CA1269089A - Selective adsorbent for co and method of manufacturing the same - Google Patents
Selective adsorbent for co and method of manufacturing the sameInfo
- Publication number
- CA1269089A CA1269089A CA000523163A CA523163A CA1269089A CA 1269089 A CA1269089 A CA 1269089A CA 000523163 A CA000523163 A CA 000523163A CA 523163 A CA523163 A CA 523163A CA 1269089 A CA1269089 A CA 1269089A
- Authority
- CA
- Canada
- Prior art keywords
- zeolite
- salt
- adsorbent
- carried
- ion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003463 adsorbent Substances 0.000 title claims abstract description 74
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 74
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000010457 zeolite Substances 0.000 claims abstract description 74
- VMQMZMRVKUZKQL-UHFFFAOYSA-N Cu+ Chemical compound [Cu+] VMQMZMRVKUZKQL-UHFFFAOYSA-N 0.000 claims abstract description 50
- 238000005342 ion exchange Methods 0.000 claims abstract description 48
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 30
- 150000003839 salts Chemical class 0.000 claims abstract description 21
- 239000011148 porous material Substances 0.000 claims abstract description 19
- 229910052751 metal Inorganic materials 0.000 claims abstract description 18
- 239000002184 metal Substances 0.000 claims abstract description 18
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 15
- 238000005341 cation exchange Methods 0.000 claims abstract description 12
- 229910052742 iron Inorganic materials 0.000 claims abstract description 6
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 6
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 6
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 5
- 238000001179 sorption measurement Methods 0.000 claims description 97
- 238000000034 method Methods 0.000 claims description 66
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 claims description 58
- 238000005470 impregnation Methods 0.000 claims description 30
- 239000000203 mixture Substances 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 8
- -1 Cu(I) halide Chemical class 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 150000004820 halides Chemical class 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims 3
- 239000001569 carbon dioxide Substances 0.000 claims 3
- 239000007789 gas Substances 0.000 description 64
- 238000011084 recovery Methods 0.000 description 31
- 239000000243 solution Substances 0.000 description 22
- 229910021591 Copper(I) chloride Inorganic materials 0.000 description 19
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 description 19
- 238000006722 reduction reaction Methods 0.000 description 19
- 239000000047 product Substances 0.000 description 17
- 239000010949 copper Substances 0.000 description 12
- 238000010926 purge Methods 0.000 description 10
- 238000005070 sampling Methods 0.000 description 10
- 238000003795 desorption Methods 0.000 description 9
- QTMDXZNDVAMKGV-UHFFFAOYSA-L copper(ii) bromide Chemical compound [Cu+2].[Br-].[Br-] QTMDXZNDVAMKGV-UHFFFAOYSA-L 0.000 description 8
- 238000002474 experimental method Methods 0.000 description 6
- 238000005259 measurement Methods 0.000 description 6
- 239000008188 pellet Substances 0.000 description 6
- 229920002545 silicone oil Polymers 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 230000003247 decreasing effect Effects 0.000 description 5
- 229910001510 metal chloride Inorganic materials 0.000 description 5
- 229910021645 metal ion Inorganic materials 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910021590 Copper(II) bromide Inorganic materials 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 239000006228 supernatant Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 229910015400 FeC13 Inorganic materials 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000011230 binding agent Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000010908 decantation Methods 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000003979 granulating agent Substances 0.000 description 2
- 229910052680 mordenite Inorganic materials 0.000 description 2
- 229920000136 polysorbate Polymers 0.000 description 2
- 239000012047 saturated solution Substances 0.000 description 2
- 238000009628 steelmaking Methods 0.000 description 2
- 239000010963 304 stainless steel Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910021589 Copper(I) bromide Inorganic materials 0.000 description 1
- 229910018965 MCl2 Inorganic materials 0.000 description 1
- JQGGAELIYHNDQS-UHFFFAOYSA-N Nic 12 Natural products CC(C=CC(=O)C)c1ccc2C3C4OC4C5(O)CC=CC(=O)C5(C)C3CCc2c1 JQGGAELIYHNDQS-UHFFFAOYSA-N 0.000 description 1
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 description 1
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 125000005843 halogen group Chemical group 0.000 description 1
- 239000003779 heat-resistant material Substances 0.000 description 1
- 239000011874 heated mixture Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002674 ointment Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000011369 resultant mixture Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
- 239000011592 zinc chloride Substances 0.000 description 1
- 235000005074 zinc chloride Nutrition 0.000 description 1
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
- B01J20/186—Chemical treatments in view of modifying the properties of the sieve, e.g. increasing the stability or the activity, also decreasing the activity
Abstract
Abstract of the Disclosure This invention proposes an adsorbent containing mainly Cu(I) ion-exchanged and carried in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10, and a salt of a least one metal selected from the group consisting of Cu(I), Fe, Zn, Ni, and Mg, the metal salt being dispersed and carried in pores of the zeolite. This invention also proposes a method of manufacturing the above adsorbent.
