IPC분류정보
국가/구분 |
United States(US) Patent
등록
|
국제특허분류(IPC7판) |
|
출원번호 |
US-0499442
(1995-07-06)
|
우선권정보 |
FR-1994-408332 (1994-07-06) |
발명자
/ 주소 |
|
출원인 / 주소 |
|
대리인 / 주소 |
Burns, Doane, Swecker & Mathis, L.L.P.
|
인용정보 |
피인용 횟수 :
5 인용 특허 :
5 |
초록
The invention relates to a process for drying a gaseous or liquid mixture by passing the said mixture into an adsorber, characterized in that the water adsorption equilibrium zone of the adsorber comprises an upstream alumina zone and a downstream molecular sieve zone.
대표청구항
▼
1. A process for drying a gaseous or liquid mixture by passing said mixture into an adsorber, the adsorber including a water adsorption equilibrium zone and a water adsorption mass transfer zone, the equilibrium zone comprising an upstream alumina zone and a downstream molecular sieve zone, the mass
1. A process for drying a gaseous or liquid mixture by passing said mixture into an adsorber, the adsorber including a water adsorption equilibrium zone and a water adsorption mass transfer zone, the equilibrium zone comprising an upstream alumina zone and a downstream molecular sieve zone, the mass transfer zone comprising a downstream portion of the molecular sieve zone, water concentration in the mass transfer zone varying from zero to the maximum water concentration at the equilibrium zone, the liquid or gaseous mixture additionally including HCl, the water adsorption zone of the adsorber being preceded, in the direction of flow of the mixture in the adsorber, by an alumina-based zone which removes HCl present in the mixture. 2. A process for drying a gaseous or liquid mixture by passing said mixture into an adsorber, the adsorber including a water adsorption equilibrium zone and a water adsorption mass transfer zone, the equilibrium zone comprising an upstream alumina zone and a downstream molecular sieve zone, the mass transfer zone comprising a downstream portion of the molecular sieve zone, water concentration in the mass transfer zone varying from zero to the maximum water concentration at the equilibrium zone, the liquid or gaseous mixture additionally including H 2 S, the water adsorption zone of the adsorber being followed, in the direction of flow of the mixture in the adsorber, by molecular sieve-based zone which removes H 2 S present in the mixture. 3. A process for drying a gaseous or liquid mixture by passing said mixture into an adsorber, the adsorber including a water adsorption equilibrium zone and a water adsorption mass transfer zone, the equilibrium zone comprising an upstream alumina zone and a downstream molecular sieve zone, the mass transfer zone comprising a downstream portion of the molecular sieve zone, water concentration in the mass transfer zone varying from zero to the maximum water concentration at the equilibrium zone, the liquid or gaseous mixture additionally including H 2 S and HCl, the water adsorption zone of the adsorber being preceded, in the direction of flow of the mixture in the adsorber, by an alumina-based zone which removes HCl present in the mixture, and the water adsorption zone being followed by a molecular sieve-based zone which removes H 2 S present in the mixture. 4. A process for drying a gaseous or liquid mixture by passing said mixture into an adsorber, the adsorber including a water adsorption equilibrium zone and a water adsorption mass transfer zone, the equilibrium zone comprising an upstream alumina zone and a downstream molecular sieve zone, the mass transfer zone comprising a downstream portion of the molecular sieve zone, water concentration in the mass transfer zone varying from zero to the maximum water concentration at the equilibrium zone, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.8 at an instant when water breaks through at an exit of the adsorber, wherein the liquid or gaseous mixture additionally includes H 2 S and HCl, the water adsorption zone of the adsorber being preceded, in the direction of flow of the mixture in the adsorber, by an alumina-based zone which removes HCl present in the mixture, and the water adsorption zone being followed by a molecular-sieve-based zone which removes H 2 S present in the mixture. 5. Process according to claim 1, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.95 at an instant when water breaks through at an exit of the adsorber. 6. Process according to claim 5, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.8 at an instant when water breaks t hrough at an exit of the adsorber. 7. Process according to claim 6, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.2 and 0.8 at an instant when water breaks through at an exit of the adsorber. 8. Process according to claim 1, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.30 at an instant when water breaks through at an exit of the adsorber. 9. Process according to claim 2, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.95 at an instant when water breaks through at an exit of the adsorber. 10. Process according to claim 9, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.8 at an instant when water breaks through at an exit of the adsorber. 11. Process according to claim 10, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.2 and 0.8 at an instant when water breaks through at an exit of the adsorber. 12. Process according to claim 2, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.30 at an instant when water breaks through at an exit of the adsorber. 13. Process according to claim 3, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.95 at an instant when water breaks through at an exit of the adsorber. 14. Process according to claim 13, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.8 at an instant when water breaks through at an exit of the adsorber. 15. Process according to claim 14, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.2 and 0.8 at an instant when water breaks through at an exit of the adsorber. 16. Process according to claim 3, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.30 at an instant when water breaks through at an exit of the adsorber. 17. Process according to claim 4, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.2 and 0.8 at an instant when water breaks through at an exit of the adsorber. 18. Process according to claim 4, wherein in the water adsorption equilibrium zone of the adsorber, the ratio Q of the volume of alumina to that of alumina and of the molecular sieve is between 0.05 and 0.30 at an instant when water breaks through at an exit of the adsorber.
※ AI-Helper는 부적절한 답변을 할 수 있습니다.