CN1062007C - Process for regenerating aromatic hydrocarbon extraction solvent - Google Patents
Process for regenerating aromatic hydrocarbon extraction solvent Download PDFInfo
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- CN1062007C CN1062007C CN97120270A CN97120270A CN1062007C CN 1062007 C CN1062007 C CN 1062007C CN 97120270 A CN97120270 A CN 97120270A CN 97120270 A CN97120270 A CN 97120270A CN 1062007 C CN1062007 C CN 1062007C
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- 239000002904 solvent Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000000605 extraction Methods 0.000 title claims abstract description 20
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 16
- 230000008569 process Effects 0.000 title description 17
- 230000001172 regenerating effect Effects 0.000 title description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000001914 filtration Methods 0.000 claims abstract description 19
- 238000011069 regeneration method Methods 0.000 claims abstract description 13
- 238000001179 sorption measurement Methods 0.000 claims abstract description 12
- 238000000746 purification Methods 0.000 claims abstract description 3
- 238000004042 decolorization Methods 0.000 claims abstract 2
- UWHCKJMYHZGTIT-UHFFFAOYSA-N Tetraethylene glycol, Natural products OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 7
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 239000003957 anion exchange resin Substances 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 claims description 5
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 claims description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N ethylene glycol Natural products OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 4
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 4
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 2
- -1 glycol ethers Chemical class 0.000 claims description 2
- 239000004576 sand Substances 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- 238000005245 sintering Methods 0.000 claims description 2
- 239000003463 adsorbent Substances 0.000 claims 2
- XALHICXNSREUAV-UHFFFAOYSA-N 2-oxopyrrolidine-1-carbaldehyde Chemical compound O=CN1CCCC1=O XALHICXNSREUAV-UHFFFAOYSA-N 0.000 claims 1
- 239000006004 Quartz sand Substances 0.000 claims 1
- 239000000919 ceramic Substances 0.000 claims 1
- JLFNLZLINWHATN-UHFFFAOYSA-N pentaethylene glycol Chemical compound OCCOCCOCCOCCOCCO JLFNLZLINWHATN-UHFFFAOYSA-N 0.000 claims 1
- 239000010451 perlite Substances 0.000 claims 1
- 235000019362 perlite Nutrition 0.000 claims 1
- 239000011148 porous material Substances 0.000 claims 1
- 125000003011 styrenyl group Chemical class [H]\C(*)=C(/[H])C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 claims 1
- 230000008929 regeneration Effects 0.000 abstract description 9
- 239000002994 raw material Substances 0.000 description 7
- 239000002594 sorbent Substances 0.000 description 7
- 238000009418 renovation Methods 0.000 description 6
- 239000011347 resin Substances 0.000 description 5
- 229920005989 resin Polymers 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000011068 loading method Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000001839 systemic circulation Effects 0.000 description 4
- 210000000689 upper leg Anatomy 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000004087 circulation Effects 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 150000002334 glycols Chemical class 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical group C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000003797 solvolysis reaction Methods 0.000 description 1
- 238000002798 spectrophotometry method Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
一种芳烃抽提溶剂的再生方法，其特点在于向待再生的溶剂中加入溶剂量的50～400%的系统循环水，再通过机械过滤或床层过滤、吸附床层脱色净化处理，再生后的溶剂清亮、透明。A method for regeneration of aromatic hydrocarbon extraction solvent, which is characterized in that system circulating water of 50 to 400% of the solvent amount is added to the solvent to be regenerated, and then through mechanical filtration or bed filtration, decolorization and purification treatment of adsorption bed, after regeneration The solvent is clear and transparent.
Description
The invention belongs to the renovation process of used solvent, more particularly, is a kind of purifying method of relevant aromatic hydrocarbon extraction solvent.
