US2953523A - Chemical process - Google Patents
Chemical process Download PDFInfo
- Publication number
- US2953523A US2953523A US645685A US64568557A US2953523A US 2953523 A US2953523 A US 2953523A US 645685 A US645685 A US 645685A US 64568557 A US64568557 A US 64568557A US 2953523 A US2953523 A US 2953523A
- Authority
- US
- United States
- Prior art keywords
- hydrocarbon
- straight run
- catalytically cracked
- sulfur
- mixture
- 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
Links
- 238000001311 chemical methods and process Methods 0.000 title description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 44
- 229930195733 hydrocarbon Natural products 0.000 claims description 42
- 150000002430 hydrocarbons Chemical class 0.000 claims description 42
- 239000004215 Carbon black (E152) Substances 0.000 claims description 39
- 150000003464 sulfur compounds Chemical class 0.000 claims description 24
- 239000000203 mixture Substances 0.000 claims description 21
- 238000000605 extraction Methods 0.000 claims description 18
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 17
- 229910052717 sulfur Inorganic materials 0.000 claims description 17
- 239000011593 sulfur Substances 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 239000000295 fuel oil Substances 0.000 description 40
- 229940065278 sulfur compound Drugs 0.000 description 22
- 229960005349 sulfur Drugs 0.000 description 16
- 235000001508 sulfur Nutrition 0.000 description 16
- 238000000034 method Methods 0.000 description 11
- 239000003921 oil Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 5
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 3
- 239000003350 kerosene Substances 0.000 description 3
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000010743 number 2 fuel oil Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/08—Inorganic compounds only
- C10G21/10—Sulfur dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
Definitions
- the extraction with sulfur dioxide should be carried out at a temperature and pressure such that the sulfur dioxide is in liquid phase. Temperatures below about ambient temperature are generally used. Temperatures below about 1 5 F. give highest selectivity. A temperature between about -20 and ambient temperature and especially about 10 to -F. is preferred. While lower and catalytically cracked hydrocarbon both of which con-- tain sulfur.
- My invention has for its object to provide improved procedure for removing sulfur compounds from straight run and catalytically cracked hydrocarbon fractions. Another object is to provide improved procedure for preparing a fuel oil from straight run and catalytically cracked hydrocarbons which contain sulfur compounds. A still further object is to provide improved procedure for preparing a mixture which is low in sulfur compoundsfrom straight run and catalytic-ally cracked stocks which contain sulfur compounds. Other objects will appear hereinafter.
- my invention includes separately extracting with sulfur dioxide a straight run hydrocarbon which contains sulfur compounds and a catalytically cracked hydrocarbon which contains sulfur compounds, separating the raffinate phase from both extractions and combining the two raffinate phases to produce a mixture of straight run and catalytically cracked hydrocarbon having a lower sulfur content.
- My invention is applicable to the preparation of any mixture of straight run and catalytically cracked hydrocarbons, the components of which mixture contain sul fur compounds in undesirable amounts.
- the invention may be applied to the preparation of a furnace oil or No. 2 fuel oil from a straight run hydrocarbon and a catalytically cracked hydrocarbon boiling in the furnace oil or No. 2 fuel oil range and containing unde sira-ble amounts of sulfur compounds.
- the invention is also applicable, for instance, to the preparation of an improved kerosene, Diesel fuel or catalytic cracking charge stock (gas oil) from straight runfand catalytically cracked hydrocarbons having appropriate distillation characteristics for the product in question and containing sulfur compounds.
- the invention is applicable to preparing a final product containing any ratio of the may be employed in either single or multi-stage.
- the sulfur dioxide to hydrocarbon ratio may be between about 01:1 and 10:1. A ratio of between about 0.511 and 5:1 is preferable.
- the extraction may be accomplished by contacting the sulfur dioxide with the individual hydrocarbon components in any known manner which will give intimate contact between the sulfur dioxide and the hydrocarbon.
- a batch or countercurrent method of contacting It is desirable to permit contact between hydrocarbon and sulfur dioxide to continue until approximate equilibrium is reached.
- a continuous counterourrent extraction system should be used.
- the sulfur dioxide is heavier than the hydrocarbon so that it is introduced into the top of the countercurrent extractor. It will sink to the bottom of the continuous countercurrent extractor from which point it may be withdrawn and separated into extracted hydrocarbon and sulfur dioxide.
- the sulfur dioxide may be recycled for further use in the process.
