US 4,373,935 AGranted

Adsorption separation cycle

AssigneeUnion Carbide Corporation

InventorsJoseph P. Ausikaitis, Desh R. Garg

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Abstract

An efficient fixed-bed vapor-phase adsorption cycle for bulk separations wherein the heat front generated by the exothermic heat of adsorption is maintained in the bed either in or behind the mass transfer zone, and is subsequently used in the desorption/regeneration step. The cycle is especially useful in drying mixtures of water and compounds which form azeotropes with water as well as the azeotropes themselves, such as 190-proof ethanol.

Claims11

Dependent claims

Adsorption separation process which comprises;

(a) passing in the vapor phase a feedstock comprising at least 2.5 weight percent water in admixture with at least one organic molecular species into a fixed adsorption bed at a temperature and pressure which prevents the capillary condensation of said organic molecular species, said fixed adsorption bed containing an adsorbent mass consisting essentially of a crystalline zeolitic molecular sieve adsorbent, small enough to substantially exclude the said organic molecular species, moving the water adsorption mass transfer front and the coinciding or trailing heat front created in said fixed bed along said bed toward the effluent end thereof to a predetermined point short of breakthrough of either of said fronts, at least that portion of said molecular sieve adsorbent contacted by said water mass transfer front containing adsorbed thereon, prior to and at the time of contact of said front, at least about 2 weight percent water, said molecular sieve adsorbent having a capacity for the adsorption of water under the imposed operating conditions greater than the water loading thereon at the time of contact by the water mass-transfer front;
(b) from the effluent end of said bed, recovering a product stream containing a lower concentration of water than the feedstock;
(c) terminating the flow of feedstock into said bed prior to breakthrough of either of the heat front and the water mass transfer front, and prior to substantial loss of the heat energy from the bed, commencing the countercurrent passage through said bed of an essentially non-sorbable purge gas at a temperature within about 25.degree. F. of the temperature of, and substantially at the same pressure as, the feedstock entering the bed during adsorption step (a), said temperature and pressure being sufficient to prevent capillary condensation of the said organic molecular species of said feedstock, whereby said heat front is moved back through said bed and utilized in desorbing water from the adsorbent mass;
(d) continuing the countercurrent purging of said bed until the water loading on said adsorbate is essentially the same as at the beginning of adsorption step (a), and
(e) repeating adsorption step (a).

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Dependencies are inferred from the claim text.

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Abstract

Adsorption separation process which comprises;

(a) passing in the vapor phase a feedstock comprising at least 2.5 weight percent water in admixture with at least one organic molecular species into a fixed adsorption bed at a temperature and pressure which prevents the capillary condensation of said organic molecular species, said fixed adsorption bed containing an adsorbent mass consisting essentially of a crystalline zeolitic molecular sieve adsorbent, small enough to substantially exclude the said organic molecular species, moving the water adsorption mass transfer front and the coinciding or trailing heat front created in said fixed bed along said bed toward the effluent end thereof to a predetermined point short of breakthrough of either of said fronts, at least that portion of said molecular sieve adsorbent contacted by said water mass transfer front containing adsorbed thereon, prior to and at the time of contact of said front, at least about 2 weight percent water, said molecular sieve adsorbent having a capacity for the adsorption of water under the imposed operating conditions greater than the water loading thereon at the time of contact by the water mass-transfer front;
(b) from the effluent end of said bed, recovering a product stream containing a lower concentration of water than the feedstock;
(c) terminating the flow of feedstock into said bed prior to breakthrough of either of the heat front and the water mass transfer front, and prior to substantial loss of the heat energy from the bed, commencing the countercurrent passage through said bed of an essentially non-sorbable purge gas at a temperature within about 25.degree. F. of the temperature of, and substantially at the same pressure as, the feedstock entering the bed during adsorption step (a), said temperature and pressure being sufficient to prevent capillary condensation of the said organic molecular species of said feedstock, whereby said heat front is moved back through said bed and utilized in desorbing water from the adsorbent mass;
(d) continuing the countercurrent purging of said bed until the water loading on said adsorbate is essentially the same as at the beginning of adsorption step (a), and
(e) repeating adsorption step (a).

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