-05 | Temperature control type ionic liquid separation aromatic hydrocarbon system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620844725.3U CN206033614U (en) | 2016-08-05 | 2016-08-05 | Temperature control type ionic liquid separation aromatic hydrocarbon system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206033614U true CN206033614U (en) | 2017-03-22 |
Family
ID=58309131
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620844725.3U Expired - Fee Related CN206033614U (en) | 2016-08-05 | 2016-08-05 | Temperature control type ionic liquid separation aromatic hydrocarbon system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206033614U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110804460A (en) * | 2019-12-18 | 2020-02-18 | 大连福佳·大化石油化工有限公司 | Online deslagging system and process for solvent regeneration tower |
-
2016
- 2016-08-05 CN CN201620844725.3U patent/CN206033614U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110804460A (en) * | 2019-12-18 | 2020-02-18 | 大连福佳·大化石油化工有限公司 | Online deslagging system and process for solvent regeneration tower |
| CN110804460B (en) * | 2019-12-18 | 2023-10-13 | 大连福佳·大化石油化工有限公司 | Online deslagging system and process for solvent regeneration tower |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170322 |