US3451925A - Solvent extraction of hydrocarbons with n-methyl-2-pyrrolidone - Google Patents
Solvent extraction of hydrocarbons with n-methyl-2-pyrrolidone Download PDFInfo
- Publication number
- US3451925A US3451925A US624970A US3451925DA US3451925A US 3451925 A US3451925 A US 3451925A US 624970 A US624970 A US 624970A US 3451925D A US3451925D A US 3451925DA US 3451925 A US3451925 A US 3451925A
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- US
- United States
- Prior art keywords
- solvent
- water
- nmp
- extract
- phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
Definitions
- This invention relates to the solvent extraction of hydrocarbon mixtures using N-methyl-Z-pyrrolidone as selective solvent, referred to hereinafter for brevity as NMP.
- NMP N-methyl-Z-pyrrolidone
- the various feed stocks and fractions treated are usually produced in contact with steam or water vapor and are stored in contact with liquid water so that they normally contain dissolved water and Aoccasionally small amounts of entrained water.
- solvent rening such wet stocks with a solvent such as NMP the dissolved yand entrained water is taken up by the solvent thereby reducing its solvent power and effectiveness for solvent refining.
- NMP is also hydroscopic so that it tends to take up water from the surrounding atmosphere in storage and handling. Water, however, has a marked effect upon the solvent power of NMP substantially reducing its ability to dissolve hydrocarbons.
- This invention relates to the solvent extraction of hydrocarbon mixtures with a primary solvent comprising NMP containing not more than 1 volume percent water. Separation of NMP from the resulting rainate phase and extract phase is effected by re-extraction with a secondary solvent and then NMP containing less than 1.0 weight percent water is separated from the secondary solvent.
- Suitable :secondary solvents are materials which exhibit selective solvency for at least one constituent of the raffnate or extract phase.
- Preferred solvents are, for example, water which selectively dissolves NMP from the extract phase, raffinate phase or both, hydrocarbons of dissimilar boiling range which may be used to selectively dissolve the hydrocarbons extract product from the extract phase. Hydrocarbon solvents having a boiling point at least 50 F. below that of NMP and the hydrocarbon mixture treated are preferred to facilitate their separation from the NMP and extract product by distillation.
- a hydrocarbon mixture to be separated into fractions comprising a rainate product of reduced aromaticity and an extract product of increased aromaticity is contacted in -a liquid-liquid extraction zone with a solvent comprising NMP and not more than 1.0 volume percent water.
- a raiinate phase comprising said ralinate product with a minor portion of NMP dissolved therein and an extract phase comprising said NMP with said extract product dissolved therein are separated.
- Solvent is advantageously separated from the rainate product by liquid-liquid extraction of the rallinate phase with water.
- the resulting solution ⁇ of NMP in water is separated by distillation.
- Extract product is separated from said extract phase by liquid-liquid extraction with another solvent which is a selective solvent for at least one constituent of said extract phase.
- the other solvent may be Water or -a hydrocarbon mixture of dissimilar boiling range from the hydrocarbon mixture feed stock and boiling at least 50 F. above or below the NMP solvent.
- the resulting solution of NMP in water may be combined with the washings from the reextraction of the rainate phase for separation of the water and NMP.
- the water s separated as distillate and may Ibe reused for additional washing of raffinate phase or extract phase.
- distillation is effected removing the solvent hydrocarbon as distillate from extract product bottoms.
- the hydrocarbon solvent distillate likewise may be reused in liquid-liquid extraction of the extract phase.
- An object of the present invention is to provide a recovery system simpler in design and operation than those of the prior art.
- the complete miscibility of NMP with water and the significant reduction of the solvent power of NMP for oil in the presence of small amounts of water may be used to advantage.
- Most solvents are only partially miscible with water with the result that only limited separation of the solvent from oil can be effected unless large quantities of Water are used.
- water or another secondary solvent lower boiling that NMP for the separation of NMP from extract or raffinate phases it is only necessary to employ temperatures high enough to distill the secondary solvent from the NMP.
