US2332562A - Conversion of hydrocarbons - Google Patents
Conversion of hydrocarbons Download PDFInfo
- Publication number
- US2332562A US2332562A US337359A US33735940A US2332562A US 2332562 A US2332562 A US 2332562A US 337359 A US337359 A US 337359A US 33735940 A US33735940 A US 33735940A US 2332562 A US2332562 A US 2332562A
- Authority
- US
- United States
- Prior art keywords
- line
- catalyst
- valve
- conversion
- oil
- 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
- 238000006243 chemical reaction Methods 0.000 title description 19
- 229930195733 hydrocarbon Natural products 0.000 title description 13
- 150000002430 hydrocarbons Chemical class 0.000 title description 12
- 239000003054 catalyst Substances 0.000 description 22
- 239000003921 oil Substances 0.000 description 20
- 238000005336 cracking Methods 0.000 description 14
- 239000007789 gas Substances 0.000 description 13
- 238000010438 heat treatment Methods 0.000 description 12
- 239000000203 mixture Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 7
- 239000007795 chemical reaction product Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- NUMXHEUHHRTBQT-AATRIKPKSA-N 2,4-dimethoxy-1-[(e)-2-nitroethenyl]benzene Chemical compound COC1=CC=C(\C=C\[N+]([O-])=O)C(OC)=C1 NUMXHEUHHRTBQT-AATRIKPKSA-N 0.000 description 1
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 1
- 230000002730 additional effect Effects 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000012084 conversion product Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000011874 heated mixture Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- -1 olefin hydrocarbons Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012254 powdered material Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 239000000725 suspension Substances 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
Definitions
- Thisinvention relates to a process for converting hydrocarbon oil into substantial yields of high antiknock gasoline. More particularly it relates to cracking hydrocarbon distillates in the y presence of a powdered crackingcatalyshur conditions adequate to produce high antiknock gasoline. v
- thepresent invention comprises mixing a hydrocarbon oil with a powdered cracking catalyst, heating the mixture at cracking conditions of temperature and pressure,'s eparately heating recycle oil and/or process gases in the presence of an additional portion of said cracking catalyst, mixing the reactants with those from the first step, adding thereto an additional quantity of powdered cracking catalyst, passing the mixture to a reaction zone followed by a vaporizing zone, recovering gasoline, gasand recycle oil, and returning a portion of .the recycle oil and gas as previously described.
- Catalyst pow- 1 der as such or in the form of a slurry in a part of the charge or,.. a fraction of reaction products or other suitable carrier, is introduced from catalyst charger I through line 8 containing valve 9, 'pump I0, valve II and valve II', mixing with the charging stock in line I; 'The mixture passes from coil 5 through line I2 and valve I3 to reaction chamber I4. An additional quantity of the catalytic agent isintroduced through line I5 containing valve I6.
- reaction products in line I2 are commingled with recycle oil and/or process gases from coil 43 whereby the temperature maybe increased if desired by heating the incoming hydrocarbons to a higher temperature than is used in coil V5.
- colder oil from line 49 may be introduced to regulate the temperature of the combined reactants, when, for example, it is desired to continue ⁇ the conversion in reactor I4 at a lower temperature than in the cracking coils. This permitsgreat ilexigasoline for .use in motor fuelsl or as aviation f bility to the process from an operating-standpoint.
- the reaction mixture from chamber I 4 passes through line II and valve I8 to vaporizing chamber I9. Residual oil containing catalyst in suspension is removed through line and valve 2
- a vapprous fraction is passed through line 22 and valve 2 3 to fractionator 24 from which gasoline and gas ⁇ are removed through line 25, valve 26, condenser -2'I and valve 28 to receiver 29.
- Gasoline is recovered through line and valve 3l, being passed to a suitable stabilizer not shown.
- a portion of the process gases may bc withdrawn through line 32 and valve 33.
- process gases may be further treated by vpolymerization and/or alkylation processes to produce additional yields of gasoline.
- a part of the receiver gases may he passed through line 34 containing valve 35, pump 36 and valve 3l to line 38 wherein they may be commingled with a Llo light recycle oil from line 39 containing valve 40, pump 4I and valve 42.
- the mixture passes through line 38 to coil 43 which isA disposed in heater 44.
- the mixture maybe heated to crack-- ing conditions of temperature and pressure of theorder o f approximately 800-1200 F. and
- the gas alone may be passed through coilY 43 as described andpart or all of the reflux may be passed through-line 49 and v alve 50 to line I2 where it acts as a4 quench and thus serves as a means of decreas-v ing-the temperature of the reaction products to a ⁇ desired point. This may be done when it is desired to bring the temperature within the range of approximately 50o-850 F. under which conditions the fresh catalyst added from line I5 serves togbrin'g about the conversion of oleI-ln hydrocarbons' in the gasoline so that the nnished gasoline may be substantially olen-free.
