US2611735A - Process for removing metals from crude petroleum oils - Google Patents
Process for removing metals from crude petroleum oils Download PDFInfo
- Publication number
- US2611735A US2611735A US756283A US75628347A US2611735A US 2611735 A US2611735 A US 2611735A US 756283 A US756283 A US 756283A US 75628347 A US75628347 A US 75628347A US 2611735 A US2611735 A US 2611735A
- Authority
- US
- United States
- Prior art keywords
- oil
- acid
- crude petroleum
- petroleum oils
- crude
- 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.)
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- 239000003921 oil Substances 0.000 title claims description 32
- 239000003208 petroleum Substances 0.000 title claims description 12
- 238000000034 method Methods 0.000 title claims description 5
- 239000002184 metal Substances 0.000 title description 11
- 229910052751 metal Inorganic materials 0.000 title description 11
- 150000002739 metals Chemical class 0.000 title description 4
- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 claims description 16
- 238000004523 catalytic cracking Methods 0.000 claims description 5
- 238000005336 cracking Methods 0.000 claims description 5
- 239000003054 catalyst Substances 0.000 claims description 3
- 150000002736 metal compounds Chemical class 0.000 claims description 3
- 239000002253 acid Substances 0.000 description 18
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- 150000001875 compounds Chemical class 0.000 description 7
- 239000010779 crude oil Substances 0.000 description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 241000370999 Losaria coon Species 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 238000009937 brining Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000011888 foil Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 235000015250 liver sausages Nutrition 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Inorganic materials [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
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
- C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
- C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
- C10G17/04—Liquid-liquid treatment forming two immiscible phases
- C10G17/06—Liquid-liquid treatment forming two immiscible phases using acids derived from sulfur or acid sludge thereof
Definitions
- This invention relates to improvements in the production of motor fuels from crude petroleum oil by catalytic cracking.
- catalytic'cracking operations as heretofore carried out, it has in most cases been necessary to use gas oil or other distillate as the charging stock.
- gas oil or other distillate As the charging stock.
- One important factor which has prevented theuse of reduced or top crude oils, with or without deasphalting, is that with the use of suchfe ed stocks the catalystrapidly. deteriorates.
- Most topped orreduced crude oils contain substantial amounts of inorganic salts, in particular sodium, calcium, and magnesium chloride, and in many cases other metallic compounds such as compounds of vanadium and nickel, the natureof which have not been fully established, and compounds of other metals.
- the crude oil, before or after topping or deasphalting is treated with fiuorosulfonic acid under appropriate conditions of temperature and prespany, New York, N. v I,
- the amountof fiuorosulfoniclacid requiredjior the removal of metal contaminants from the oil is slightly in excess "of one equivalent of 'fiuoro sulfonic acid for each equivalent of metal; and with most reduced or topped crude oils, this corresponds to a fraction of 1% of fluorosulfonic acid basedon the oil. Becausejdiflicultiesimay'been: countered in brin ing. about intimate contact of the oil with this small amount of fluorosulfonic acid, it is usually'adyantageous .toruse. a some what larger. amount, for example; 3 to5 'o'ifiluo rosulfonic acid based 'onfthe foil, recover the "ex.
- the resulting fiuorosulfonates are readily separated from the oil by filtration, settling, centrifuging or the like, and the resulting crude oil, substantially free from metal contaminants, is useful as such as the charging stock for catalytic cracking operations.
- the use of this as charging stock as compared with gas oil or the like results in substantial economic benefits.
- the fluorosulfonic acid may be brought into contact with the metal-contaminated oil in any suitable way.
- the fluorosulfonic acid is used as the anhydrous liquid material, although it may be in the vapor phase or in aqueous form.
- the temperature used in the treatment may vary from about atmospheric temperature to around 400 F., advantageously above 200 F., and the pressure used should advantageously be such as to keep the anhydrous fiuorosulfonic acid liquid at the temperature selected.
- the operation may be carried out batch-wise by thoroughly mixing the oil with the fluorosulionic acid and permitting the batch to settle, separating the oil from the acid and metal salts by decantation, flashing off the hydrogen chloride if desired, and using the recovered fluorosulfonic acid from another batch until it is exhausted.