In order to obtain the aromatic hydrocarbons of required purity from oil, petroleum refining industry adopts liquid-liquid method for extracting promptly to utilize hydro carbons difference of solubleness in solvent to reach the purpose of aromatics separation and non-aromatics to cracking hydrogenated gasoline or reformed oil usually.Because solvent is in the medium-term and long-term cycle operation of device, a small amount of solvent inevitably can oxidized generation acidic substance, add the influence of the resistance to acid material monoethanolamine of contained trace amounts of olefin in the extracting raw material and adding, make the color of circulating solvent more and more dark, superpolymer and acidic substance constantly accumulate, gradually influence extraction procedure, when serious even influence the quality of extracting product.Therefore, must regenerate to circulating solvent.
Existing renovation process is to adopt underpressure distillation (Hou Xianglin chief editor, " Chinese oil Refining Technologies ", Sinopec press, P185,1991.12. first version).This method troublesome poeration, solvent loss is big, the energy consumption height, the coking of regenerator column reboiler is remarkable, especially higher solvent such as Tetraglycol 99 to boiling point, its coking and solvolysis problem are more outstanding.U.S. Pat 2878812 once proposed to adopt ion exchange resin that glycol ether and triglycol are carried out absorption regeneration, but the solvent after lacking the work-ing life of this method resin, regenerating still is yellow, and particularly regeneration of resin need be used alkaline solution.Early seventies, U.S. Pat 3595781 has been invented a kind of renovation process of extraction solvent, this method is to treat that the regenerated circulating solvent mixes with raffinating oil, 0.7～100 times the water that adds the regenerated solvent amount, utilize the affinity of solvent and water, make organic impurity, painted thing priority enrichment in raffinating oil, to reach the purpose of purifying solvent.The shortcoming of this method is that the product of raffinating oil can be subjected to a certain degree pollution.Recently, U.S. Pat 4919816 proposes the renovation process of tetramethylene sulfone extraction system recirculated water, and this method can be removed the acidic substance in the recirculated water effectively, reduces the corrosion of equipment, but can't remove the pollutent of solvent systems, outstanding shortcoming still is that regeneration of resin need be used alkaline solution.
The objective of the invention is to overcome the defective of existing reclaiming process, propose a kind of simple to operate, solvent loss is few, the renovation process of the aromatic hydrocarbon extraction solvent of non-environmental-pollution.
Realize the main technical schemes of the object of the invention: in treating the regenerated aromatic hydrocarbon extraction solvent, add systemic circulation water, do decolouring by filtration, adsorption bed and handle.
Specific embodiment of the present invention is followed successively by:
(1) arene extracting process treat in the regenerated solvent add systemic circulation water and thorough mixing, the amount of described recirculated water is to treat 100～400% of regenerated solvent amount, preferably 100～200%;
(2) treated the mixture of regenerated solvent and recirculated water is by mechanical filter or bed filtration, 30～100 ℃ of bed filtration temperature, air speed 0.1～3.0h (1) step
-1, to remove various mechanical impuritys;
(3) by the material after the filtration of (2) step, at 30～100 ℃ of temperature, air speed 0.1～5.0h
-1, handle through the adsorption bed decolorizing purification under 1: 5～1: 20 condition of bed blade diameter length ratio.
The pressure reduction of above-mentioned filtration or adsorption bed surpasses 1. 0kg/cm
2The time, adopt usual method backwash or switching, to remove filter residue.Described mechanical filter method comprises that plate basket filter filters, whizzer filters, by the cylindrical or plate shaped millipore filter filtration that the sintering such as powder of pottery, stainless steel, copper or nickel form, its aperture is 3～30 μ m.The medium that described bed filtration adopts comprises 20～80 purpose quartz sands, sand, pearlstone.
The sorbent material that described adsorption bed adopts comprises: weak base anion-exchange resin, silica gel, gac, preferably adopt the macropore weak basic anion exchange resin or 20～80 purpose granulated active carbons of phenylethylene.
