[특허]Production of high purity and ultra-high purity gas

Praxair Technology, Inc.

검색어에 아래의 연산자를 사용하시면 더 정확한 검색결과를 얻을 수 있습니다.
검색연산자

검색도움말
검색연산자	기능	검색시 예
()	우선순위가 가장 높은 연산자	예1) (나노 (기계 \| machine))
공백	두 개의 검색어(식)을 모두 포함하고 있는 문서 검색	예1) (나노 기계) 예2) 나노 장영실
\|	두 개의 검색어(식) 중 하나 이상 포함하고 있는 문서 검색	예1) (줄기세포 \| 면역) 예2) 줄기세포 \| 장영실
!	NOT 이후에 있는 검색어가 포함된 문서는 제외	예1) (황금 !백금) 예2) !image
*	검색어의 *란에 0개 이상의 임의의 문자가 포함된 문서 검색	예) semi*
""	따옴표 내의 구문과 완전히 일치하는 문서만 검색	예) "Transform and Quantization"

과학기술 지식인프라 ScienceON

연합인증

연합인증 가입 기관의 연구자들은 소속기관의 인증정보(ID와 암호)를 이용해 다른 대학, 연구기관, 서비스 공급자의 다양한 온라인 자원과 연구 데이터를 이용할 수 있습니다.

이는 여행자가 자국에서 발행 받은 여권으로 세계 각국을 자유롭게 여행할 수 있는 것과 같습니다.

연합인증으로 이용이 가능한 서비스는 NTIS, DataON, Edison, Kafe, Webinar 등이 있습니다.

한번의 인증절차만으로 연합인증 가입 서비스에 추가 로그인 없이 이용이 가능합니다.

다만, 연합인증을 위해서는 최초 1회만 인증 절차가 필요합니다. (회원이 아닐 경우 회원 가입이 필요합니다.)

연합인증 절차는 다음과 같습니다.

최초이용시에는
ScienceON에 로그인 → 연합인증 서비스 접속 → 로그인 (본인 확인 또는 회원가입) → 서비스 이용

그 이후에는
ScienceON 로그인 → 연합인증 서비스 접속 → 서비스 이용

연합인증을 활용하시면 KISTI가 제공하는 다양한 서비스를 편리하게 이용하실 수 있습니다.

특허 상세정보

MyON담기

내보내기 페이스북 공유 트위터 공유 카카오톡 공유

Production of high purity and ultra-high purity gas

특허상세정보
국가/구분	United States(US) Patent 등록
국제특허분류(IPC7판)	B01D-053/04 B01D-053/62
미국특허분류(USC)	095/118; 095/139; 095/140; 096/132; 423/247; 422/190
출원번호	UP-0515307 (2003-05-30)
등록번호	US-7524358 (2009-07-01)
국제출원번호	PCT/US03/017296 (2003-05-30)
§371/§102 date	20060509 (20060509)
국제공개번호	WO03/101587 (2003-12-11)
발명자 / 주소	Saxena, Himanshu Ackley, Mark William Billingham, John Fredric Barrett, Philip Alexander
출원인 / 주소	Praxair Technology, Inc.
대리인 / 주소	Schwartz, Iurie A.
인용정보	피인용 횟수 : 17 인용 특허 : 24

초록

Trace amounts of carbon monoxide and optionally hydrogen are removed from gaseous feed streams by passing the feed stream through a carbon monoxide adsorbent (33) prior to passing it through a supported metal catalyst (34). The invention saves significant capital and operational costs over existing processes.

