Patent US4238631A successfully refreshed from Google Patents.
US4238631A
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Fluid zeolite catalyzed conversion of alcohols and oxygenated derivatives to hydrocarbons by controlling exothermic reaction heat
Assignee: Mobil Oil AS
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Filing: 1979-10-30
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Granted: 1980-12-09
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Expires: 1999-10-30
Abstract
Abstract Alcohols and related oxygenates converted in a riser reactor and dense fluid catalyst bed (ZSM-5 cat) circulated through a plurality of satellite stripping-cooling zones for temperature control. Catalyst utilized comprises from 5 to 20 weight percent coke for activity and selectivity characteristics promoting the formation of olefins and aromatics at temperatures below 800 DEG F.
Inventors
- 👤 Nicholas Daviduk
- 👤 James H. Haddad
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-30 15:40
CPC Classifications
B; B01; B01J; B01J8/00; B01J8/18; B01J8/24; B01J8/26; C; C07; C07C; C07C1/00; C07C1/20; C10; C10G; C10G3/00; C10G3/42; C10G3/44; C10G3/48; C10G3/49; C10G3/54; C10G3/55; C10G3/57; C10G3/60; C10G3/62; C07C2529/00; C07C2529/04; C07C2529/06; C07C2529/40; C07C2529/65; C07C2529/70; C10G2300/00; C10G2300/40; C10G2300/4006; C10G2300/4093; C10G2300/70; C10G2300/708; C10G2400/00; C10G2400/02; C10G2400/28; C10G2400/30; Y; Y02; Y02P; Y02P30/00; Y02P30/20
Claims Analysis
Total Claims: 13
Claim 1
Independent Claim
77 words
A method for converting reactants comprising lower alcohols and related oxygenates to C 10 and lower boiling carbon-hydrogen compounds including LPG and gasoline boiling components which comprises: passing a suspension of vaporized reactant material and fluid catalyst particles comprising a special crystallive zeolite represented by ZSM-5 crystallive zeolite upwardly through a relatively dispersed catalyst phase riser contact zone for a time temperature and pressure suitable to achieve at least 70% conversion of methanol in the reactant feed;
Claim 2
Independent Claim
77 words
A method for converting reactants comprising lower alcohols and related oxygenates to C 10 and lower boiling carbon-hydrogen compounds including LPG and gasoline boiling components which comprises: passing a suspension of vaporized reactant material and fluid catalyst particles comprising a special crystallive zeolite represented by ZSM-5 crystallive zeolite upwardly through a relatively dispersed catalyst phase riser contact zone for a time temperature and pressure suitable to achieve at least 70% conversion of methanol in the reactant feed;
Claim 3
Dependent Claim
98 words
passing the suspension comprising products of reaction upwardly through a relatively dense fluid mass of catalyst particles for a residence time and temperature sufficient to achieve a total conversion of methanol in the feed equivalent to at least 90% and produce simultaneously a product mixture of C 1 to C 10 hydrocarbons comprising paraffins, olefins and aromatics; passing catalyst withdrawn from a lower portion of said relatively dense fluid mass of catalyst particles downwardly through a plurality of separate catalyst stripping-cooling zones of desired temperature restriction and thence to the riser reactor for admixture with charged vaporous reactant;
Claim 4
Dependent Claim
98 words
passing the suspension comprising products of reaction upwardly through a relatively dense fluid mass of catalyst particles for a residence time and temperature sufficient to achieve a total conversion of methanol in the feed equivalent to at least 90% and produce simultaneously a product mixture of C 1 to C 10 hydrocarbons comprising paraffins, olefins and aromatics; passing catalyst withdrawn from a lower portion of said relatively dense fluid mass of catalyst particles downwardly through a plurality of separate catalyst stripping-cooling zones of desired temperature restriction and thence to the riser reactor for admixture with charged vaporous reactant;
Claim 5
Dependent Claim
42 words
passing stripped products from the stripping-cooling zone into a dispersed phase of catalyst above said more dense fluid mass of catalyst and withdrawing reaction products separated from catalyst in said dispersed phase of catalyst from an upper portion of said reaction zone.
Claim 6
Dependent Claim
42 words
passing stripped products from the stripping-cooling zone into a dispersed phase of catalyst above said more dense fluid mass of catalyst and withdrawing reaction products separated from catalyst in said dispersed phase of catalyst from an upper portion of said reaction zone.
Claim 7
Dependent Claim
43 words
The method of claim 1 wherein the exothermic temperature rise of said conversion in said riser and said relatively dense fluid mass of catalyst is restricted to maintain a dispersed phase temperature above said dense fluid mass of not more than 800° F.
Claim 8
Dependent Claim
17 words
The method of claim 2 wherein said dispersed phase temperature is restricted not to exceed 765° F.
Claim 9
Dependent Claim
27 words
The method of claim 1 wherein the catalyst to reactant ratio of the initially formed suspension in the riser is within the range of 10-20 to 1.
Claim 10
Dependent Claim
33 words
The method of claim 1 wherein conversion of methanol in the reactant feed is at least 90% in the riser conversion zone before distribution in the relatively dense fluid mass of catalyst thereabove.
Claim 11
Dependent Claim
41 words
The method of claim 1 wherein the relatively dense fluid mass of catalyst is provided with vertically extending baffle means arranged to restrict the vaporous catalyst mixture passing upwardly therethrough to a hydraulic diameter within the range of 4 to 8.
Claim 12
Dependent Claim
54 words
The method of claim 1 wherein a portion of the circulated catalyst is withdrawn and subjected to partial regeneration and thereafter returned to the circulated catalyst to maintain residual coke on the circulated catalyst and catalyst charged to the riser in the range of from 5 to 20 weight percent coke on the catalyst.
Claim 13
Dependent Claim
47 words
The method of claim 1 wherein catalyst circulation through the riser, dense fluid mass of catalyst thereabove and the stripper-cooling zone is in response to reactant feed rate and the catalyst pressure at the base of a catalyst transfer zone in communication with said riser reaction zone.
References Cited (Backward Citations)
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1983-12-09 | 1984-06-09 | 1984-12-09 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1987-12-09 | 1988-06-09 | 1988-12-09 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1991-12-09 | 1992-06-09 | 1992-12-09 | $7700.00 | Window Closed / Lapsed |