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US4381418A Expired / Lapsed US ⏱️ 0.0 years remaining

Catalytic dehydrogenation process

Assignee: Honeywell UOP LLC
•
Filing: 1981-12-04
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Granted: 1983-04-26
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Expires: 2001-12-04
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Abstract

Abstract A process for the catalytic dehydrogenation of C2+ normally gaseous paraffinic hydrocarbons to produce the corresponding monoolefinic hydrocarbons is disclosed. The energy-efficient process is particularly directed to the separation of recycle hydrogen from the olefinic hydrocarbon products and unreacted paraffinic hydrocarbons.

Inventors

  • 👤 Steve A. Gewartowski
  • 👤 Dennis E. O'Brien

Bibliographic Details

Application Number —
Jurisdiction US
Data Source google_patents
Last Synchronized 2026-11-01 20:47
CPC Classifications
C; C07; C07C; C07C5/00; C07C5/32; C07C5/327; C07C5/333; Y; Y10; Y10S; Y10S62/00; Y10S62/931; Y10S62/932

Claims Analysis

Total Claims: 10
Claim 1
Independent Claim 297 words
A catalytic dehydrogenation process which comprises the steps of: (a) heat exchanging a C 2 + normally gaseous paraffinic hydrocarbon feed stream with a net hydrogen product stream and a net hydrocarbon product stream chilled in accordance with step (g); (b) further cooling said hydrocarbon feed stream by admixture with a hydrogen recycle stream chilled in accordance with step (g) and recycled in accordance with step (h); (c) heating the combined hydrogen/hydrocarbon stream by indirect heat exchange with a reaction zone effluent stream compressed in accordance with step (e); (d) contacting the heated combined stream with a dehydrogenation catalyst in a reaction zone at dehydrogenation conditions producing a reaction zone effluent stream comprising hydrogen, olefinic hydrocarbon product and unreacted paraffinic hydrocarbons; (e) compressing said effluent stream and cooling the same by indirect heat exchange with the combined stream in accordance with step (c) and forming a liquid hydrocarbon phase and a hydrogen-rich vapor phase; (f) separating the thus cooled liquid hydrocarbon phase; (g) expanding the hydrogen-rich vapor phase to effect a further chilling and condensation of a residual hydrocarbon phase therefrom; (h) combining one portion of the chilled vapor phase with the hydrocarbon feed stream as recycle hydrogen in accordance with step (b); (i) heat exchanging the remaining portion of the chilled hydrogen-rich vapor phase with the hydrocarbon feed stream in accordance with step (a) and thereafter recovering said vapor phase as a net hydrogen product stream; (j) combining the cooled liquid hydrocarbon phase from step (f) and the chilled residual hydrocarbon phase from step (g), heat exchanging the combined hydrocarbon stream with the hydrocarbon feed stream in accordance with step (a), and thereafter recovering the combined stream as a net hydrocarbon products stream comprising olefinic hydrocarbon products stream comprising olefinic hydrocarbon products and unreacted paraffinic hydrocarbons.
Claim 2
Dependent Claim 297 words
A catalytic dehydrogenation process which comprises the steps of: (a) heat exchanging a C 2 + normally gaseous paraffinic hydrocarbon feed stream with a net hydrogen product stream and a net hydrocarbon product stream chilled in accordance with step (g); (b) further cooling said hydrocarbon feed stream by admixture with a hydrogen recycle stream chilled in accordance with step (g) and recycled in accordance with step (h); (c) heating the combined hydrogen/hydrocarbon stream by indirect heat exchange with a reaction zone effluent stream compressed in accordance with step (e); (d) contacting the heated combined stream with a dehydrogenation catalyst in a reaction zone at dehydrogenation conditions producing a reaction zone effluent stream comprising hydrogen, olefinic hydrocarbon product and unreacted paraffinic hydrocarbons; (e) compressing said effluent stream and cooling the same by indirect heat exchange with the combined stream in accordance with step (c) and forming a liquid hydrocarbon phase and a hydrogen-rich vapor phase; (f) separating the thus cooled liquid hydrocarbon phase; (g) expanding the hydrogen-rich vapor phase to effect a further chilling and condensation of a residual hydrocarbon phase therefrom; (h) combining one portion of the chilled vapor phase with the hydrocarbon feed stream as recycle hydrogen in accordance with step (b); (i) heat exchanging the remaining portion of the chilled hydrogen-rich vapor phase with the hydrocarbon feed stream in accordance with step (a) and thereafter recovering said vapor phase as a net hydrogen product stream; (j) combining the cooled liquid hydrocarbon phase from step (f) and the chilled residual hydrocarbon phase from step (g), heat exchanging the combined hydrocarbon stream with the hydrocarbon feed stream in accordance with step (a), and thereafter recovering the combined stream as a net hydrocarbon products stream comprising olefinic hydrocarbon products stream comprising olefinic hydrocarbon products and unreacted paraffinic hydrocarbons.
Claim 3
Dependent Claim 25 words
The process of claim 1 further characterized with respect to step (a) in that said hydrocarbon feed stream comprises C 3 -C 4 paraffinic hydrocarbons.
Claim 4
Dependent Claim 20 words
The process of claim 1 further characterized with respect to step (a) in that said hydrocarbon feed stream comprises isobutane.
Claim 5
Dependent Claim 39 words
The process of claim 1 further characterized with respect to step (d) in that said dehydrogenation conditions include a temperature of from about 900° to about 1300° F. and a pressure of from about 0 to about 35 psig.
Claim 6
Dependent Claim 39 words
The process of claim 1 further characterized with respect to step (d) in that said dehydrogenation conditions include a temperature of from about 1000° to about 1200° F. and a pressure of from about 10 to about 30 psig.
Claim 7
Dependent Claim 43 words
The process of claim 1 further characterized with respect to step (e) in that said effluent stream is compressed to a pressure of from about 85 to about 185 psig and cooled to a temperature of from about -10° to about -50° F.
Claim 8
Dependent Claim 43 words
The process of claim 1 further characterized with respect to step (e) in that said effluent stream is compressed to a pressure of from about 110 to about 160 psig and cooled to a temperature of from about -20° to about -40° F.
Claim 9
Dependent Claim 43 words
The process of claim 1 further characterized with respect to step (g) in that said vapor phase is expanded to reduce the pressure thereof to from about 15 to about 65 psig, and the temperature to from about -75° to about -95° F.
Claim 10
Dependent Claim 43 words
The process of claim 1 further characterized with respect to step (g) in that said vapor phase is expanded to reduce the pressure thereof to from about 30 to about 50 psig, and the temperature to from about -80° to about -90° F.

References Cited (Backward Citations)

US2620314A Cited
US3119677A Cited
US3647680A Cited
JPS5128565A Cited
CA1041003A Cited
US4272270A Cited
US4257794A Cited
US4343633A Cited

USPTO Annuity & Maintenance Windows

Annuity Stage Window Opens Payment Deadline Surcharge Period Until Estimated Fee Status
3.5 Years (Year 4) 1986-04-25 1986-10-25 1987-04-26 $2000.00 Window Closed / Lapsed
7.5 Years (Year 8) 1990-04-25 1990-10-25 1991-04-26 $3760.00 Window Closed / Lapsed
11.5 Years (Year 12) 1994-04-25 1994-10-25 1995-04-26 $7700.00 Window Closed / Lapsed

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