대표
청구항
▼

What is claimed is: 1. An adsorption apparatus for the removal of CO from a feed stream containing CO in an amount of less than 50 ppm, said apparatus comprising at least one adsorption vessel containing a CO adsorbent layer, the CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g, and a source which supplies said feed stream, wherein a) when said feed stream further contains at least one gas selected from the group consisting of nitrogen, He, Ne, Ar, Xe, Kr, CH4 and mixtures thereof, said adsorbent is ion exchanged with a Group IB element; or b) when said feed stream further contains at least one gas selected from the group consisting of oxygen and air and mixtures thereof, said adsorbent is a zeolite having a SiO2/Al2O3 ratio of <20, and is ion-exchanged with a Ag+ or Au+. 2. The apparatus of claim 1, wherein said apparatus contains two or more of said adsorption vessels. 3. The apparatus of claim 1, wherein said adsorption vessel is selected from the group consisting of vertical flow vessels, horizontal flow vessels, lateral flow vessels or radial flow vessels. 4. The adsorption apparatus of claim 1, wherein said apparatus further contains an adsorbent selective for the adsorption of water, and wherein the water selective adsorbent layer is upstream of said CO adsorbent layer. 5. The adsorption apparatus of claim 1, wherein said apparatus further contains a catalyst layer for the catalytic oxidation of H2 to H2O, and wherein said catalyst layer is downstream of said CO adsorbent layer. 6. The adsorption apparatus of claim 5, wherein said apparatus further contains an auxiliary adsorbent for the removal of water, and wherein said auxiliary adsorbent is downstream of said catalyst layer. 7. The apparatus of claim 1, wherein said ΔCO working capacity is greater than or equal to 0.03 mmol/g. 8. The apparatus of claim 4, wherein the water selective adsorbent is one or more of alumina or NaX zeolite. 9. The apparatus of claim 5, wherein the H2 catalyst is a supported metal catalyst. 10. The apparatus of claim 9, wherein said supported metal catalyst comprises one or more of the metals Os, Ir, Pt, Ru, Rh, Pd, Fe, Co, Ni, Cu, Ag, Au, Zn, Sn, Mn, Cr, Pb, Ce and is supported on a substrate selected from the group consisting of alumina, silica, natural or synthetic zeolites, titanium dioxide, magnesium oxide and calcium oxide. 11. The apparatus of claim 1, wherein said apparatus further contains: a) at least one adsorbent layer upstream of said CO adsorbent for the adsorption of one or more of H2O and CO2, b) a catalyst layer for the catalytic conversion of H2 to H2O that is downstream of said CO adsorbent layer; and c) one or more additional adsorbents for the adsorption of one or more of H2O, CO2, N2O and hydrocarbons, wherein said additional adsorbents are downstream of said catalyst layer. 12. The apparatus of claim 11, wherein said one or more additional adsorbents are selected from the group consisting of alumina, silica gel, clinoptilolite, zeolites, composites thereof and mixtures thereof. 13. The apparatus of claim 1, wherein the CO adsorbent has a ΔCO/ΔN2 separation factor of greater than or equal to 1×10-3. 14. The apparatus of claim 1, wherein when said feed stream further contains at least one gas selected from the group consisting of nitrogen, He, Ne, Ar, Xe, Kr, H2, CH4 and mixtures thereof, said CO adsorbent is selected from the group consisting of AgX zeolite, Ag-Mordenite, Cu-clinoptilolite, AgA zeolite and AgY zeolite. 15. The apparatus of claim 1, wherein when said feed stream further contains at least one gas selected from the group consisting of oxygen and air and mixtures thereof, said CO adsorbent is selected from the group consisting of AgX zeolite, Ag-Mordenite, AgA zeolite and AgY zeolite. 16. The apparatus of claim 1, wherein said CO adsorbent is AgX zeolite. 17. The apparatus of claims 1, wherein when said feed gas further contains air, said apparatus is an air prepurifier. 18. The apparatus of claim 1, wherein said CO adsorbent is AgX having 100% of its cations associated with Ag. 19. A process for the removal of CO from a feed stream containing CO in an amount of less than 50 ppm, said process comprising contacting said feed stream with a CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g to produce a CO depleted gas stream; and wherein a) when said feed stream further contains at least one gas selected from the group consisting of nitrogen, He, Ne, Ar, Xe, Kr, H2, CH4 and mixtures thereof, said adsorbent is a zeolite exchanged with a Group IB element; or b) when said feed stream further contains at least one gas selected from the group consisting of oxygen and air and mixtures thereof, said adsorbent is a zeolite having a SiO2/Al2O3 ratio of <20, and is ion-exchanged with a Ag+ or Au+. 20. The process of claim 19, further comprising recovering said CO depleted gas stream, wherein CO is present in said CO depleted gas stream at a concentration of less than 100 ppb. 21. The process of claim 19, further comprising recovering said CO depleted gas stream, wherein CO is present in said CO depleted gas stream at a concentration of less than 5 ppb. 22. The process of claim 19, wherein said CO concentration in said feed stream is less than 1 ppm CO. 23. The process of claim 19, wherein said CO concentration in said feed stream is less than 0.5 ppm CO. 24. The process of claim 19, wherein said feed gas further comprises water (H2O), and said process further comprises contacting said feed stream with a water selective adsorbent that is located upstream of said CO adsorbent. 25. The process of claim 19, wherein said feed gas further comprises hydrogen, and said process further comprises contacting said CO depleted feed stream with a catalyst layer for the catalytic oxidation of H2 to H2O to produce a H2 depleted and H2O enriched gas, and wherein said catalyst layer is located downstream of said CO adsorbent layer. 26. The process of claim 25, wherein said process further comprises the step of contacting said H2O enriched gas with an adsorbent for the removal of water, and wherein the H2O adsorbent layer is located downstream of said catalyst layer to produce a gas that is depleted in CO, H2 and H2O. 27. The process of claim 19, wherein said ΔCO working capacity is greater than or equal to 0.03 mmol/g. 28. The process of claim 19, wherein the CO adsorbent has a ΔCO/ΔN2 separation factor that is greater than or equal to 1×10-3. 