- the charge stock is introduced into the bottom of the countercurrent extractor and the raflinate is removed from the upper portion of the continuous countercurrent extractor.
- the rafiinate is ready for the final step, i.e. intermixture with the other hydrocarbon component to produce the straight run-catalytically cracked hydrocarbon mixture containing a smaller amount of sulfur compounds.
- Raflinate Gravity API 40.3 21. 5 35.4 41. 7 42.7 43.3 44. 7 Mean Molecular Weight..- 246 242 265 Sulfur, Braun-Shell, Percent O. 93 2. 78 1. 38 0. 58 0. 43 0.39 0.25 Sediment, Percent, ASTM D 473- 0.02 0.01 0.01 Aniline Point, F AS'IM D611- T 140 170 176 175 181 Cetane Number 56 36 62 65 67 69 Extract Gravity, APT 24. 8 25. 1 18. 9 19.1 Mean Molecular Weight-.- 215 213 199 214 Sulfur, Braun-Shell, Percent 2. 79 2. 72 3. 46 3.
- the process for preparing an improved hydrocarbon contains sulfur compounds which process comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide and thereafter combining the raflinates from both extractions to produce a mixed straight run-catalytically cracked furnace oil having a lower sulfur content.
- the process for preparing an improved furnace oil containing a relatively small amount of sulfur compounds from a straight run furnace oil which contains sulfur compounds and a catalytically cracked furnace oil which contains sulfur compounds comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide at a temperature between about ambient temperature and 20 F., at a sulfur dioxide-furnace oil ratio between about 0.111 and 10:1
- the process for preparing an improved furnace oil containing a relatively small amount of sulfur compounds from a straight run furnace oil which contains sulfur comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide at a temperature of about 15 F, at a sulfur dioxide-furnace oil ratio between about 0.5 :1 and 5 :-1 and thereafter combining the raflinates .from both extractions to produce a mixed straight runcompounds and a catalytically cracked furnace oil which catalytically cracked furnace oil having a lower sulfurv content.
Description
United States Patent CHEMICAL PROCESS William R. Lehrian, Verona, Pa., assignor to Gnu Research & Development Company, Pittsburgh, Pa., a corporation of Delaware No Drawing. Filed Mar. 13, 1957, Ser. No. 645,685
Claims. (Cl. 208-242) This invention relates to procedure for preparing a desulfurized hydrocarbon mixture from a straight run" Patented Sept. 20, 1960 straight run and catalytically cracked hydrocarbons. This ratio usually depends upon the amount of these stocks which are available in the refinery. In general the mixture contains about 1 to 99 percent of either component.
The extraction with sulfur dioxide should be carried out at a temperature and pressure such that the sulfur dioxide is in liquid phase. Temperatures below about ambient temperature are generally used. Temperatures below about 1 5 F. give highest selectivity. A temperature between about -20 and ambient temperature and especially about 10 to -F. is preferred. While lower and catalytically cracked hydrocarbon both of which con-- tain sulfur.
It is common practice in petroleum refining operations to mix straight run and catalytically cracked stocks used for various purposes. For instance, in preparing furnace oils it is general practice to mix straight run furnace oil with cat-al-ytioally cracked furnace oil. Similarly it is common practice to mix straight run gas oil with cycle stock before catalytically cracking. The straight run and catalytically cracked stocks frequently contain sulfur compounds and removal of such sulfur compounds is desirable.
My invention has for its object to provide improved procedure for removing sulfur compounds from straight run and catalytically cracked hydrocarbon fractions. Another object is to provide improved procedure for preparing a fuel oil from straight run and catalytically cracked hydrocarbons which contain sulfur compounds. A still further object is to provide improved procedure for preparing a mixture which is low in sulfur compoundsfrom straight run and catalytic-ally cracked stocks which contain sulfur compounds. Other objects will appear hereinafter.
These and other objects are accomplished by my invention which includes separately extracting with sulfur dioxide a straight run hydrocarbon which contains sulfur compounds and a catalytically cracked hydrocarbon which contains sulfur compounds, separating the raffinate phase from both extractions and combining the two raffinate phases to produce a mixture of straight run and catalytically cracked hydrocarbon having a lower sulfur content.
In the following examples and description I have set forth several of the preferred embodiments of my invention but it is to be understood that they are given for the purpose of illustration and not in limitation thereof.