- catalytic agents employed in the present process are preferably-those known as silicaalumina, silica-zirconia and silica-alumina-zirponia.
- This type of catalytic lagent is prepared by the separate or simultaneous precipitation of the components under conditions such that a powdered material of particle size approaching colloidal dimensions is produced. The material is washed until substantially free of alkali metal ions and may be dried prior to introduction into the system.
- the catalyst may be introduced as a dry powder or as a slurry in a. part of the oil undergoing conversion, or in a part of the reaction products or any other suitable carrying medium.
- the quantity of catalyst used may vary from approximately 0.1-20% by Weight of the oil and is normally within the range of approximately 0.5-% of the oil.
- the catalyst may be recovered and reactivated by treatment with an oxygen-containing gas under conditions such that the carbonaceous and hydrocarbonaceous deposits are burned'.
- the temperature of reactivation should be kept ata point below 1500 F. ⁇ and preferably below 1200 F.
- Ezra'mple I 'A Mid-.Continent gas oil may be, converted in the manner described using a silica-alumina powder employing a temperature in the gas oil conversion step of approximately 1000 F. and atemperature of-1100/ F. in the gas -conversion coil 43. No recycle oil or catalyst is employed in coil A3. Sufficient side cut maybe added to the combined feed'line I2 so that a temperature of approximately 750 F. is maintained in the reaction chamber. Approximately 1% of catalyst by Weight of the charging stock is used, half of .this
- a process for the conversion of hydrocarbon oil which comprises adding fresh powdered siliceous cracking catalyst to said oil,passingthe mixture in a confined stream through a heating zone and therein heating the same to a cracking temperature, commingling additional fresh powdered siliceous cracking catalyst with the stream of reaction products leaving said heating zone, supplying the resulting mixture to a reaction zone and therein continuing the conversion, separating cracked vaporous and non-vaporous residue containing the powdered catalyst from the resultant conversion products, fractionating said cracked vapors to separate therefrom as reux condensate fractions higher 'boiling than gasoline, cooling and condensing the fractionated vapors, separating normally gaseous materials from the resulting distillate, adding additional fresh powdered catalyst to at least a portion of the normally gaseous materials, heating the mixture of gases and catalyst to conversion temperature and introducing the heated mixture into said reaction zone.
- a process for the conversion of hydrocarbon oil which comprises adding a fresh powdered -siliceous cracking catalyst to said hydrocarbon oil, passingl the mixture in a confined stream through a heating zene and therein heating the same to a cracking temperature, commingling additional fresh powdered siliceous cracking catalyst with the stream of reaction products leaving said heating zone, supplying the resulting mixture to a reaction chamber and therein maintaining the same at cracking temperature, separating non-vaporous liquid residue containing the powdered catalyst.
Landscapes
- 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
Oct. 26, 1943.
t G. lazcaLol-'Fr GONVERS ION OF HYDROCARBON S Filed May 27, 1940 QNNE .Q Y QS.
w .Mn ./NHM
a. ha QN.
Patented Oct. .26,I 1 943 f UNITED sm'rssl PATENT OFFICE Gustav Egloff, Chicago, Ill., assignor-to Universal Oil Products Company, Chicago, Ill., a corporation of Delaware I Application May 27, 1940, Serial No. 337,359
- r 2 Claims. (Cl. 196-52) Thisinvention relates to a process for converting hydrocarbon oil into substantial yields of high antiknock gasoline. More particularly it relates to cracking hydrocarbon distillates in the y presence of a powdered crackingcatalystunder conditions adequate to produce high antiknock gasoline. v
In one'specific embodiment thepresent invention comprises mixing a hydrocarbon oil with a powdered cracking catalyst, heating the mixture at cracking conditions of temperature and pressure,'s eparately heating recycle oil and/or process gases in the presence of an additional portion of said cracking catalyst, mixing the reactants with those from the first step, adding thereto an additional quantity of powdered cracking catalyst, passing the mixture to a reaction zone followed by a vaporizing zone, recovering gasoline, gasand recycle oil, and returning a portion of .the recycle oil and gas as previously described. f