29. The process of claim 19, wherein the CO adsorbent has a ΔCO/ΔN2 separation factor that is greater than or equal to 1×10-2. 30. The process of claim 24, wherein the water selective adsorbent is one or more of alumina or NaX. 31. The process of claim 25, wherein the catalyst is a supported metal catalyst. 32. The process of claim 31, wherein said supported metal catalyst is comprises one or more of the metals Os, Ir, Pt, Ru, Rh, Pd, Fe, Co, Ni, Cu, Ag, Au, Zn, Sn, Mn, Cr, Pb, Ce and is supported on a substrate selected from the group consisting of alumina, silica, natural or synthetic zeolites, titanium dioxide, magnesium oxide and calcium oxide. 33. The process of claim 19, wherein said process further comprises passing said feed gas over: a) at least one adsorbent layer upstream of said CO adsorbent for the adsorption of one or more of H2O and CO2, b) a catalyst layer for the catalytic conversion of H2 to H2O that is downstream of said CO adsorbent layer; and c) one or more additional adsorbents for the adsorption of one or more of H2O, CO2, N2O and hydrocarbons, wherein said additional adsorbents are downstream of said catalyst layer. 34. The process of claim 33, wherein said one or more additional adsorbents are selected from the group consisting of alumina, silica gel, clinoptilolite, zeolites, composites thereof and mixtures thereof. 35. The process of claim 19, wherein said process is selected from the group consisting of pressure swing adsorption, temperature swing adsorption, or a combination thereof. 36. The process of claim 19, wherein said process takes place in an adsorber vessel selected from a vertical flow vessel, a horizontal flow vessel or a radial flow vessel. 37. The process of claim 25, wherein the hydrogen depleted gas contains less than 100 ppb hydrogen. 38. The process of claim 25, wherein the hydrogen depleted gas contains less than 5 ppb hydrogen. 39. The process of claim 19, wherein the adsorption step of said process is operated at a temperature of zero to fifty degrees Celsius. 40. The process of claim 19, wherein when said feed gas further contains at least one gas selected from the group consisting of nitrogen, He, Ne, Ar, Xe, Kr, H2, CH4 and mixtures thereof said CO adsorbent is selected from the group consisting of AgX, Ag-Mor, Cu-clinoptilolite, AgA zeolite and AgY zeolite. 41. The process of claim 19, wherein when said feed gas further contains at least one gas selected from the group consisting of air and oxygen and mixtures thereof said CO adsorbent is selected from the group consisting of AgX, Ag-Mor, AgA zeolite and AgY zeolite. 42. The process of claim 19, wherein said CO adsorbent is AgX having greater than 50% of its cations associated with Ag. 43. The process of claim 19, wherein said CO adsorbent is AgX having 100% of its cations associated with Ag. 44. The process of claim 19, wherein said feed stream contains air, and wherein said CO depleted gas stream is passed to a cryogenic distillation column. 45. The process of claim 19, further comprising recovering said CO depleted gas stream, wherein CO is present in said CO depleted gas stream at a concentration of less than 1 ppb. 46. The process of claim 19, wherein the CO partial pressure in said feed stream is less than 0.1 mmHg. 47. The process of claim 19, wherein the CO partial pressure in said feed stream is less than 0.005 mmHg. 48. A process for the removal of CO from a feed stream containing CO in an amount of less than 50 ppm and hydrogen said process comprising contacting said feed stream with a CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g to produce a CO depleted gas stream; and wherein said adsorbent is a zeolite exchanged with a Group IB element. 49. An adsorption apparatus for the removal of CO from a feed stream containing CO in an amount of less than 50 ppm, and hydrogen, said apparatus comprising at least one adsorption vessel containing a CO adsorbent layer, the CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g; and wherein said adsorbent is a zeolite exchanged with a Group IB element, and a source which supplies said feed stream. 50. An air prepurification adsorption apparatus for the removal of CO from an air feed stream containing CO in an amount of less than 50 ppm, said apparatus comprising at least one adsorption vessel containing a CO adsorbent layer, the CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g, and a source which supplies said feed stream, and wherein said adsorbent is a zeolite having a SiO2/Al2O3 ratio of <20, and is ion-exchanged with a Ag+ or Au+. 51. The apparatus of claim 50, wherein said apparatus further comprises at least one adsorbent layer upstream of said CO adsorbent for the adsorption of one or more of H2O and CO2. 52. The apparatus of claim 49 or claim 50, further comprising a catalyst layer for the catalytic conversion of H2 to H2O that is downstream of said CO adsorbent layer; and one or more additional adsorbents for the adsorption of one or more of H2O, CO2, N2O and hydrocarbons, wherein said additional adsorbents are downstream of said catalyst layer. 53. The apparatus of claim 49 or claim 50, wherein said CO adsorbent is AgX. 54. A process for the removal of CO from a feed stream containing CO in an amount of less than 50 ppm and air said process comprising contacting said feed stream in an adsorber vessel with a CO adsorbent having a ΔCO working capacity greater than or equal to 0.01 mmol/g to produce a CO depleted gas stream; and wherein_said adsorbent is a zeolite having a SiO2/Al2O3 ratio of <20, and is ion-exchanged with a Ag+ or Au+. 55. The process claim 54, wherein said process further comprises passing said feed stream over at least one adsorbent layer upstream of said CO adsorbent for the adsorption of one or more of H2O and CO2 to produce a H2O and or CO2 depleted feed stream. 56. The process of claim 54, wherein said process further comprises, passing said feed stream over a catalyst layer that is downstream of said CO adsorbent layer for the catalytic conversion of H2 to H2O layer and one or more additional adsorbents for the adsorption of one or more of H2O, CO2, N2O and hydrocarbons, wherein said additional adsorbents are downstream of said catalyst layer to produce a feed stream that is depleted in CO, H2 and one or more of H2O, CO2, N2O and hydrocarbons. 57. The process of claim 54, wherein said CO adsorbent is AgX. 58. The process of claim 54, wherein the depleted feed stream is passed to a cryogenic distillation column for the separation of air.