- the operation may also be carried out continuously as by passing the oil and the fluorosulfonic acid to a continuous mixer such as a time tank provided with an agitator or a contacter of the type used for cold acid treating and alkylation, consisting of a vertical vessel with an open inner cylinder with a circulating pump at its bottom such that the liquid in the vessel is circulated downwardly through the inner cylinder and upwardly through the annulus between the inner cylinder and the wall of the vessel thus affording intimate admixture of immiscible liquids or liquid and gas.
- a continuous mixer such as a time tank provided with an agitator or a contacter of the type used for cold acid treating and alkylation, consisting of a vertical vessel with an open inner cylinder with a circulating pump at its bottom such that the liquid in the vessel is circulated downwardly through the inner cylinder and upwardly through the annulus between the inner cylinder and the wall of the vessel thus affording intimate admixture of immiscible liquids or liquid and gas.
- suitable separators such
- I 0 represents a time tank provided with agitating means.
- the oil to be treated is introduced through the inlet l2 and fluorosulfonic acid throughthe inlet M.
- the flu orosulfcnic acid and the oil are brought into intimate contact in the time tank, with such metal quantitatively, iiijadequate I compounds as there are in the oil being converted to the corresponding fluorosulfonates.
- the treated oil, in admixture with the acid and salt flows out of the outlet I6 to the settle l8, where the oil separates from the acid and the salts, and is removed by the line 20.
- the fluorosulfonic acid and fluorosulfonates, with the hydrogen chloride formed, are removed from the bottom of the settler l8 by the conduit 22 to the flash chamber 23, in which the hydrogen chloride is flashed oif and then supplied to the evaporating chamber 24 in which the fluorosulfonic acid is taken as an overhead product, condensed in the condenser 26 and recycled.
- hydrogen chloride or a part of it may be carried away with the fiuorosulionic acid and recycled, in which case a bleed 25 is provided.
- the operation is carried out at a temperature of about 200 F.
- the improvement which comprises jsubjecting the crude petroleum oils in the pretreatin'g operation and prior to bringing theoil into contact with the cracking "catalyst into intimate admixture with fluorosulfonic acid whereby the metal compounds initially present in the crude petroleum oils react with the fiuorosulfonlc acid to form the corresponding fluorosulfonates, and separating the resulting fiuorosulfonates from the oil.
- the im-' provement consisting of admixing fluorosulfonic acid with the crude petroleum oil during the pretreating operation in an amount substantially in excess of that required to react with the meta compounds present in the oil.
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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)
Description
Sept. 23, 1952 E. A. cooNs 2,611,735
PROCESS FOR REMOVING METALS FROM CRUDE PETROLEUM OILS Filed June 21, 1947 MAKE UP ACID I2 I4 A, on. ACID TM TA I E NK HCL. l0 a I6 FLASH CHAMBER CONDENSER SETTLER 24 EVAPORATOR 22 SALTS INVENTOR EDWARD ADAMSON COONS BY l m, %mda,7nofin%maw J ATTORNEYS Patented Sept. 23, 1952 Edward Adams on' Coons, Chicago, Ill., assignor "to Sinclair Refining Com acorporation 'of Maine H, Application June 21, 1947, SerialNoQ 3 Claims. (o1. 196-39 This invention relates to improvements in the production of motor fuels from crude petroleum oil by catalytic cracking. In catalytic'cracking operations, as heretofore carried out, it has in most cases been necessary to use gas oil or other distillate as the charging stock. One important factor which has prevented theuse of reduced or top crude oils, with or without deasphalting, is that with the use of suchfe ed stocks the catalystrapidly. deteriorates. Most topped orreduced crude oils contain substantial amounts of inorganic salts, in particular sodium, calcium, and magnesium chloride, and in many cases other metallic compounds such as compounds of vanadium and nickel, the natureof which have not been fully established, and compounds of other metals. These metallic compounds are corrosive and probably responsible for the catalyst deterioration which is experienced when reduced or topped crudes are used as charging stocks to eatalytic cracking operations. The economic difference between the use of such materials as gasoil and reduced crude oil as charging stocks for cracking operations is substantial; and the present invention provides improvements which permit the use of the reduced crude oil as charging stock for catalytic cracking operations.