- the solvent need not be distilled from the refined oil and extract products, there is no limitation on the boiling range of the feed stock which may be processed.
- NMP may be employed for the solvent refining of kerosene and middle distillates, particularly for jet fuel manufacture, which stocks contain constituents coboiling with NMP and which cannot be separated by simple distillation procedures.
- secondary solvents may be selected to permit the use of relatively low temperatures thereby avoiding metallurgical problems and problems of solvent deterioration. Additionally the use of a secondary solvent provides a means to control the Water content of the NMP solvent to achieve highest solvent efficiency.
- FIGURE l shows the flow diagram of a solvent refining system employing NMP as solvent with liquid-liquid extraction of both raffinate phase and extract phase with a single secondary solvent which is recovered in common distillation facilities.
- FIGURE 2 shows a flow diagram of a solvent refining system employing a second solvent for re-extraction of extract products from NMP in the extract phase and a third solvent for re-extraction of NMP from the raffinate product in the raffinate phase.
- charge oil enters primary extraction tower through line 1 and is countercurrently contacted therein with recirculated NMP solvent entering through line 4.
- the charge stock may be any petroleum fraction which is liquid under the treating tower conditions.
- Treating tower conditions typically include a top tower temperature within the range of about 100 to 390 F. preferably within the range of about 100 to 250 F., and a bottom temperature range of about 100 to 390 F. preferably within the range of about 100 to 200 F.
- the treating tower pressure is typically maintained within the range of about Oto 100 pounds per square inch gauge and preferably within the range of about 20 to 50 pounds per square inch gauge.
- An NMP solvent dosage within the range of about 50 to 500 volume percent basis charge is used and preferably within the range of about 100 to 300 volume percent basis charge.
- Primary extraction tower 20 may be any efficient liquid-liquid contacting device having from 3 to 10 theoretical stages for example packed, spray, baffled or sieve-tray towers with or without mechanical pulse or sonic induced agitation, rotating disc contactors and centrifugal contacting devices.
- the water content of the entering solvent is maintained at a low level and below a maximum of about 1.0 weight percent basis solvent when treating lubricating oil stocks.
- the constituents of the charge stock soluble in the solvent are extracted and the resulting extract phase leaves tower 20 through line 3 and comprises principally aromatics dissolved in the bulk of the solvent.
- the non-extracted constituents of the charge stock comprising principally parains with some dissolved solvent leave tower 20 through line 2.
- the amount of dissolved solvent in the raffinate phase is characteristically related to the temperature of the tower top and the nature of the refined oil, that is, the raffinate product.
- Raffinate phase from tower 20 is discharged through line 2 to raffinate phase extractor 21.
- the raffinate phase is countercurrently contacted with Water introduced through line ⁇ 6.
- the water is introduced at a dosage of 20 to 100 volume percent basis the NMP in the rafiinate phase and preferably at a dosage within the range of 30 to 50 percent.
- the contacting temperature is maintained from ambient to about 210 F. and preferably within the range of about to 190 F. Extraction pressures of zero to 150 p.s.i.g. (pounds per square inch gauge) are suitable and pressures within the range of 10 to 2O p.s.i.g. are preferred.
- Raffinate phase extractor 21 may be any suitable liquid-liquid contacting device as in the case of tower 20. Solvent free raffinate product is discharged through line 5 for further processing or storage not shown. Wash water containing dissolved solvent is discharged from the Ibottom of extractor 21 through line 7.
- Extract phase from the bottom of tower 20 ⁇ is Withdrawn through line 3 and passed to extract phase extractor 23.
- Extractor 23 may be similar to extractor 21 except that it is necessarily larger in size due to the larger volume of solvent to be removed.
- Water is introduced at the top of extractor 23 through line 9 at a dosage of about 20 to 100 volume percent basis the solvent in the extract phase and preferably at a dosage of 40 to 50 volume percent.