이 특허에 인용된 특허 (24)

이 특허를 인용한 특허 피인용횟수: 17

IPC 상위 출원인

내보내기

상세정보
내보내기 구분	파일저장 인쇄 메일전송
구성항목	관리번호, 국가코드, 자료구분, 상태, 출원번호, 출원일자, 공개번호, 공개일자, 등록번호, 등록일자, 발명명칭(한글), 발명명칭(영문), 출원인(한글), 출원인(영문), 출원인코드, 대표IPC 관리번호, 국가코드, 자료구분, 상태, 출원번호, 출원일자, 공개번호, 공개일자, 공고번호, 공고일자, 등록번호, 등록일자, 발명명칭(한글), 발명명칭(영문), 출원인(한글), 출원인(영문), 출원인코드, 대표출원인, 출원인국적, 출원인주소, 발명자, 발명자E, 발명자코드, 발명자주소, 발명자 우편번호, 발명자국적, 대표IPC, IPC코드, 요약, 미국특허분류, 대리인주소, 대리인코드, 대리인(한글), 대리인(영문), 국제공개일자, 국제공개번호, 국제출원일자, 국제출원번호, 우선권, 우선권주장일, 우선권국가, 우선권출원번호, 원출원일자, 원출원번호, 지정국, Citing Patents, Cited Patents
저장형식	Text(ASCII format) Excel format PIAS분석(.xls)
메일정보	받는사람 (필수) @ 보내는사람 (선택) @ 제목 내용 KISTI 검색결과 이메일 서비스
안내	> 총 건의 자료가 검색되었습니다. > 다운받으실 자료의 인덱스를 입력하세요. (1-10,000) > 검색결과의 순서대로 최대 10,000건 까지 다운로드가 가능합니다. > 데이타가 많을 경우 속도가 느려질 수 있습니다.(최대 2~3분 소요) > 다운로드 파일은 UTF-8 형태로 저장됩니다. 파일의 내용이 제대로 보이지 않을실 때는 웹브라우저 상단의 보기 -> 인코딩 -> 자동선택 여부를 확인하십시오 > ~ > Text(ASCII format) Excel format

과학기술 지식인프라 ScienceON

ScienceON Chatbot

연합인증

특허 상세정보

Production of high purity and ultra-high purity gas

초록

대표
청구항
▼

이 특허에 인용된 특허 (24)

이 특허를 인용한 특허 피인용횟수: 17

IPC 상위 출원인

과제정보

상세정보조회

원문조회

IPC 상세정보(version : 201201)

연구과제 성과물(0)

참여연구원의 다른 문헌(0)

처리중입니다.

잠시만 기다려주세요.

ScienceON Chatbot

연합인증

특허 상세정보

Production of high purity and ultra-high purity gas

초록

대표청구항 ▼

이 특허에 인용된 특허 (24)

이 특허를 인용한 특허 피인용횟수: 17

IPC 상위 출원인

과제정보

상세정보조회

원문조회

IPC 상세정보(version : 201201)

연구과제 성과물(0)

참여연구원의 다른 문헌(0)

처리중입니다.

잠시만 기다려주세요.

대표
청구항
▼