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US 5,177,293 AGranted
Separation process for the product streams resulting from the dehydrogenation of hydrocarbons
AssigneeUop LLC
InventorsMichael J. Mitariten, Norman H. Scott
Life of this patent
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Abstract
A process for the separation and recovery of the products stream resulting from the dehydrogenation of dehydrogenatable hydrocarbons which process utilizes an integrated system for the recovery of liquid olefin product by the use of a compression system, a pressure swing adsorption unit and a chiller system to concentrate the olefin product.
Claims14
A process for the dehydrogenation of a dehydrogenatable hydrocarbon which process comprises:
- (a) contacting said dehydrogenatable hydrocarbon with a dehydrogenation catalyst in a dehydrogenation zone at dehydrogenation conditions to produce a hydrocarbon effluent stream comprising dehydrogenated hydrocarbons, unconverted dehydrogenatable hydrocarbons and hydrogen;
- (b) compressing said hydrocarbon effluent stream comprising dehydrogenated hydrocarbons, unconverted dehydrogenatable hydrocarbons and hydrogen to produce a first compressed stream;
- (c) cooling said first compressed stream to a temperature less than about 150.degree. F. (65.degree. C.);
- (d) introducing the resulting compressed, cooled stream produced in step (c) into a vapor-liquid separator;
- (e) withdrawing from said vapor-liquid separator a liquid stream comprising at least a portion of said dehydrogenated hydrocarbons and said unconverted dehydrogenatable hydrocarbon contained in said hydrocarbon effluent stream;
- (f) withdrawing from said vapor-liquid separator a hydrogen-rich gaseous stream comprising at least a portion of said dehydrogenated hydrocarbons and unconverted dehydrogenatable hydrocarbons;
- (g) passing said hydrogen-rich gaseous stream from step (f) to a first adsorber bed containing adsorbent having adsorptive capacity for hydrocarbons at effective adsorption conditions;
- (h) withdrawing a hydrogen-rich gaseous stream having a reduced concentration of hydrocarbons from said first adsorber bed;
- (i) withdrawing a stream rich in hydrocarbons from a second adsorber bed containing adsorbent having adsorptive capacity for hydrocarbons which bed has become loaded with hydrocarbons and is undergoing desorption;
- (j) compressing said stream rich in hydrocarbons recovered from step (i) to produce a second compressed stream;
- (k) cooling said second compressed stream from step (j) to a temperature less than about 100.degree. F. (38.degree. C.);
- (l) introducing the resulting compressed, cooled stream produced in step (k) into a vapor-liquid separator to produce a vapor stream comprising hydrogen and a liquid stream comprising dehydrogenated hydrocarbon;
- (m) recycling said vapor stream comprising hydrogen recovered in step (l) to step (g);
- and
- (n) recovering a hydrocarbon stream comprising a dehydrogenated hydrocarbon.
12 more elements
A process for the dehydrogenation of a dehydrogenatable hydrocarbon which process comprises:
- (a) contacting said dehydrogenatable hydrocarbon with a dehydrogenation catalyst in a dehydrogenation zone at dehydrogenation conditions which include a temperature from about 1022.degree. F. (550.degree. C.) to about 1472.degree. F. (800.degree. C.), a pressure from about 0.01 to about 10 atmospheres absolute, a liquid hourly space velocity from about 0.1 to about 100 hr..sup.-1 and a hydrogen to hydrocarbon mole ratio from about 0.01:1 to about 40:1 to produce a hydrocarbon effluent stream comprising dehydrogenated hydrocarbons, unconverted dehydrogenatable hydrocarbons and hydrogen;
- (b) compressing said hydrocarbon effluent stream comprising dehydrogenated hydrocarbons, unconverted dehydrogenatable hydrocarbons and hydrogen to a pressure in the range from about 70 psig (482 kPa gauge) to about 1000 psig (6895 kPa gauge) to produce a first compressed stream;
- (c) cooling said first compressed stream to a temperature in the range from about 60.degree. F. (16.degree. C.) to about 120.degree. F. (49.degree. C.);
- (d) introducing the resulting compressed, cooled stream produced in step (c) into a vapor-liquid separator;
- (e) withdrawing from said vapor-liquid separator a liquid stream comprising at least a portion of said dehydrogenated hydrocarbons and said unconverted dehydrogenatable hydrocarbon contained in said hydrocarbon effluent stream;
- (f) withdrawing from said vapor-liquid separator a hydrogen-rich gaseous stream comprising at least a portion of said dehydrogenated hydrocarbons and unconverted dehydrogenatable hydrocarbons;
- (g) passing said hydrogen-rich gaseous stream from step (f) to a first adsorber bed containing adsorbent having adsorptive capacity for hydrocarbons at effective adsorption conditions;
- (h) withdrawing a hydrogen-rich gaseous stream having a reduced concentration of hydrocarbons from said first adsorber bed;
- (i) withdrawing a stream rich in hydrocarbons from a second adsorber bed containing adsorbent having adsorptive capacity for hydrocarbons which bed has become loaded with hydrocarbons and is undergoing desorption;
- (j) compressing said stream rich in hydrocarbons recovered from step (i) to a pressure in the range from about 70 psig (482 kPa gauge) to about 1000 psig (6895 kPa gauge) to produce a second compressed stream;
- (k) cooling said second compressed stream from step (j) to a temperature in the range from about -20.degree. F. (-29.degree. C.) to about 100.degree. F. (38.degree. C.);
- (l) introducing the resulting compressed, cooled stream produced in step (k) into a vapor-liquid separator to produce a vapor stream comprising hydrogen and a liquid stream comprising dehydrogenated hydrocarbon;
- (m) recycling said vapor stream comprising hydrogen recovered in step (l) to step (g);
- and
- (n) recovering a hydrocarbon stream comprising a dehydrogenated hydrocarbon.
12 more elements
Dependencies are inferred from the claim text.