- the temperatures and pressures employed are conveniently about the same as those employed in extractor 21.
- Solvent free extract product is discharged from the top of extractor 23 through line 8 to storage or further use not shown.
- Water containing dissolved solvent is discharged from the bottom of extractor 23 through line 10, combined with the water-NMP stream in line 7 and passed through line 11 to water-NMP distillation tower 22.
- Tower 22 may be a conventional distillation column of 5 to 10 theoretical stages and is operated to separate water as distillate from bottoms comprising NMP and not more than 1.0 weight percent water.
- the dried solvent is withdrawn from the bottom of tower 22 through line 4 for recycle to primary extraction tower 20.
- Distillate comprising water is discharged through line 12 and may be used to supply the extraction water passed through lines 6 and 9 to extractors 21 and 23 respectively.
- makeup water and makeup NMP may be added to the respective circulating systems to compensate for losses, leaks and the like, and correspondingly small amounts may be withdrawn to eliminate contaminants or excess water which may accumulate in the system.
- charge stock is introduced through line 30 into the lower portion of primary extractor 50, NMP solvent containing less than 1.0 weight percent water is introduced at the top of extractor 50 through line 31.
- the charge oil and solvent are countercurrently contacted forming raffinate phase comprising raffinate product with a small amount of NMP dissolved therein.
- Rafiinate phase is Withdrawn through line 32.
- Extract phase comprising NMP solvent with extract product dissolved therein is Withdrawn through line 33.
- Raffinate phase in line 32 is combined with water from line 34 and water phase from line 35 and passed to settler.
- the amount of water introduced through lines 34 and 35 is sufficient to cause about 80% of the NMP to separate thereby facilitating complete separation of the remaining NMP in subsequent Washing.
- an oil phase comprising raffinate product and a reduced amount of dissolved NMP separates from a lower solvent phase containing substantially all of the NMP.
- the separated oil phase is passed to countercurrent raffinate phase extractor 52 wherein it is contacted with water introduced through line 44 to remove remaining NMP.
- Bottoms from extractor 52 comprising water phase with NMP dissolved therein is returned to line 32 as described hereinbefore.
- Raffinate product is withdrawn from extractor 52 through line 41 and passed to dehydrator 54.
- Dehydrator 54 may be, for example, a vacuum stripper used to remove dissolved water when the manufacture of a bone dry product is desired.
- the dried raffinate product is discharged through line 42 to storage or use not shown.
- Solvent phase from settler 51 is withdrawn through line 43 and passed to water stripping distillation tower 53.
- water is separated as a distillate through line 44 from bottoms comprising NMP and not more than 1.0 weight percent water is withdrawn through line 31. Water in excess of that passed to extractor 52 is withdrawn through line 45.
- Extract phase in line 33 is passed to extract phase extractor 55 wherein it is countercurrently contacted with light hydrocarbon introduced through line 46.
- the light hydrocarbon in line ⁇ 46 has a boiling range which does not overlap the boiling range of the charge stock and preferably has a boiling range at least 50 F. below that of NMP.
- the hydrocarbon solvent may be paraflinic, naphthenic, or aromatic or a mixture of hydrocarbon types, preferably a parafiinic stock is employed.
- the light hydrocarbon acts as a solvent to dissolve the extract product from the extract phase forming a secondary extract withdrawn through line 47. NMP stripped of the extract product is withdrawn from the bottom of extractor 55 through line 48 and recycled through line 31 to primary extractor 50. Makeup solvent, as required, is added to line 31 from line 29.
- Extract phase comprising extract product dissolved in hydrocarbon solvent in line 47 is passed to stripper 56 wherein the light hydrocarbon solvent is separated by distillation and returned to extractor 55 through line 46. Extract product is withdrawn from the bottom of stripper 56 through line 49 and discharged to storage or use not shown.