In accordance with the present invention, the crude oil, before or after topping or deasphalting, is treated with fiuorosulfonic acid under appropriate conditions of temperature and prespany, New York, N. v I,
idly and substantially contact isprovided.
The amountof fiuorosulfoniclacid requiredjior the removal of metal contaminants from the oil is slightly in excess "of one equivalent of 'fiuoro sulfonic acid for each equivalent of metal; and with most reduced or topped crude oils, this corresponds to a fraction of 1% of fluorosulfonic acid basedon the oil. Becausejdiflicultiesimay'been: countered in brin ing. about intimate contact of the oil with this small amount of fluorosulfonic acid, it is usually'adyantageous .toruse. a some what larger. amount, for example; 3 to5 'o'ifiluo rosulfonic acid based 'onfthe foil, recover the "ex. cess acid and recycle it until it i' s'icon'sumed. As the fiuorosulfonic' acid reactswithTthe/mtal compounds, it forms a substantially equivalent quantity of hydrogen chloride, which may be permitted to remain in the recycle stream or may be flashed off if it is desired. Retaining it in the recycle stream gives the stream an approximately constant bulb without interfering with the chemical efficiency of the reaction.
sure, with conversion of the metals present into the corresponding fiuorosulfonates substantially quantitatively. The resulting fiuorosulfonates are readily separated from the oil by filtration, settling, centrifuging or the like, and the resulting crude oil, substantially free from metal contaminants, is useful as such as the charging stock for catalytic cracking operations. The use of this as charging stock as compared with gas oil or the like results in substantial economic benefits.
The fluorosulfonic acid may be brought into contact with the metal-contaminated oil in any suitable way. Advantageously, the fluorosulfonic acid is used as the anhydrous liquid material, although it may be in the vapor phase or in aqueous form. The temperature used in the treatment may vary from about atmospheric temperature to around 400 F., advantageously above 200 F., and the pressure used should advantageously be such as to keep the anhydrous fiuorosulfonic acid liquid at the temperature selected. What is required is adequate intimate contact of the fluorosulfonic acid with the oil, because the reaction forming the metal fluorosulfonates proceeds rap- The operation may be carried out batch-wise by thoroughly mixing the oil with the fluorosulionic acid and permitting the batch to settle, separating the oil from the acid and metal salts by decantation, flashing off the hydrogen chloride if desired, and using the recovered fluorosulfonic acid from another batch until it is exhausted.
The operation may also be carried out continuously as by passing the oil and the fluorosulfonic acid to a continuous mixer such as a time tank provided with an agitator or a contacter of the type used for cold acid treating and alkylation, consisting of a vertical vessel with an open inner cylinder with a circulating pump at its bottom such that the liquid in the vessel is circulated downwardly through the inner cylinder and upwardly through the annulus between the inner cylinder and the wall of the vessel thus affording intimate admixture of immiscible liquids or liquid and gas. The eflluent mixture of oil, acid, and metal fiuorosulfonates is passed to suitable separators such as settlers, centrifuges, filters or the like to separate the oil from the acid and salt.
Apparatus suitable for such an operation is illustrated diagrammatically in the appended drawing. In the drawing, I 0 represents a time tank provided with agitating means. The oil to be treated is introduced through the inlet l2 and fluorosulfonic acid throughthe inlet M. The flu orosulfcnic acid and the oil are brought into intimate contact in the time tank, with such metal quantitatively, iiijadequate I compounds as there are in the oil being converted to the corresponding fluorosulfonates. The treated oil, in admixture with the acid and salt flows out of the outlet I6 to the settle l8, where the oil separates from the acid and the salts, and is removed by the line 20. The fluorosulfonic acid and fluorosulfonates, with the hydrogen chloride formed, are removed from the bottom of the settler l8 by the conduit 22 to the flash chamber 23, in which the hydrogen chloride is flashed oif and then supplied to the evaporating chamber 24 in which the fluorosulfonic acid is taken as an overhead product, condensed in the condenser 26 and recycled. If desired, hydrogen chloride or a part of it, may be carried away with the fiuorosulionic acid and recycled, in which case a bleed 25 is provided. Make up fiuoro'sulfonic a'cidis supplied to the line 30. Advantageously the operation is carried out at a temperature of about 200 F. Pressure is not required unless hydrogen chloride is recycled, in which case pressure is used to prevent its vaporization. The quantity'of circulatin'g fiuorosulfonic acid or a mixture of fluorosulfonic acid and hydrogen chloride is a few per cent by volume based on the oil, for example, 3 to I claim:
l. In aprocess involving pretreatment of crude petroleum oils containing metal compounds and subsequent use of the pretreated crude petroleum oils as a charging stock in a'catalytic cracking opei'ation, the improvement which comprises jsubjecting the crude petroleum oils in the pretreatin'g operation and prior to bringing theoil into contact with the cracking "catalyst into intimate admixture with fluorosulfonic acid whereby the metal compounds initially present in the crude petroleum oils react with the fiuorosulfonlc acid to form the corresponding fluorosulfonates, and separating the resulting fiuorosulfonates from the oil.
