US3898299A
Expired / Lapsed
US
⏱️ 0.0 years remaining
Production of gaseous olefins from petroleum residue feedstocks
Assignee: BP Chemicals Ltd
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Filing: 1973-11-02
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Granted: 1975-08-05
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Expires: 1993-11-02
Abstract
Abstract Normally gaseous olefins are produced from an atmospheric petroleum residue feedstock by: A. CONTACTING THE FEEDSTOCK IN A HYDROGENATION ZONE WITH A HYDROGENATION CATALYST, OF WHICH NICKEL/TUNGSTEN/SILICA/ALUMINA AND COBALT/MOLYBDENUM/ALUMINA ARE MOST SUITABLE, UNDER CONDITIONS WHICH EFFECT HYDROGENATION OF AROMATIC HYDROCARBONS. Typical conditions are a temperature in the range 50* to 500*C, a pressure in the range 50 to 500 psig, and an LHSV of 0.1 to 5.0 with a hydrogen feed rate of 5 to 10 times the molar feed rate of the feedstock. B. SEPARATING FROM THE HYDROGENATED FEEDSTOCK A GASEOUS PHASE CONTAINING HYDROGEN AND A LIQUID PHASE CONTAINING HYDROCARBONS. C. RECYCLING AT LEAST A PORTION OF SAID GASEOUS PHASE CONTAINING HYDROGEN TO SAID HYDROGENATION ZONE. D. SEPARATING THE LIQUID PHASE FROM (C) INTO A DISTILLATE FRACTION HAVING A BOILING RANGE BELOW 650*C and a residue fraction having a higher boiling range, advantageously by vacuum distillation. E. SUBJECTING THE DISTILLATE FRACTION FROM (D) TO THERMAL CRACKING IN THE PRESENCE OF STEAM THEREBY CONVERTING AT LEAST A PORTION OF THE LIQUID PHASE TO NORMALLY GASEOUS HYDROCARBONS AND F. RECOVERING THE NORMALLY GASEOUS OLEFINS FROM THE PYROLYSIS ZONE EFFLUENT.
Inventors
- 👤 John Robert Jones
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-27 11:18
CPC Classifications
C; C10; C10G; C10G45/00; C10G45/44; C10G2400/00; C10G2400/20
Claims Analysis
Total Claims: 11
Claim 1
Independent Claim
216 words
A PROCESS FOR THE PRODUCTION OF NORMALLY GASEOUS OLEFINS FROM AN ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK WHICH PROCESS COMPRISES THE STEPS OF: A. CONTACTING THE PETROLEUM RESIDUE FEEDSTOCK IN A HYDROGENATION ZONE WITH A HYDROGENATION CATALYST SELECTED FROM NICKEL/MOLYBDENUM/ALUMINA, COBALT/TUNGSTEN/ALUMINA, NICLEL/TUNGSTEN/ALUMINA, COBALT/MOLYBEDENUM/ALUMINA, NICKLE/COBALT/MOLYBDENUM/ALUMINA, COBALT/MOLYBDENUM/SILICA/ALUMINA, NICLEL/MOLYBDENUM/SILICA/ALUMINA, NICKEL/TUNGSTEN/SILICA/ALUMINA AND HYDROGEN AT A TEMPERATURE IN THE RANGE 50* TO 500*C, A PRESSURE IN THE RANGE 50 TO 5,000 PSIG, A LIQUID HOURLY SPACE VELOCITY IN THE RANGE 0.1 TO 5.0, AND A HYDROGEN FEED RATE OF 5 TO 10 TIMES THE MOLAR FEED RATE OF THE ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK, TO EFFECT HYDROGENATION OF AROMATIC HYDROCARBONS, B. SEPARATING FROM THE RESULTING HYDROGENATED ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK A GASEOUS PHASE CONTAINING HYDROGEN AND A LIQUID PHASE CONTAINING HYDROCARBONS, C. RECYCLING AT LEAST A PORTION OF SAID GASEOUS PHASE CONTAINING HYDROGEN TO SAID HYDROGENATION ZONE, D. SPARATING SAID LIQUID PHASE CONTAINING HYDROCARBONS INTO A DISTILLATE FRACTION HAVING A BOILING RANGE BELOW 650*C AND A RESIDUE FRACTION HAVING A BOILING RANGE ABOVE THAT OF THE DISTILLATE FRACTION, E. SUBJECTING SAID DISTILLATE FRACTION IN THE PRESENCE OF STEAM TO THERMAL CRACKING IN A PYROLYSIS ZONE UNDER CONDITIONS EFFECTING CONVERSION OF AT LEAST A PORTION OF SAID LIQUID PHASE TO NORMALLY GASEOUS OLEFILNS AND F. RECOVERING THE NORMALLY GASEOUS OLEFINS FROM THE PYROLYSIS ZONE EFFUENT.