My invention is applicable to the preparation of any mixture of straight run and catalytically cracked hydrocarbons, the components of which mixture contain sul fur compounds in undesirable amounts. Thus the invention may be applied to the preparation of a furnace oil or No. 2 fuel oil from a straight run hydrocarbon and a catalytically cracked hydrocarbon boiling in the furnace oil or No. 2 fuel oil range and containing unde sira-ble amounts of sulfur compounds. The invention is also applicable, for instance, to the preparation of an improved kerosene, Diesel fuel or catalytic cracking charge stock (gas oil) from straight runfand catalytically cracked hydrocarbons having appropriate distillation characteristics for the product in question and containing sulfur compounds. The invention is applicable to preparing a final product containing any ratio of the may be employed in either single or multi-stage.
temperatures than 20 F. may be employed, the cost of operation is increased by the additional refrigeration required. Higher temperatures than ambient temperature can be used. However the additional compression necessary to maintain the sulfur dioxide in liquid phase adds to the cost of operation. The sulfur dioxide to hydrocarbon ratio may be between about 01:1 and 10:1. A ratio of between about 0.511 and 5:1 is preferable.
The extraction may be accomplished by contacting the sulfur dioxide with the individual hydrocarbon components in any known manner which will give intimate contact between the sulfur dioxide and the hydrocarbon. Thus a batch or countercurrent method of contacting It is desirable to permit contact between hydrocarbon and sulfur dioxide to continue until approximate equilibrium is reached. For highest eificiency a continuous counterourrent extraction system should be used. The sulfur dioxide is heavier than the hydrocarbon so that it is introduced into the top of the countercurrent extractor. It will sink to the bottom of the continuous countercurrent extractor from which point it may be withdrawn and separated into extracted hydrocarbon and sulfur dioxide. The sulfur dioxide may be recycled for further use in the process. The charge stock is introduced into the bottom of the countercurrent extractor and the raflinate is removed from the upper portion of the continuous countercurrent extractor. -After separation of the small amount of absorbed sulfur dioxide the rafiinate is ready for the final step, i.e. intermixture with the other hydrocarbon component to produce the straight run-catalytically cracked hydrocarbon mixture containing a smaller amount of sulfur compounds.
EXAMPLE Virgin and catalytically cracked No. 2 furnace oils having the properties shown in the first and second columns respectively of the accompanying table were mixed in the ratio of 77 percent by volume Kuwait No. 2 straight run furnace oil and 23 percent by volume Kuwait catalytically cracked No. 2 furnace oil. This mixture was then extracted with sulfur dioxide in a sulfur dioxidehydrocarbon ratio of 2:1 and 5 :1. The results of these extractions are given in the fourth and fifth columns of the accompanying table. In another experiment the same straight run Kuwait No. 2 furnace oil and the same Kuwait catalytic No. 2 furnace oil were extracted sep parately with liquid sulfur dioxide in a sulfur dioxidehydrocarbon ratio of 2:1 and 5:1. The raffi-nates from these extractions were then blended. The proportions of this blend corresponded to the yield of raffinate which 'would be obtained when 77 parts by volume of Kuwait #2 furnace oil and 23 parts by volume of Kuwait catalytic #2 furnace oil are separately extracted. The results of these extractions are given in the sixth and seventh columns of the accompanying table.
Table LIQUID SULFUR DIOXIDE EXTRACTION OF KUWAIT VIRGIN AND KUWAIT FLUID CATALYTIC NO. 2 FURNACE OILS Charge Stocks Extraction of Separate Extraction Operation Blended Of Furnace Furnace Oils Oils Followed Virgin Catalytic Blend 1 by Blending Liquid Sulfur Dioxide/Oil Ratio" 2. 5. 0 2.0 5.0 Temperature, F 15 15 15 Yield of Raflinate: Percent by Vol.
of Combined No. 2 Furnace Oils. 65.3 58.9 70.5 63. 8 Inspections:
Raflinate Gravity, API 40.3 21. 5 35.4 41. 7 42.7 43.3 44. 7 Mean Molecular Weight..- 246 242 265 Sulfur, Braun-Shell, Percent O. 93 2. 78 1. 38 0. 58 0. 43 0.39 0.25 Sediment, Percent, ASTM D 473- 0.02 0.01 0.01 Aniline Point, F AS'IM D611- T 140 170 176 175 181 Cetane Number 56 36 62 65 67 69 Extract Gravity, APT 24. 8 25. 1 18. 9 19.1 Mean Molecular Weight-.- 215 213 199 214 Sulfur, Braun-Shell, Percent 2. 79 2. 72 3. 46 3. 12 Sediment, Percent, ASTM D473-48 0.03 Aniline Point, F., ASTM D6l151T 66 63 32 32 1 Blend of 77% by volume Kuwait No. 2 Furnace Oil and 23% by volume Kuwait catalytic No. 2 Furnace Oil.