Described solvent comprises glycol ether, triglycol, Tetraglycol 99, five glycol, glycol ethers, tetramethylene sulfone, N-formyl morpholine, N-Methyl pyrrolidone or its mixture.
Further describe technological process of the present invention below in conjunction with accompanying drawing.
Fig. 1 is glycols solvent extraction aromatic hydrocarbons typical process and solvent regeneration process combined process flow synoptic diagram of the present invention.
10,20,22,23,24,25,26,27 be respectively extraction tower, stripping tower among the figure, the water wash column of raffinating oil, stripping water pot, mixing tank, filtration bed, adsorption bed, backflow aromatic hydrocarbons jar.Specific operation process: raw material 1 and solvent 2 enter from the middle part and the top of extraction tower 10 respectively, at the bottom of entering extraction tower from the backwash liquor 3 at stripping tower 20 tops, oil phase is an external phase in extraction tower, solvent phase is a disperse phase, two-phase counter current contact in extraction tower is carried out heat and mass transport, cat head obtains raffinating oil 4, this is raffinated oil and enters water wash column 22 bottoms of raffinating oil, wash with water 17 counter current contact of telling from stripping tower 20 side lines, wash back water 16 and be admitted to backflow aromatic hydrocarbons jar 27, the water 15 that this jar told enters stripping water pot 23, and a part directly is used as water stripping 21, the water 8 that a part needs as solvent reclamation.Rich solvent 5 enters stripping tower 20 tops at the bottom of the extraction tower, cat head steam thing divide after the water outlet sent back to extraction tower as backwash liquor 3 at the bottom of.The mixture 13 of aromatic hydrocarbons and water vapor is extracted out from the side line of stripping tower, obtains BTX aromatics 19 after condensate cooler water outlet in 28 fens, obtains lean solvent 6 at the bottom of the tower.Tell 1～3% lean solvent and treat that promptly regenerated solvent stream strands 7 and water stream 8 from stripping water pot 23 become stream strands 9 behind mixing tank 24 thorough mixing, this stream thigh is at first by filtering bed 25 or mechanical filter, perhaps advance to filter bed 25 again through mechanical filter earlier, the bed top obtains preliminary regenerated solvent 11, further by adsorption bed 26, solvent 12 after obtaining bottom the bed to regenerate, this stream thigh mixes the back with stream thigh 21 and enters 20 ends of stripping tower as water stripping.Stream thigh 18 and 19 is sent device as non-aromatics and aromatic hydrocarbon product respectively.
Processing method of the present invention can also and other aromatic hydrocarbons extracting flow process comprise that glycols extracting five tower flow processs, tetramethylene sulfone extracting flow process unite use.
Advantage of the present invention: the solvent reclamation of present method is the normal temperature and pressure operation, has avoided the pyrolytic decomposition of solvent; Owing to no vacuum operating, alleviated the possibility of air admission system greatly, therefore the solvent protection of total system is of great benefit to; The present invention compares with vacuum distillation method, helps energy-conservationly, and solvent loss is few; Present method need not to use soda acid, and adopts systemic circulation water, therefore helps environment protection.Example 1
Raw material: the lean solvent of reformed oil Tetraglycol 99 extracting aromatic device.
Operation: add the deionized water of 200% (to Tetraglycol 99) in lean solvent, mix the back by the columniform porous filter of powder of stainless steel agglomerating, the strainer blade diameter length ratio is 1: 3, and the maximum diameter of hole is 5 μ m; Circulation speed is 1.0m
3/ m
2.h; Service temperature is 40 ℃.When strainer both sides pressure reduction surpasses 1.0kg/cm
2The time, carry out blowback with 80 ℃ hot water, blowback hot water circulation speed is 2.0m
3/ m
2.h.By 20～60 purpose active carbon beds are housed, the bed blade diameter length ratio is 1: 8 to gained filtrate again, and the operation air speed is 2.0h
-1Temperature is 40 ℃.The total treatment capacity of lean solvent is 900 times of sorbent material loading amount.The relevant table 1 that the results are shown in.Example 2
This example is the Comparative Examples of example 1.