2. In a process as defined in claim 1 the improvement consisting of conducting the -pretreat ing operation by admixing anhydrous liquid fluorosulfonic acid with the crude petroleum oils un der a superatmospheric pressure sufficient to maintain the fluorosulfonic acid in liquid phase.
3. In a process as defined in claim 1 the im-' provement consisting of admixing fluorosulfonic acid with the crude petroleum oil during the pretreating operation in an amount substantially in excess of that required to react with the meta compounds present in the oil.
EDWARD ADAMSON COONS.
REFERENCES CITED The following references are of record inthei file of'this pate'nt:'
- UNITED STATES PATENTS Number Name Date 1,833,331 Park Nov. 24, 1931 1,984,903 Wagner Dec.'18,'l934 2,203,470 Pier et a1. June', 1940 2,206,500 Q Fischer etal. July 2,1940 2,428,753 Linn Oct. 7,1947 2,450,588 Evering et al Oct. 5,1948
FOREIGN PATENTS Number Country Date 309,042 Great Britain Sept. 3,1930
Claims (1)
1. IN A PROCESS INVOLVING PRETREATMENT OF CRUDE PETROLEUM OILS CONTAINING METAL COMPOUNDS AND SUBSEQUENT USE OF THE PRETREATED CRUDE PETROLEUM OILS AS A CHARGING STOCK IN A CATALYTIC CRACKING OPERATION, THE IMPROVEMENT WHICH COMPRISES SUBJECTING THE CRUDE PETROLEUM OILS IN THE PRETREATING OPERATION AND PRIOR TO BRINGING THE OIL INTO CONTACT WITH THE CRACKING CATALYST INTO INTIMATE ADMIXTURE WITH FLUOROSULFONIC ACID WHEREBY THE
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US756283A US2611735A (en) | 1947-06-21 | 1947-06-21 | Process for removing metals from crude petroleum oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US756283A US2611735A (en) | 1947-06-21 | 1947-06-21 | Process for removing metals from crude petroleum oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2611735A true US2611735A (en) | 1952-09-23 |
Family
ID=25042798
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US756283A Expired - Lifetime US2611735A (en) | 1947-06-21 | 1947-06-21 | Process for removing metals from crude petroleum oils |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2611735A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2778777A (en) * | 1954-02-16 | 1957-01-22 | Texas Co | Removal of metal components from petroleum oils |
| US2891004A (en) * | 1955-10-19 | 1959-06-16 | Exxon Research Engineering Co | Process for removal of metal contaminants from high boiling oils by use of boron compounds |
| US2902430A (en) * | 1955-02-21 | 1959-09-01 | Exxon Research Engineering Co | Removal of metal contaminants from catalytic cracking feed stocks with sulfuric acid |
| US2919245A (en) * | 1956-09-04 | 1959-12-29 | Kerr Mc Gee Oil Ind Inc | Treatment of organic materials |
| US2941939A (en) * | 1956-03-07 | 1960-06-21 | Shiah Chyn Duog | Removal of metallic impurities from light hydrocarbon oils with boron trifluoride coordination compounds |
| US3095368A (en) * | 1957-07-31 | 1963-06-25 | Exxon Research Engineering Co | Process for removing metallic contaminants from oils |
| DE1181847B (en) * | 1957-07-31 | 1964-11-19 | Exxon Research Engineering Co | Process for the removal of non-volatile metal-containing impurities from high-boiling petroleum fractions |
| US3322664A (en) * | 1964-06-26 | 1967-05-30 | Chevron Res | Method of removing calcium sulfate from a hydrocarbon feed stock |