Claim 2
Dependent Claim
216 words
A PROCESS FOR THE PRODUCTION OF NORMALLY GASEOUS OLEFINS FROM AN ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK WHICH PROCESS COMPRISES THE STEPS OF: A. CONTACTING THE PETROLEUM RESIDUE FEEDSTOCK IN A HYDROGENATION ZONE WITH A HYDROGENATION CATALYST SELECTED FROM NICKEL/MOLYBDENUM/ALUMINA, COBALT/TUNGSTEN/ALUMINA, NICLEL/TUNGSTEN/ALUMINA, COBALT/MOLYBEDENUM/ALUMINA, NICKLE/COBALT/MOLYBDENUM/ALUMINA, COBALT/MOLYBDENUM/SILICA/ALUMINA, NICLEL/MOLYBDENUM/SILICA/ALUMINA, NICKEL/TUNGSTEN/SILICA/ALUMINA AND HYDROGEN AT A TEMPERATURE IN THE RANGE 50* TO 500*C, A PRESSURE IN THE RANGE 50 TO 5,000 PSIG, A LIQUID HOURLY SPACE VELOCITY IN THE RANGE 0.1 TO 5.0, AND A HYDROGEN FEED RATE OF 5 TO 10 TIMES THE MOLAR FEED RATE OF THE ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK, TO EFFECT HYDROGENATION OF AROMATIC HYDROCARBONS, B. SEPARATING FROM THE RESULTING HYDROGENATED ATMOSPHERIC PETROLEUM RESIDUE FEEDSTOCK A GASEOUS PHASE CONTAINING HYDROGEN AND A LIQUID PHASE CONTAINING HYDROCARBONS, C. RECYCLING AT LEAST A PORTION OF SAID GASEOUS PHASE CONTAINING HYDROGEN TO SAID HYDROGENATION ZONE, D. SPARATING SAID LIQUID PHASE CONTAINING HYDROCARBONS INTO A DISTILLATE FRACTION HAVING A BOILING RANGE BELOW 650*C AND A RESIDUE FRACTION HAVING A BOILING RANGE ABOVE THAT OF THE DISTILLATE FRACTION, E. SUBJECTING SAID DISTILLATE FRACTION IN THE PRESENCE OF STEAM TO THERMAL CRACKING IN A PYROLYSIS ZONE UNDER CONDITIONS EFFECTING CONVERSION OF AT LEAST A PORTION OF SAID LIQUID PHASE TO NORMALLY GASEOUS OLEFILNS AND F. RECOVERING THE NORMALLY GASEOUS OLEFINS FROM THE PYROLYSIS ZONE EFFUENT.
Claim 3
Dependent Claim
70 words
A process according to claim 1 wherein the whole of said liquid phase containing hydrocarbons is, after separation of a gaseous phase containing hydrogen, fed in the presence of steam directly to the pyrolysis zone wherein unvapourised feedstock is removed as a residue fraction in a separation zone prior to entry of the vapourised distillate fraction into that region of the pyrolysis zone maintained under conditions which effect thermal cracking.
Claim 4
Dependent Claim
44 words
A process according to claim 1 wherein the separation of said liquid phase containing hydrocarbons into a distillate fraction having a boiling range below 650*C and a residue fraction having a boiling range above that of the distillate fraction is effected by vacuum distillation.
Claim 5
Dependent Claim
12 words
A process according to claim 1 wherein said hydrogenation catalyst is nickel/tungsten/silica/alumina.
Claim 6
Dependent Claim
12 words
A process according to claim 1 wherein said hydrogenation catalyst is cobalt/molybdenum/alumina.
Claim 7
Dependent Claim
43 words
A process according to claim 1 wherein said hydrogenation catalyst is activated before use in the hydrogenation reaction by contact with a stream of hydrogen at a temperature in the range 100* to 800*C for a period of 1 minute to 24 hours.
Claim 8
Dependent Claim
40 words
A process according to claim 1 wherein the temperature is in the range 300* to 600*C, the pressure is in the range 200 to 3, 000 psig and the Liquid Hourly Space Velocity is in the range 0.1 to 0.5.
Claim 9
Dependent Claim
46 words
A process according to claim 1 wherein the major portion of the gaseous phase containing hydrogen is separated from the liquid phase containing hydrocarbons in a high pressure separator and recycled either directly or, after scrubbing to remove hydrogen sulphide and ammonia, to the hydrogenation zone.
Claim 10
Dependent Claim
26 words
A process according to claim 1 wherein the hydrogenation zone is a single zone or a series of zones employing the same or different hydrogenation catalyst.
Claim 11
Dependent Claim
57 words
A process according to claim 1 wherein thermal cracking of the distillate fraction in the presence of steam is effected at a steam to hydrocarbon weight ratio of 0.5:1 to 2.0:1 in a heated zone at a maximum temperature in the range 700* to 1,000*C with a residence time in this range between 0.01 and 5 seconds.
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USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1978-08-04 | 1979-02-03 | 1979-08-05 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1982-08-04 | 1983-02-03 | 1983-08-05 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1986-08-04 | 1987-02-03 | 1987-08-05 | $7700.00 | Window Closed / Lapsed |