- Solvent dosage vol. percent- 200 200 200 200 200 200 Extraction temperature
- Extract RI at 70 C 1. 5030 1. 5072 1.5077 1. 5194 1. 5349 It will be noted that as water is added to the NMP solvent, the amount of oil extracted decreases. The effect of the reduced extraction of undesired constituents however, does not affect refined oil quality until the amount of water in the solvent exceeds about 1.0 percent. The solvents efficiency in producing a refined oil of high quality is then significantly affected as shown by the higher refractive index of the refined oil at solvent water levels above 2.0 Weight percent. It should also be noted that at 0.5 weight percent water, a higher yield of refined oil is obtained having the same quality as the product obtained with water-free solvent as indicated by the refined oil refractive index.
- a lubricating oil stock referred to as Wax Distillate 20 is treated with NMP containing a trace of water to produce a refined oil (raffinate product) of increased viscosity index and improved inhibitor response useful in the manufacture of high quality lubricating oil of high viscosity index and high stability.
- NMP a trace of water
- the conditions used and results obtained are shown in Table III following:
- Solvent dosage vol. percent 282 Extract out temp., F 160 Refined oil out temp., F 165 Refined oil yield, vol. percent- 62. 2 Charge oil rate, b.p.d 10, 000
- Rencd oil Water extraction tower conditions tower Extract tower Temperature, F 150 150 Pressure, p.s.i.g 10 10 Water dosage, w
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Lubricants (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Pyrrole Compounds (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US62497067A | 1967-03-13 | 1967-03-13 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3451925A true US3451925A (en) | 1969-06-24 |
Family
ID=24504072
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US624970A Expired - Lifetime US3451925A (en) | 1967-03-13 | 1967-03-13 | Solvent extraction of hydrocarbons with n-methyl-2-pyrrolidone |
Country Status (5)
Country | Link |
---|---|
US (1) | US3451925A (de) |
DE (1) | DE1645813C3 (de) |
FR (1) | FR1555437A (de) |
GB (1) | GB1159772A (de) |
NL (1) | NL147469B (de) |
Cited By (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3658659A (en) * | 1969-09-24 | 1972-04-25 | Phillips Petroleum Co | Separating p-dichlorobenzene from n-methyl pyrrolidone by steam distillation |
US4101413A (en) * | 1974-11-08 | 1978-07-18 | Coal Industry (Patents) Limited | Extraction of coal |
DE3107360A1 (de) * | 1980-03-07 | 1982-02-18 | Texaco Development Corp., 10650 White Plains, N.Y. | "verfahren zur loesungsmittelraffinierung von kohlenwasserstoffgemischen" |
US4333824A (en) * | 1980-06-27 | 1982-06-08 | Texaco Inc. | Refining highly aromatic lube oil stocks |
US4334983A (en) * | 1980-06-30 | 1982-06-15 | Exxon Research & Engineering Co. | Stripping steam recycle for solvent recovery processes |
US4342646A (en) * | 1980-09-24 | 1982-08-03 | Texaco Inc. | Trace solvent recovery in selective solvent extraction |
US4390418A (en) * | 1982-05-12 | 1983-06-28 | Texaco Inc. | Recovery of solvent in hydrocarbon processing systems |
US4419227A (en) * | 1982-05-12 | 1983-12-06 | Texaco Inc. | Recovery of solvent from a hydrocarbon extract |
US4510047A (en) * | 1983-12-14 | 1985-04-09 | Exxon Research And Engineering Co. | Selective extraction solvent recovery using regenerated cellulose membrane under reverse osmosis conditions |