| US20090221417A1 (en) * | 2007-06-05 | 2009-09-03 | Alex Magdics | Catalyst slurry recycle |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB309042A (en) * | 1928-04-03 | 1930-09-03 | Oranienburger Chem Fab Ag | Improved process of refining mineral oils, brown coal tar oils, tars, waxes or the like |
| US1833331A (en) * | 1929-12-10 | 1931-11-24 | Ici Ltd | Purification of synthetic alcohols |
| US1984903A (en) * | 1933-01-16 | 1934-12-18 | Pure Oil Co | Process for removing salt compounds from crude oil |
| US2203470A (en) * | 1936-07-29 | 1940-06-04 | Ig Farbenindustrie Ag | Cracking hydrocarbon mixtures |
| US2206500A (en) * | 1936-08-01 | 1940-07-02 | Hydrocarbon Synthesis Corp | Process for preparing solid paraffins |
| US2428753A (en) * | 1945-09-28 | 1947-10-07 | Universal Oil Prod Co | Process for treating a hydrocarbon mixture which is contaminated by small amounts oforganic fluorine compounds |
| US2450588A (en) * | 1945-05-19 | 1948-10-05 | Standard Oil Co | Desulfurization of oils |
-
1947
- 1947-06-21 US US756283A patent/US2611735A/en not_active Expired - Lifetime
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB309042A (en) * | 1928-04-03 | 1930-09-03 | Oranienburger Chem Fab Ag | Improved process of refining mineral oils, brown coal tar oils, tars, waxes or the like |
| US1833331A (en) * | 1929-12-10 | 1931-11-24 | Ici Ltd | Purification of synthetic alcohols |
| US1984903A (en) * | 1933-01-16 | 1934-12-18 | Pure Oil Co | Process for removing salt compounds from crude oil |
| US2203470A (en) * | 1936-07-29 | 1940-06-04 | Ig Farbenindustrie Ag | Cracking hydrocarbon mixtures |
| US2206500A (en) * | 1936-08-01 | 1940-07-02 | Hydrocarbon Synthesis Corp | Process for preparing solid paraffins |
| US2450588A (en) * | 1945-05-19 | 1948-10-05 | Standard Oil Co | Desulfurization of oils |
| US2428753A (en) * | 1945-09-28 | 1947-10-07 | Universal Oil Prod Co | Process for treating a hydrocarbon mixture which is contaminated by small amounts oforganic fluorine compounds |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2778777A (en) * | 1954-02-16 | 1957-01-22 | Texas Co | Removal of metal components from petroleum oils |
| US2902430A (en) * | 1955-02-21 | 1959-09-01 | Exxon Research Engineering Co | Removal of metal contaminants from catalytic cracking feed stocks with sulfuric acid |
| US2891004A (en) * | 1955-10-19 | 1959-06-16 | Exxon Research Engineering Co | Process for removal of metal contaminants from high boiling oils by use of boron compounds |
| US2941939A (en) * | 1956-03-07 | 1960-06-21 | Shiah Chyn Duog | Removal of metallic impurities from light hydrocarbon oils with boron trifluoride coordination compounds |
| US2919245A (en) * | 1956-09-04 | 1959-12-29 | Kerr Mc Gee Oil Ind Inc | Treatment of organic materials |
| US3095368A (en) * | 1957-07-31 | 1963-06-25 | Exxon Research Engineering Co | Process for removing metallic contaminants from oils |
| DE1181847B (en) * | 1957-07-31 | 1964-11-19 | Exxon Research Engineering Co | Process for the removal of non-volatile metal-containing impurities from high-boiling petroleum fractions |
| US3322664A (en) * | 1964-06-26 | 1967-05-30 | Chevron Res | Method of removing calcium sulfate from a hydrocarbon feed stock |
| US20090221417A1 (en) * | 2007-06-05 | 2009-09-03 | Alex Magdics | Catalyst slurry recycle |
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