The invention is further understood by ref4 to 1000 pounds per square inch. Catalyst pow- 1 der as such or in the form of a slurry in a part of the charge or,.. a fraction of reaction products or other suitable carrier, is introduced from catalyst charger I through line 8 containing valve 9, 'pump I0, valve II and valve II', mixing with the charging stock in line I; 'The mixture passes from coil 5 through line I2 and valve I3 to reaction chamber I4. An additional quantity of the catalytic agent isintroduced through line I5 containing valve I6. The reaction products in line I2 are commingled with recycle oil and/or process gases from coil 43 whereby the temperature maybe increased if desired by heating the incoming hydrocarbons to a higher temperature than is used in coil V5. Alternatively, colder oil from line 49 may be introduced to regulate the temperature of the combined reactants, when, for example, it is desired to continue` the conversion in reactor I4 at a lower temperature than in the cracking coils. This permitsgreat ilexigasoline for .use in motor fuelsl or as aviation f bility to the process from an operating-standpoint. The reaction mixture from chamber I 4 passes through line II and valve I8 to vaporizing chamber I9. Residual oil containing catalyst in suspension is removed through line and valve 2|. A vapprous fraction is passed through line 22 and valve 2 3 to fractionator 24 from which gasoline and gas` are removed through line 25, valve 26, condenser -2'I and valve 28 to receiver 29. Gasoline is recovered through line and valve 3l, being passed to a suitable stabilizer not shown. A portion of the process gases may bc withdrawn through line 32 and valve 33. The
process gases may be further treated by vpolymerization and/or alkylation processes to produce additional yields of gasoline. A part of the receiver gases may he passed through line 34 containing valve 35, pump 36 and valve 3l to line 38 wherein they may be commingled with a Llo light recycle oil from line 39 containing valve 40, pump 4I and valve 42. The mixture passes through line 38 to coil 43 which isA disposed in heater 44. The mixture maybe heated to crack-- ing conditions of temperature and pressure of theorder o f approximately 800-1200 F. and
passed through line and valve 46, joining with line I2 .and mixing with the reactants therein as previously described. Alternatively, an additional quantity of catalyst maybe introduced through line 41 and valve 48.
As a further alternative, the gas alone may be passed through coilY 43 as described andpart or all of the reflux may be passed through-line 49 and v alve 50 to line I2 where it acts as a4 quench and thus serves asa means of decreas-v ing-the temperature of the reaction products to a `desired point. This may be done when it is desired to bring the temperature within the range of approximately 50o-850 F. under which conditions the fresh catalyst added from line I5 serves togbrin'g about the conversion of oleI-ln hydrocarbons' in the gasoline so that the nnished gasoline may be substantially olen-free.
yWhen operating in this way, .the temperatures, maintained in coils 5 and 43 are normally in excess of approximately 900 F, whereby an olefincontaining gasoline o f high antiknock value is produced. Higher boiling fractionator bottoms may be withdrawn from fractionator 24 through line 5I and valve 52 to be further cracked or to be used as ,a fuel oil.
'I'he catalytic agents employed in the present processare preferably-those known as silicaalumina, silica-zirconia and silica-alumina-zirponia. This type of catalytic lagent is prepared by the separate or simultaneous precipitation of the components under conditions such that a powdered material of particle size approaching colloidal dimensions is produced. The material is washed until substantially free of alkali metal ions and may be dried prior to introduction into the system. The catalyst may be introduced as a dry powder or as a slurry in a. part of the oil undergoing conversion, or in a part of the reaction products or any other suitable carrying medium. The quantity of catalyst used may vary from approximately 0.1-20% by Weight of the oil and is normally within the range of approximately 0.5-% of the oil. The catalyst may be recovered and reactivated by treatment with an oxygen-containing gas under conditions such that the carbonaceous and hydrocarbonaceous deposits are burned'. The temperature of reactivation should be kept ata point below 1500 F. `and preferably below 1200 F.
The following examples are given to illustrate the practicability of the invention but should not be construed as limiting it to the exact conditions given therein.
Ezra'mple I 'A Mid-.Continent gas oil may be, converted in the manner described using a silica-alumina powder employing a temperature in the gas oil conversion step of approximately 1000 F. and atemperature of-1100/ F. in the gas -conversion coil 43. No recycle oil or catalyst is employed in coil A3. Sufficient side cut maybe added to the combined feed'line I2 so that a temperature of approximately 750 F. is maintained in the reaction chamber. Approximately 1% of catalyst by Weight of the charging stock is used, half of .this
being introduced' into the combined feed line by way of line I5. A total yield of approximately 68% of '78 octane number gasoline substantially free of olefin hydrocarbons may be obtained in this manner.
' Example II to 7 pounds Reid vapor pressure andpolymerizing the olens in the stabilizer gases, an addi tional quantity of gasoline of 83 octane number may be obtained.