Description
~Z~;9089 The present invention relates to an adsorbent suitable for selectively adsorbing or separating Co by a PSA ~pressure swing adsorption) method, and a method of manufacturing the same.
Japanese Patent Disclosure (Kokai) No. 58-15~517 discloses a solid adsorbent containing copper halide(I) and active carbon as a C0 adsorbent. However, stable use of this adsorbent for a long period of time has never been reported. U.S.P, No. 4,019,879 describes an adsorbent prepared by carrying Cu(I) in zeolite whose silica/alumina ratio is as high as 20 to 200.
In zeolite having such a high silica/alumina ratio, it is known that the number of cations capable of ion exchange tends to be reduced. It may be concluded that the C0 adsorption amount per unit weight is reduced.
A C0 desorption technique by the PSA method has ; been developed as a typical adsorption method.
For example, Japanese Patent Disclosure (Kokai) 2û No. 59-22625 describes a two-step treatment for performing a PSA to eliminate moisture and C02 in a pretreatment step. Japanese Patent Disclosure (Kokai) No. 59-26121 describes a two-step treatment of sepa-rating C0 from a converter gas. According to this ~ 25 method, mordenite is used as an adsorbent, and Cû2-PSA
t and C0-PSA are separately performed. These conventional j~ proposals indicate that the adsorbents have a large C0 ' ~IZ69089 adsorption amount near room temperature. However, the C2 adsorption amount is larger than the C0 adsorption amount. In order to separate C0 from a gas mixture containing C02, C02 is separated from the gas mixture in the pretreatment, and then Co is separated by the C0-PSA process.
It is a first object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein C0 can be selectively separated from a gas mixture containing mainly C0, C02, and N2 by a single step at a PSA temperature closer to room temperature, so that the separated C0 can be condensed.
It is a second object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein a large amount of gas can be treated by a smaller amount of adsorbent.
It is a third object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein an adsorption tower and a treating gas need not be heated, thus reducing the operation cost.
It is a fourth object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein a material for a switching valve and the like in a PSA apparatus need not be a heat-resistant material.
According to an aspect of the present invention, lZ69089 there is provided a selective adsorbent for C0, comprising: mainly Cu(I) carried in an ion exchange site of zeolite having a silica/alumina ratio of not more than 10 at an ion exchange ratio of not less than 50% and preferably not less than 70%; and a salt of at least one metal selected from the group consisting of Cu(I), Fe, Zn, Ni, and Mg, the salt being dispersed and carried in pores of the zeolite, the salt being more preferably a Cu(I) salt and most preferably a salt containlng as a major constituent a halide such as a Cu(I) chloride, and the metal salt being contained in a total amount of 0.8 mmol to 2.5 mmol and more preferably l.û mmol to 2.û mmol per gram of ion-exchange Cu(I) zeolite. Carbon monoxide can be selectively separated by the adsorbent at a temperature of 40 to I00C.
According to another aspect of the present invention, there is provided a method of manufacturing the above adsorbent, comprising the steps of:
ion-exchanging and carrying Cu(II) in a cation exchange site of the zeolite; dispersing and carrying mainly a Cu(II) salt in pores of the zeolite by an impregnation method; and reducing the Cu(II) and the Cu(II) salt with a reducing gas such as H2 or C0 to obtain mainly Cu(I) and a Cu(I) salt. After Cu(II) is carried by ion exchanging, the Cu(II) salt is preferably dispersed and carried by the impregnation method.
A method of manufacturing an improved adsorbent 1~69089 comprises the steps of: ion-exchanging and carrying Cu(II) in a cation exchange site of the zeolite;
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method; heating the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing Cu~II) and the remaining Cu(II) salt with a reducing gas such as H2 or C0 to obtain Cu(I) and a Cu(I) salt. After Cu(II) is carried by ion exchanging, the Cu(II) salt is preferably dispersed and carried by the impregnation method.