US4569755A (en) * | 1984-12-31 | 1986-02-11 | Sun Refining And Marketing Company | Extraction of aromatics with N-cyclohexyl-2-pyrrolidone |
WO1986004082A1 (en) * | 1984-12-28 | 1986-07-17 | Union Carbide Corporation | Separation of aromatic and nonaromatic components in mixed hydrocarbon feeds |
US4604184A (en) * | 1983-11-16 | 1986-08-05 | Domtar Inc. | Modified coal-tar pitch |
US20130062254A1 (en) * | 2011-07-29 | 2013-03-14 | Omer Refa Koseoglu | Selective single-stage hydroprocessing system and method |
KR20140064824A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 직렬-흐름 수소화처리 시스템 및 방법 |
KR20140064816A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 2-단계 수소화처리 시스템 및 방법 |
KR20140064818A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 2-단계 수소화처리 시스템 및 방법 |
KR20140064817A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 직렬-흐름 수소화처리 시스템 및 방법 |
CN104718276A (zh) * | 2012-08-09 | 2015-06-17 | 科学工业研究委员会 | 用于通过从含有机过氧化物的未加工的裂化汽油馏分回收高纯度苯来制备贫苯汽油的方法 |
WO2016162887A1 (en) * | 2015-04-09 | 2016-10-13 | Bharat Petroleum Corporation Limited | Aromatic free solvent and process of preparing the same from petroleum stream |
US9512369B1 (en) | 2013-03-14 | 2016-12-06 | James Joseph Noble | Process for removing color bodies from used oil |
WO2022079053A1 (en) * | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
WO2022079060A1 (en) * | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
WO2023083655A1 (de) * | 2021-11-12 | 2023-05-19 | Thyssenkrupp Industrial Solutions Ag | Verfahren und vorrichtung zur trennung eines kohlenwasserstoffhaltigen einsatzstoffstroms durch extraktivdestillation |
BE1029922B1 (de) * | 2021-11-12 | 2023-06-12 | Thyssenkrupp Uhde Eng Services Gmbh | Verfahren und Vorrichtung zur Trennung eines kohlenwasserstoffhaltigen Einsatzstoffstroms durch Extraktivdestillation |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2012809B (en) * | 1977-12-22 | 1982-04-15 | Exxon Research Engineering Co | Simultaneous deasphalting extraction process |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2963427A (en) * | 1956-04-18 | 1960-12-06 | Standard Oil Co | Aromatics recovery system using butyrolactone in the first stage and propane in the second stage |
CA610414A (en) * | 1960-12-13 | D. Morin Richard | Separation of hydrocarbon mixtures |
-
1967
- 1967-03-13 US US624970A patent/US3451925A/en not_active Expired - Lifetime
-
1968
- 1968-02-07 GB GB6047/68A patent/GB1159772A/en not_active Expired
- 1968-03-12 FR FR1555437D patent/FR1555437A/fr not_active Expired
- 1968-03-13 DE DE19681645813 patent/DE1645813C3/de not_active Expired
- 1968-03-13 NL NL686803582A patent/NL147469B/xx not_active IP Right Cessation
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA610414A (en) * | 1960-12-13 | D. Morin Richard | Separation of hydrocarbon mixtures | |
US2963427A (en) * | 1956-04-18 | 1960-12-06 | Standard Oil Co | Aromatics recovery system using butyrolactone in the first stage and propane in the second stage |
Cited By (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3658659A (en) * | 1969-09-24 | 1972-04-25 | Phillips Petroleum Co | Separating p-dichlorobenzene from n-methyl pyrrolidone by steam distillation |
US4101413A (en) * | 1974-11-08 | 1978-07-18 | Coal Industry (Patents) Limited | Extraction of coal |
DE3107360A1 (de) * | 1980-03-07 | 1982-02-18 | Texaco Development Corp., 10650 White Plains, N.Y. | "verfahren zur loesungsmittelraffinierung von kohlenwasserstoffgemischen" |
US4333824A (en) * | 1980-06-27 | 1982-06-08 | Texaco Inc. | Refining highly aromatic lube oil stocks |