I claim as my invention:
1. A process for the conversion of hydrocarbon oil which comprises adding fresh powdered siliceous cracking catalyst to said oil,passingthe mixture in a confined stream through a heating zone and therein heating the same to a cracking temperature, commingling additional fresh powdered siliceous cracking catalyst with the stream of reaction products leaving said heating zone, supplying the resulting mixture to a reaction zone and therein continuing the conversion, separating cracked vaporous and non-vaporous residue containing the powdered catalyst from the resultant conversion products, fractionating said cracked vapors to separate therefrom as reux condensate fractions higher 'boiling than gasoline, cooling and condensing the fractionated vapors, separating normally gaseous materials from the resulting distillate, adding additional fresh powdered catalyst to at least a portion of the normally gaseous materials, heating the mixture of gases and catalyst to conversion temperature and introducing the heated mixture into said reaction zone.
2. A process for the conversion of hydrocarbon oil, which comprises adding a fresh powdered -siliceous cracking catalyst to said hydrocarbon oil, passingl the mixture in a confined stream through a heating zene and therein heating the same to a cracking temperature, commingling additional fresh powdered siliceous cracking catalyst with the stream of reaction products leaving said heating zone, supplying the resulting mixture to a reaction chamber and therein maintaining the same at cracking temperature, separating non-vaporous liquid residue containing the powdered catalyst. from cracked vapors, fractionating the cracked vapors to separate as reflux condensate fractions higher boiling than gasoline, separately heating said reflux condensate to a conversion temperature and subjecting the same to further conversion in said reaction chamber, cooling and condensing the fractionatedl vapors, separating normally gaseous hydrocarbons from distillate, combining fresh catalyst with said normally gaseous hydrocarbons and subjecting thel mixture to heating with said reflux condensate. GUSTAV EGLOFF.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US337359A US2332562A (en) | 1940-05-27 | 1940-05-27 | Conversion of hydrocarbons |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US337359A US2332562A (en) | 1940-05-27 | 1940-05-27 | Conversion of hydrocarbons |
Publications (1)
Publication Number | Publication Date |
---|---|
US2332562A true US2332562A (en) | 1943-10-26 |
Family
ID=23320247
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US337359A Expired - Lifetime US2332562A (en) | 1940-05-27 | 1940-05-27 | Conversion of hydrocarbons |
Country Status (1)
Country | Link |
---|---|
US (1) | US2332562A (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2432277A (en) * | 1945-01-02 | 1947-12-09 | Shell Dev | Catalytic cracking of hydrocarbon oils |
US2470263A (en) * | 1946-07-27 | 1949-05-17 | Shell Dev | Hydrocarbon conversion process |
US2568967A (en) * | 1946-04-15 | 1951-09-25 | Gulf Research Development Co | Cracking process |
-
1940
- 1940-05-27 US US337359A patent/US2332562A/en not_active Expired - Lifetime
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2432277A (en) * | 1945-01-02 | 1947-12-09 | Shell Dev | Catalytic cracking of hydrocarbon oils |
US2568967A (en) * | 1946-04-15 | 1951-09-25 | Gulf Research Development Co | Cracking process |
US2470263A (en) * | 1946-07-27 | 1949-05-17 | Shell Dev | Hydrocarbon conversion process |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US2358888A (en) | Catalytic conversion of hydrocarbons | |
US2360622A (en) | Method of producing aviation gasoline | |
US2353731A (en) | Hydrocarbon conversion | |
US2283854A (en) | Conversion of hydrocarbon oils | |
US2270071A (en) | Hydrocarbon conversion | |
US2235133A (en) | Hydrocarbon conversion | |
US2297773A (en) | Hydrocarbon conversion | |
US2332562A (en) | Conversion of hydrocarbons | |
US2287940A (en) | Hydrocarbon conversion | |
US2319710A (en) | Catalytic cracking process | |
US2521757A (en) | Conversion of heavy hydrocarbon materials | |
US2286447A (en) | Catalytic conversion of hydrocarbon oils | |
US2328773A (en) | Catalytic conversion of hydrocarbons | |
US2428532A (en) | Catalytic hydrocarbon conversion process in the presence of steam | |
US2333625A (en) | Conversion of hydrocarbon oils | |
US2420904A (en) | Conversion of hydrocarbons | |
US2327510A (en) | Conversion of hydrocarbon oils | |
US2374095A (en) | Process for the catalytic treatment of hydrocarbons | |
US1955268A (en) | Process for preparing low boiling hydrocarbons from higher boiling hydrocarbons | |
US2236083A (en) | Catalytic conversion of hydrocarbon oils | |
US2343649A (en) | Conversion of hydrocarbons | |
US2327099A (en) | Conversion of hydrocarbons | |
US2339918A (en) | Hydrocarbon conversion | |
US2294584A (en) | Catalytic treatment of hydrocarbon oils | |
US2345753A (en) | Catalytic conversion of hydrocarbon oils |