Raw material: with example 1.
Operation: adding system recirculated water not in lean solvent, the trade mark that adsorption medium adopts Chemical Plant of Nankai Univ. to produce is the D290 macroporous anion exchange resin, and the total treatment capacity of lean solvent only is 200 times of sorbent material loading amount, and other the results are shown in Table 1 with example 1.
By table 1 data as can be known, adopt technology of the present invention, the treatment capacity of sorbent material is more much higher than the technology that does not add water, and treatment effect also clearly.Example 3
Raw material: with example 1.
Operation: the systemic circulation water of adding 350% in lean solvent, filter and adopt the bed that 20～60 order sands are housed, the bed blade diameter length ratio is 1: 10; The operation air speed is 0.3h
-1, temperature is 80 ℃, other the results are shown in table 1 with example 1.Example 4
Raw material: reformed oil triglycol extraction plant lean solvent
Operation: the trade mark that adsorption medium adopts Chemical Plant of Nankai Univ. to produce is the D290 macroporous anion exchange resin, and the bed blade diameter length ratio is 1: 15, and the operation air speed is 1.0h
-1, the total treatment capacity of lean solvent is 500 times of sorbent material loading amount, other the results are shown in table 1 with example 3.Example 5
Raw material: reformed oil tetramethylene sulfone aromatic extraction unit lean solvent
Operation: add the deionized water of 100% (to the amount of tetramethylene sulfone) in sulfolane solvent, service temperature is 70 ℃, and other is with example 1, and the total treatment capacity of solvent is 850 times of sorbent material loading amount, and the solvent quality index is listed in table 1 before and after the regeneration.Table 1 example 1～5 main operational condition and result
*Spectrophotometric determination, absorbing wavelength 420nm (as follows).
| Project | Operational condition | Result | Treatment capacity (doubly) | ||||||||||||||
| Solvent | Quantity of circulating water % | Filter | Absorption | Before the regeneration | After the regeneration | ||||||||||||
| Medium | Temperature ℃ | Air speed h -1 | Blade diameter length ratio | Sorbent material | Temperature ℃ | Air speed h -1 | Blade diameter length ratio | Outward appearance | Colourity * | The pH value | Outward appearance | Colourity * | The pH value | ||||
| Example 1 example 2 examples 3 examples 4 examples 5 | Tetraglycol 99 Tetraglycol 99 Tetraglycol 99 triglycol tetramethylene sulfone | 200 0 350 200 100 | Mechanical sand sand machinery | 40 40 80 40 70 | 1 1 0.3 1 1 | 1∶3 1∶3 1∶10 1∶8 1∶3 | Gac resin gac resin gac | 40 40 80 40 70 | 2 2 3 2 2 | 1∶8 1∶8 1∶10 1∶15 1∶8 | The muddy dark brown of the muddy dark brown dark brown of muddy dark brown dark brown | 640 640 640 320 850 | 5.8 5.8 5.8 6.5 5.0 | Limpid transparent clear transparent clear is limpid transparent | 40 60 30 65 32 | 7.1 9.0 7.8 8.8 7.5 | 900 200 800 500 850 |
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97120270A CN1062007C (en) | 1997-11-11 | 1997-11-11 | Process for regenerating aromatic hydrocarbon extraction solvent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97120270A CN1062007C (en) | 1997-11-11 | 1997-11-11 | Process for regenerating aromatic hydrocarbon extraction solvent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1217367A CN1217367A (en) | 1999-05-26 |
| CN1062007C true CN1062007C (en) | 2001-02-14 |
Family
ID=5175856