US4334983A (en) * | 1980-06-30 | 1982-06-15 | Exxon Research & Engineering Co. | Stripping steam recycle for solvent recovery processes |
US4342646A (en) * | 1980-09-24 | 1982-08-03 | Texaco Inc. | Trace solvent recovery in selective solvent extraction |
US4390418A (en) * | 1982-05-12 | 1983-06-28 | Texaco Inc. | Recovery of solvent in hydrocarbon processing systems |
US4419227A (en) * | 1982-05-12 | 1983-12-06 | Texaco Inc. | Recovery of solvent from a hydrocarbon extract |
US4604184A (en) * | 1983-11-16 | 1986-08-05 | Domtar Inc. | Modified coal-tar pitch |
US4510047A (en) * | 1983-12-14 | 1985-04-09 | Exxon Research And Engineering Co. | Selective extraction solvent recovery using regenerated cellulose membrane under reverse osmosis conditions |
WO1986004082A1 (en) * | 1984-12-28 | 1986-07-17 | Union Carbide Corporation | Separation of aromatic and nonaromatic components in mixed hydrocarbon feeds |
US4569755A (en) * | 1984-12-31 | 1986-02-11 | Sun Refining And Marketing Company | Extraction of aromatics with N-cyclohexyl-2-pyrrolidone |
KR20140064816A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 2-단계 수소화처리 시스템 및 방법 |
US9359566B2 (en) * | 2011-07-29 | 2016-06-07 | Saudi Arabian Oil Company | Selective single-stage hydroprocessing system and method |
US20130062254A1 (en) * | 2011-07-29 | 2013-03-14 | Omer Refa Koseoglu | Selective single-stage hydroprocessing system and method |
KR20140064818A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 2-단계 수소화처리 시스템 및 방법 |
KR20140064823A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 단일-단계 수소화처리 시스템 및 방법 |
KR20140064817A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 직렬-흐름 수소화처리 시스템 및 방법 |
KR20140064824A (ko) * | 2011-07-29 | 2014-05-28 | 사우디 아라비안 오일 컴퍼니 | 선택적 직렬-흐름 수소화처리 시스템 및 방법 |
CN104718276A (zh) * | 2012-08-09 | 2015-06-17 | 科学工业研究委员会 | 用于通过从含有机过氧化物的未加工的裂化汽油馏分回收高纯度苯来制备贫苯汽油的方法 |
CN104718276B (zh) * | 2012-08-09 | 2017-08-25 | 科学工业研究委员会 | 用于通过从含有机过氧化物的未加工的裂化汽油馏分回收高纯度苯来制备贫苯汽油的方法 |
EP2882830B1 (de) * | 2012-08-09 | 2018-01-03 | Council of Scientific & Industrial Research | Verfahren zur herstellung von benzin mit geringem benzolgehalt durch rückgewinnung von hochreinem benzol aus unbehandelten krackbenzinfraktionen mit organischen peroxiden |
US9512369B1 (en) | 2013-03-14 | 2016-12-06 | James Joseph Noble | Process for removing color bodies from used oil |
WO2016162887A1 (en) * | 2015-04-09 | 2016-10-13 | Bharat Petroleum Corporation Limited | Aromatic free solvent and process of preparing the same from petroleum stream |
WO2022079053A1 (en) * | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
WO2022079060A1 (en) * | 2020-10-16 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Recovery of aliphatic hydrocarbons |
WO2023083655A1 (de) * | 2021-11-12 | 2023-05-19 | Thyssenkrupp Industrial Solutions Ag | Verfahren und vorrichtung zur trennung eines kohlenwasserstoffhaltigen einsatzstoffstroms durch extraktivdestillation |
BE1029922B1 (de) * | 2021-11-12 | 2023-06-12 | Thyssenkrupp Uhde Eng Services Gmbh | Verfahren und Vorrichtung zur Trennung eines kohlenwasserstoffhaltigen Einsatzstoffstroms durch Extraktivdestillation |
Also Published As
Publication number | Publication date |
---|---|
NL147469B (nl) | 1975-10-15 |
DE1645813B2 (de) | 1972-07-13 |
DE1645813A1 (de) | 1970-03-12 |
GB1159772A (en) | 1969-07-30 |
DE1645813C3 (de) | 1973-03-01 |
FR1555437A (de) | 1969-01-24 |
NL6803582A (de) | 1968-09-16 |
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