The results of the last mentioned extractions when compared with the corresponding extractions of the blend show that the procedure of the invention resulted in a considerably lower sulfur content in the product. Furthermore the procedure of the invention gave a substantially higher yield of final product and the cetane number in every case was improved.
I claim:
1. The process for preparing an improved mixture of a straight run hydrocarbon and a catalytically cracked hydrocarbon both of which initially contain sulfur compounds, the straight run hydrocmbon and the catalytically cracked hydrocarbon being selected from the group consisting of kerosene, diesel fuel, gas oil and fuel oil, said mixture after preparation containing a relatively small amount of sulfur compounds, which comprises in combination separately extracting the straight run hydrocarbon and catalytically cracked hydrocarbon with a liquid comprising essentially sulfur dioxide, separating the raffinate phases from both extractions, and combining the railinate phases to produce a mixture of said straight run and said catalytically cracked hydrocarbon having a lower sulfur content.
2. The process for preparing an improved hydrocarbon contains sulfur compounds which process comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide and thereafter combining the raflinates from both extractions to produce a mixed straight run-catalytically cracked furnace oil having a lower sulfur content.
4. The process for preparing an improved furnace oil containing a relatively small amount of sulfur compounds from a straight run furnace oil which contains sulfur compounds and a catalytically cracked furnace oil which contains sulfur compounds which process comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide at a temperature between about ambient temperature and 20 F., at a sulfur dioxide-furnace oil ratio between about 0.111 and 10:1
and thereafter combining the raflinates from both extractions to produce a mixed straight run-catalytically cracked furnace oil having a lower sulfur content.
mixture of a straight run hydrocarbon and a catalytically i cracked hydrocarbon both of which initially contain sulsulfur compounds, the straight run hydrocarbon and the catalytically cracked hydrocarbon being selected from the group consisting of kerosene, diesel fuel, gas oil and fuel oil, said mixture after preparation containing a relatively small amount of sulfur compounds, which comprises in combination separately extracting the straight run hydrocarbon and catalytically cracked hydrocarbon with a liquid comprising essentially sulfur dioxide at a temperature below about ambient temperature, at a sulfur dioxide-hydrocarbon ratio between about 01:1 and 10:1, separating the raflinate phases from both extractions, and combining the raffinate phases to produce an improved hydrocarbon mixture of said straight run and said catalytically cracked hydrocarbon having a lower sulfur content.
3. The process for preparing an improved furnace oil containing a relatively small amount of sulfur compounds from a straight run furnace oil which contains sulfur 5. The process for preparing an improved furnace oil containing a relatively small amount of sulfur compounds from a straight run furnace oil which contains sulfur compounds and a catalytically cracked furnace oil which contains sulfur compounds which process comprises separately extracting the straight run furnace oil and the catalytically cracked furnace oil with a liquid comprising essentially sulfur dioxide at a temperature of about 15 F, at a sulfur dioxide-furnace oil ratio between about 0.5 :1 and 5 :-1 and thereafter combining the raflinates .from both extractions to produce a mixed straight runcompounds and a catalytically cracked furnace oil which catalytically cracked furnace oil having a lower sulfurv content.