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97120270A Expired - Lifetime CN1062007C (en) | 1997-11-11 | 1997-11-11 | Process for regenerating aromatic hydrocarbon extraction solvent |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1062007C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003512145A (en) * | 1999-10-15 | 2003-04-02 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Treatment of extraction solvents to remove acidic contaminants |
| CN101172927B (en) * | 2006-10-31 | 2010-06-30 | 北京金伟晖工程技术有限公司 | Improved raffinate processing system and method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB0107908D0 (en) * | 2001-03-29 | 2001-05-23 | Bp Oil Int | Decolourisation method |
| EP1650287B1 (en) * | 2003-07-04 | 2012-03-28 | Beijing Grand Golden-Bright Engineering & Technologies Co. Ltd. | A method for recombining catalytic hydrocarbons |
| CN100378197C (en) * | 2003-11-07 | 2008-04-02 | 丁冉峰 | Catalytic hydrocarbon recombinant treating method |
| CN100377758C (en) * | 2003-10-24 | 2008-04-02 | 北京金伟晖工程技术有限公司 | Water soluble solvent vegenerating system and method |
| CN102659758A (en) * | 2012-06-01 | 2012-09-12 | 唐山中润煤化工有限公司 | Regeneration and purification method of sulfolane in crude benzene hydrofining |
| CN102731472B (en) * | 2012-06-28 | 2015-01-07 | 中国石油化工股份有限公司 | Apparatus for reducing arene extraction solvent sulfolane, and application thereof |
| CN106957297A (en) * | 2016-12-31 | 2017-07-18 | 光华（营口）化工技术服务有限公司 | A kind of regeneration method of inferior sulfolane solvent |
| CN108929187A (en) * | 2017-05-27 | 2018-12-04 | 中国石油化工股份有限公司 | A method of the separation of extractive distillation target product from hydrocarbon mixture |
| CN110604967A (en) * | 2019-10-15 | 2019-12-24 | 北京宝晨能源工程技术有限公司 | Sulfolane regeneration device and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3492222A (en) * | 1967-11-14 | 1970-01-27 | Universal Oil Prod Co | Solvent recovery process |
| US3595781A (en) * | 1967-12-06 | 1971-07-27 | Inst Francais Du Petrole | Solvent extraction of aromatic hydrocarbons |
| JPS62246992A (en) * | 1986-04-18 | 1987-10-28 | Mitsubishi Petrochem Co Ltd | Solvent recovering process |
| US5008004A (en) * | 1988-10-03 | 1991-04-16 | Uop | Aromatics extraction process having improved water stripper |
| CN1059851A (en) * | 1991-11-08 | 1992-04-01 | 中国石油化工总公司 | Solvent recovery methods in hydrocarbon processing |
-
1997
- 1997-11-11 CN CN97120270A patent/CN1062007C/en not_active Expired - Lifetime
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3492222A (en) * | 1967-11-14 | 1970-01-27 | Universal Oil Prod Co | Solvent recovery process |
| US3595781A (en) * | 1967-12-06 | 1971-07-27 | Inst Francais Du Petrole | Solvent extraction of aromatic hydrocarbons |
| JPS62246992A (en) * | 1986-04-18 | 1987-10-28 | Mitsubishi Petrochem Co Ltd | Solvent recovering process |
| US5008004A (en) * | 1988-10-03 | 1991-04-16 | Uop | Aromatics extraction process having improved water stripper |
| CN1059851A (en) * | 1991-11-08 | 1992-04-01 | 中国石油化工总公司 | Solvent recovery methods in hydrocarbon processing |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003512145A (en) * | 1999-10-15 | 2003-04-02 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Treatment of extraction solvents to remove acidic contaminants |
| JP4892150B2 (en) * | 1999-10-15 | 2012-03-07 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Treatment of extraction solvents to remove acidic contaminants |
| CN101172927B (en) * | 2006-10-31 | 2010-06-30 | 北京金伟晖工程技术有限公司 | Improved raffinate processing system and method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1217367A (en) | 1999-05-26 |
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