US4010093A
Expired / Lapsed
US
⏱️ 0.0 years remaining
Method of operating a platinum reformer comprising a selective zeolite catalyst in third reactor
Assignee: Mobil Oil AS
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Filing: 1975-02-04
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Granted: 1977-03-01
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Expires: 1995-02-04
Abstract
Abstract A reforming operation is described which incorporates a zeolite selective conversion catalyst as a final catalyst composition contacted under temperature conditions controlled by quench gas as a function of product and seasonal demands. Preferably the zeolite catalyst is included as a separate downstream bed of catalyst in an enlarged final reactor of a three reactor reforming operation.
Inventors
- 👤 John Maziuk
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-04 12:21
CPC Classifications
C; C10; C10G; C10G35/00; C10G35/04; C10G35/06; C10G35/095; C10G59/00; C10G59/02
Claims Analysis
Total Claims: 10
Claim 1
Independent Claim
187 words
In a processing combination comprising a bed of crystalline zeolite conversion catalyst downstream of a plurality of separate sequentially arranged beds of naphtha reforming catalyst, the method for altering the product distribution obtained from the combination processing naphtha boiling material in the presence of hydrogen rich gas which comprises: promoting the formation of gasoline boiling range material of higher octane rating than the naphtha charged to the combination process by operating the catalytic reforming portion under reduced recycled hydrogen partial pressure to promote dehydrogenation and the formation of gasoline boiling products in combination with relying upon a major portion of recycle hydrogen rich gas as quench fluid to reduce the temperature of the effluent obtained from catalytic reforming below about 650° F. before contacting the zeolite conversion catalyst and promoting the formation of LPG and aromatic rich concentrates with the catalytic combination by raising the hydrogen partial pressure of the catalytic reforming operation with hydrogen rich recycle gas sufficient to promote hydrocracking during reforming in combination with reducing the hydrogen gas quench fluid to raise the temperature of the effluent of reforming to at least 650° F.
Claim 2
Dependent Claim
187 words
In a processing combination comprising a bed of crystalline zeolite conversion catalyst downstream of a plurality of separate sequentially arranged beds of naphtha reforming catalyst, the method for altering the product distribution obtained from the combination processing naphtha boiling material in the presence of hydrogen rich gas which comprises: promoting the formation of gasoline boiling range material of higher octane rating than the naphtha charged to the combination process by operating the catalytic reforming portion under reduced recycled hydrogen partial pressure to promote dehydrogenation and the formation of gasoline boiling products in combination with relying upon a major portion of recycle hydrogen rich gas as quench fluid to reduce the temperature of the effluent obtained from catalytic reforming below about 650° F. before contacting the zeolite conversion catalyst and promoting the formation of LPG and aromatic rich concentrates with the catalytic combination by raising the hydrogen partial pressure of the catalytic reforming operation with hydrogen rich recycle gas sufficient to promote hydrocracking during reforming in combination with reducing the hydrogen gas quench fluid to raise the temperature of the effluent of reforming to at least 650° F.
Claim 3
Dependent Claim
33 words
The method of claim 1 wherein quenching of the reforming effluent is restricted to maintain a temperature within the range of 650° F. to about 850° F. during contact with the zeolite catalyst.
Claim 4
Dependent Claim
37 words
The method of claim 1 wherein a multi-metallic reforming catalyst is employed in the catalytic reforming operation at a temperature selected from within the range of 800° F. to 1000° F. at a pressure below 700 psig.
Claim 5
Dependent Claim
46 words
The method of claim 1 wherein the distribution of hydrogen rich gas recycled to the catalytic reforming operation and as quench fluid is adjusted to reduce the aging rate of the crystalline zeolite catalyst to an interval commensurate with the aging rate of the reforming catalyst.
Claim 6
Dependent Claim
36 words
The method of claim 1 wherein the crystalline zeolite conversion catalyst may be one of the group of selective relatively small pore crystalline zeolites identifiable with erionite type zeolites and the family of ZSM-5 crystalline zeolites.
Claim 7
Dependent Claim
43 words
The method of claim 1 wherein the selective zeolite conversion catalyst is maintained at a temperature within the range of 700° F. to 800° F. by recycle hydrogen rich quench gas in admixture with the effluent obtained from a platinum reforming catalyst operation.
Claim 8
Dependent Claim
46 words
The method of claim 1 wherein the crystalline zeolite catalyst material is maintained as a separate bed of catalyst in the last reforming zone of a plurality of sequentially arranged catalytic reforming zones and downstream of a bed of reforming catalyst in said last reforming zone.
Claim 9
Dependent Claim
20 words
The method of claim 1 wherein the crystalline zeolite is a ZSM-5 crystalline zeolite and the reforming catalyst contains platinum.
Claim 10
Dependent Claim
38 words
The method of claim 1 wherein the amount of adjustment of the reforming effluent quench and hydrogen to hydrocarbon ratio maintained during catalytic reforming of naphtha is determined as a function of the yield of desired LPG product.
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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) | 1980-02-29 | 1980-08-30 | 1981-03-01 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1984-02-29 | 1984-08-30 | 1985-03-01 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1988-02-29 | 1988-08-30 | 1989-03-01 | $7700.00 | Window Closed / Lapsed |