References Cited in the file of this patent UNITED STATES PATENTS 2,592,383 Blatz Apr. 8, 1952 2,646,390 Arnold et a1. July 21, 1953 2,673,830 Arnold Mar. 30, 1954 2,717,229 Findlay Sept. 6, 1955 2,719,105 Peterson Sept. 27, 1955 2,726,989 Seelig et a1. Dec. 13, 1955 2,727,851 Krause Dec. 20, 1955 2,754,342 Shelton July 10, 1956 2,764,522 Hettick Sept. 25, 1956
Claims (1)
1. THE PROCESS FOR PREPARING AN IMPROVED MIXTURE OF A STRAIGHT RUN HYDROCARBON AND A CATALYTICALLY CRACKED HYDROCARBON BOTH OF WHICH INTIALLY CONTAIN SULFUR COMPOUNDS, THE STRAIGHT RUN HYDROCARBON AND THE CATALYTICALLY CRACKED HYDROCARBON BEING SELECTED FROM THE GROUP MIXTURE AFTER PREPARATION CONTAINING A RELATIVELY SMALL AMOUNT OF SULFUR COMPOUNDS, WHICH COMPRISES IN COMBINATION SEPARATELY EXTRACTING THE STRAIGHT RUN HYDROCARBON AND CATALYTICALLY CRACKED HYDROCARBON WITH A LIQUID COMPRISING ESSENTIALLY SULFUR DIOXIDE, SEPARATING THE RAFFINATE PHASES FROM BOTH EXTRACTIONS, AND COMBINING THE RAFFINATE PHASE TO PRODUCE A MIXTURE OF SAID STRAIGHT RUN AND SAID CATALYTICALLY CRACKED HYDROCARBON HAVING A LOWER SULFUR CONTENT.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US645685A US2953523A (en) | 1957-03-13 | 1957-03-13 | Chemical process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US645685A US2953523A (en) | 1957-03-13 | 1957-03-13 | Chemical process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2953523A true US2953523A (en) | 1960-09-20 |
Family
ID=24590047
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US645685A Expired - Lifetime US2953523A (en) | 1957-03-13 | 1957-03-13 | Chemical process |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2953523A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4948494A (en) * | 1989-06-28 | 1990-08-14 | Union Oil Company Of California | Removal of hydrogen sulfide from produced fluids |
| US5346614A (en) * | 1992-11-10 | 1994-09-13 | Union Oil Company Of California | Removal of hydrogen sulfide from an oil-containing mixture having a continuous aqueous phase |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2592383A (en) * | 1949-06-28 | 1952-04-08 | Standard Oil Dev Co | Process for preparing heating oil |
| US2646390A (en) * | 1950-12-16 | 1953-07-21 | Standard Oil Co | Desulfurization of distillate fuels |
| US2673830A (en) * | 1950-06-23 | 1954-03-30 | Standard Oil Co | Desulfurization of distillate fuels |
| US2717229A (en) * | 1952-09-22 | 1955-09-06 | Phillips Petroleum Co | Solvent extraction process |
| US2719105A (en) * | 1952-02-27 | 1955-09-27 | Exxon Research Engineering Co | Process for the production of high quality heating oil blends |
| US2726989A (en) * | 1952-11-26 | 1955-12-13 | Standard Oil Co | Heater oil purification using sulfur dioxide and a halogen |
| US2727851A (en) * | 1952-07-18 | 1955-12-20 | Standard Oil Co | Refining of heater oil |
| US2754342A (en) * | 1951-11-05 | 1956-07-10 | Phillips Petroleum Co | Aromatic hydrocarbon separation process |
| US2764522A (en) * | 1952-12-29 | 1956-09-25 | Phillips Petroleum Co | Hydrocarbon extraction unit and operation |
-
1957
- 1957-03-13 US US645685A patent/US2953523A/en not_active Expired - Lifetime
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2592383A (en) * | 1949-06-28 | 1952-04-08 | Standard Oil Dev Co | Process for preparing heating oil |
| US2673830A (en) * | 1950-06-23 | 1954-03-30 | Standard Oil Co | Desulfurization of distillate fuels |
| US2646390A (en) * | 1950-12-16 | 1953-07-21 | Standard Oil Co | Desulfurization of distillate fuels |
| US2754342A (en) * | 1951-11-05 | 1956-07-10 | Phillips Petroleum Co | Aromatic hydrocarbon separation process |
| US2719105A (en) * | 1952-02-27 | 1955-09-27 | Exxon Research Engineering Co | Process for the production of high quality heating oil blends |
| US2727851A (en) * | 1952-07-18 | 1955-12-20 | Standard Oil Co | Refining of heater oil |
| US2717229A (en) * | 1952-09-22 | 1955-09-06 | Phillips Petroleum Co | Solvent extraction process |
| US2726989A (en) * | 1952-11-26 | 1955-12-13 | Standard Oil Co | Heater oil purification using sulfur dioxide and a halogen |
| US2764522A (en) * | 1952-12-29 | 1956-09-25 | Phillips Petroleum Co | Hydrocarbon extraction unit and operation |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4948494A (en) * | 1989-06-28 | 1990-08-14 | Union Oil Company Of California | Removal of hydrogen sulfide from produced fluids |
| WO1991000243A1 (en) * | 1989-06-28 | 1991-01-10 | Union Oil Company Of California | Removal of hydrogen sulfide from produced fluids |
| US5346614A (en) * | 1992-11-10 | 1994-09-13 | Union Oil Company Of California | Removal of hydrogen sulfide from an oil-containing mixture having a continuous aqueous phase |
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