Patent US4338973A successfully refreshed from Google Patents.
US4100218A
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Ethane conversion process
Assignee: Mobil Oil AS
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Filing: 1977-05-31
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Granted: 1978-07-11
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Expires: 1997-05-31
Abstract
Abstract Ethane is converted to LPG and gasoline and/or aromatics concentrate in a combination process which comprises directly passing olefin effluent from the thermal cracking of ethane over a special crystalline aluminosilicate zeolite of the ZSM-5 type and recovering aromatics and C3+ hydrocarbons. For best yields, the thermal cracking step is conducted under more severe conditions than are used when ethylene production is optimized. The second, olefin conversion step is carried out at either the same pressure as the cracking step or higher. The process is of particular interest where low cost ethane is available.
Inventors
- 👤 Nai Yuen Chen
- 👤 Werner O. Haag
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-29 15:03
CPC Classifications
C; C07; C07C; C07C15/00; C07C2/00; C07C4/00; C07C4/02; C07C4/04; C07C9/00; C07C9/02; C07C2529/00; C07C2529/04; C07C2529/06; C10; C10G; C10G2400/00; C10G2400/30
Claims Analysis
Total Claims: 17
Claim 1
Independent Claim
166 words
An ethane conversion process which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7:1 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling the olefin-rich effluent to a temperature within the range from about 600° to 1200° F; c. contacting the cooled, olefin-rich effluent, without prior separation or purification, at a pressure within the range from about 0 to 200 psig and a WHSV of from about 1 to 10 with a crystalline aluminosilicate zeolite characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12 and a constraint index within the range of from 1 to 12; and d. recovering a C 5 + product suitable for use as gasoline, an LPG product, and light fuel gases.
Claim 2
Dependent Claim
166 words
An ethane conversion process which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7:1 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling the olefin-rich effluent to a temperature within the range from about 600° to 1200° F; c. contacting the cooled, olefin-rich effluent, without prior separation or purification, at a pressure within the range from about 0 to 200 psig and a WHSV of from about 1 to 10 with a crystalline aluminosilicate zeolite characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12 and a constraint index within the range of from 1 to 12; and d. recovering a C 5 + product suitable for use as gasoline, an LPG product, and light fuel gases.
Claim 3
Dependent Claim
22 words
The process of claim 1 wherein at least a portion of the light fuel gases are recycled to the thermal cracking step.
Claim 4
Dependent Claim
19 words
The process of claim 1 wherein the crystalline aluminosilicate zeolite has been exchanged with hydrogen ions or ammonium ions.
Claim 5
Dependent Claim
15 words
The process of claim 3 wherein a hydrogenation/dehydrogenation component is associated with the crystalline aluminosilicate.
Claim 6
Dependent Claim
11 words
The process of claim 4 wherein the hydrogenation/dehydrogenation component is zinc.
Claim 7
Dependent Claim
18 words
The process of claim 1 wherein the ethane conversion in the thermal cracker is greater than 75 percent.
Claim 8
Dependent Claim
25 words
The process of claim 1 wherein at least a portion of the recovered C 5 + product is further treated by separating an aromatics concentrate.
Claim 9
Dependent Claim
23 words
The process of claim 7 wherein the separated aromatics concentrate is dealkylated and a benzene product is recovered from the dealkylated aromatics concentrate.
Claim 10
Dependent Claim
31 words
The process of claim 1 wherein at least a portion of the water in the olefin-rich effluent is separated therefrom prior to contacting said olefin-rich effluent with the crystalline aluminosilicate zeolite.
Claim 11
Independent Claim
188 words
A method for converting ethane to LPG and gasoline which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7:1 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling the olefin-rich effluent to a temperature within the range from about 600° to about 800° to 850° F; c. contacting the cooled, olefin-rich effluent, without prior separation or purification, at a pressure within the range from about 0 to 200 psig and a WHSV of from about 1 to 10 with a crystalline aluminosilicate zeolite which has been exchanged with hydrogen ions or ammonium ions and which is characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12, and a constraint index within the range of from 1 to 12; and d. recovering a C 5 + gasoline product, a C 3 + C 4 LPG product, and light fuel gases.
Claim 12
Independent Claim
188 words
A method for converting ethane to LPG and gasoline which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7:1 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling the olefin-rich effluent to a temperature within the range from about 600° to about 800° to 850° F; c. contacting the cooled, olefin-rich effluent, without prior separation or purification, at a pressure within the range from about 0 to 200 psig and a WHSV of from about 1 to 10 with a crystalline aluminosilicate zeolite which has been exchanged with hydrogen ions or ammonium ions and which is characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12, and a constraint index within the range of from 1 to 12; and d. recovering a C 5 + gasoline product, a C 3 + C 4 LPG product, and light fuel gases.
Claim 13
Dependent Claim
18 words
The process of claim 10 wherein the ethane conversion in the thermal cracker is greater than 75 percent.
Claim 14
Independent Claim
232 words
A method for converting ethane to LPG and aromatics which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling and compressing the olefin-rich effluent to a temperature within the range from about 80° to 120° F and to a pressure within the range from about 100 to 200 psig; c. drying the cooled, olefin-rich effluent; d. contacting the dried, olefin-rich effluent, without further prior separation or purification, at a temperature within the range from about 800° to about 1200° F, at a pressure within the range from about 100 to 200 psig, and a WHSV of from about 1 to 10 with a zinc-containing crystalline aluminosilicate zeolite which has been exchanged with hydrogen ions or ammonium ions and which is characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12, and a constraint index within the range of from 1 to 12; and e. recovering a C 5 + fraction, a C 3 + C 4 LPG product, and light fuel gases; and f. separating an aromatics concentrate from the C 5 + fraction.
Claim 15
Independent Claim
232 words
A method for converting ethane to LPG and aromatics which comprises: a. thermally cracking ethane at temperatures within the range from about 1500° to 1600° F, pressures within the range from about 20 to 50 psig, and steam:ethane molar ratios within the range from about 0.1-0.7 to produce an olefin-rich effluent in a thermal cracker wherein the ethane conversion is greater than about 60 weight percent; b. cooling and compressing the olefin-rich effluent to a temperature within the range from about 80° to 120° F and to a pressure within the range from about 100 to 200 psig; c. drying the cooled, olefin-rich effluent; d. contacting the dried, olefin-rich effluent, without further prior separation or purification, at a temperature within the range from about 800° to about 1200° F, at a pressure within the range from about 100 to 200 psig, and a WHSV of from about 1 to 10 with a zinc-containing crystalline aluminosilicate zeolite which has been exchanged with hydrogen ions or ammonium ions and which is characterized by a pore dimension greater than about 5 Angstroms, a silica to alumina ratio of at least 12, and a constraint index within the range of from 1 to 12; and e. recovering a C 5 + fraction, a C 3 + C 4 LPG product, and light fuel gases; and f. separating an aromatics concentrate from the C 5 + fraction.
Claim 16
Dependent Claim
23 words
The process of claim 12 wherein the separated aromatics concentrate is dealkylated and a benzene product is recovered from the dealkylated aromatics concentrate.
Claim 17
Dependent Claim
18 words
The process of claim 12 wherein the ethane conversion in the thermal cracker is greater than 75 percent.
References Cited (Backward Citations)
US3760024A
Cited
US3928483A
Cited
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1981-07-10 | 1982-01-09 | 1982-07-11 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1985-07-10 | 1986-01-09 | 1986-07-11 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1989-07-10 | 1990-01-09 | 1990-07-11 | $7700.00 | Window Closed / Lapsed |