This invention can be more fully ùnderstood from the following detailed description when taken in con~unction with the accompanying drawings, in which:
Fig. 1 is a graph showing the relationship between the temperature and the adsorption amount in an experiment in Reference Example 1:
Figs. 2 and 3 are graphs showing the relationships between the temperatures and the adsorption amounts in experiments in Examples 1 and 2 respectively:
Fig. 4 is a graph showing the relationship be-tween the temperature and the adsorption amount in an experiment in Comparative Example 1:
Fig. 5 is a graph showing the relationship between the MC12 impregnation amount and C0 and C02 adsorption amounts in Cu(I)Y + MC12 in Example 3:
Fig. 6 is a graph showing the relationship between the CuCl impregnation amount and C0 and C02 adsorption :, :
" ' , ' , lZ690~9 amounts in Cu(I)Y + CuCl in Example 4;
Fig 7 is a graph showing the relationship be-tween the Cû recovery ratio and the Cû purity in the experiments in Reference Examples 2 to 4; and Fig. 8 is a graph showing the relationship between the C0 recovery ratio and the C0 purity in experiments in Examples 6 to 8.
A zeolite carrier may be of A, X, Y, or mordenite type if it has a silica/alumina ratio of 10 or less.
If the silica/alumina ratio is decreased, the amount of a metal carried by an ion exchange method is increased, so that a C0 adsorption amount tends to be increased.
However, the resultant zeolite has poor resistance to acids and a high hydrophilic level. As a result, a moisture adsorption amount and hence a C02 adsorption amount tend to be increased. Since the zeolite has poor resistance to acids if the silica/alumina ratio is reduced, a pH of a solution must be controlled to prepare an adsorbent by the ion exchange method and then the impregnation method. In consideration of the chemical properties of zeolite, the silica/alumina ratio must be 10 or less. A preferable zeolite is a Y type zeolite with a silica/alumina ratio of about 5.
Cu(I), to be carried by the ion exchange method on a cation exchange site of zeolite, has an ion exchange ratio of 50% or more, and preferably 70% or more because an increase in ion exchange ratio increases the C0 , ~
.~,.~,, , ,. ~ .
lZ69089 adsorption amount. A small amount of Cu(II) or Cu in addition to Cu(I) may be contained in the cation exchange site.
A metal salt carried in the pores of zeolite by an impregnation method is selected from salts of Cu(I), Fe, Zn, Ni, and Mg. When the amount of the metal salt carried in zeolite is increased, the C02 adsorption amount is reduced. As a result, a ratio of the C0 adsorption amount to the C02 adsorption amount is larger lû than that of the basic Cu(Y) zeolite. The metal salt is preferably a halide, and more preferably a chloride such as CuCl, FeC13, ZnCl2, NiCl2, or MgCl2. CuCl may be obtained by reducing CuC12 with a reducing gas.
Alternatively, CuC12 is heated and decomposed to produce CuCl.
CuCl has a Cû/C02 adsorption amount ratio exceeding 1 at room temperature and is most preferable. If zeolite is impregnated with CuCl, the amount of CuCl is approximately in proportion to the C02 adsorption amount. However, in association with the C0 adsorption amount, an increase in Cu increases the C0 adsorption amount, and the pores are covered by the impregnation of CuCl to reduce the surface area of zeolite. The impregnation amount of CuCl falls within the range where the equilibrium adsorption amounts of C0 and C02 at 20C
are equal for 1 9 of thq ion exchange Cu(I) zeolite, i.e., preferably 0.8 to 2.5 mmol/g, and most preferably :
.~. .
~Z69089 1.0 to 2.0 mmol/g wherein a C0/C02 ratio is 1.1 or more. Fig. 6 is a graph showing an impregnation amount ratio of CuCl/CuY and the C0 and C02 adsorption amounts (20C) in Cu(I)Y + CuCl. Cu(I)Y + CuCl is prepared by reducing Cu(II)Y + CuC12 in a C0 gas atmosphere at a temperature of 250C for an hour.
The present inventors assumed methods o~ carrying a salt in zeolite having a silica/alumina ratio of 10 or less:
(1) an ion exchange method utilizing an ion exchange function as a property of zeolite; and
Japanese Patent Disclosure (Kokai) No. 58-15~517 discloses a solid adsorbent containing copper halide(I) and active carbon as a C0 adsorbent. However, stable use of this adsorbent for a long period of time has never been reported. U.S.P, No. 4,019,879 describes an adsorbent prepared by carrying Cu(I) in zeolite whose silica/alumina ratio is as high as 20 to 200.
In zeolite having such a high silica/alumina ratio, it is known that the number of cations capable of ion exchange tends to be reduced. It may be concluded that the C0 adsorption amount per unit weight is reduced.
A C0 desorption technique by the PSA method has ; been developed as a typical adsorption method.
For example, Japanese Patent Disclosure (Kokai) 2û No. 59-22625 describes a two-step treatment for performing a PSA to eliminate moisture and C02 in a pretreatment step. Japanese Patent Disclosure (Kokai) No. 59-26121 describes a two-step treatment of sepa-rating C0 from a converter gas. According to this ~ 25 method, mordenite is used as an adsorbent, and Cû2-PSA
t and C0-PSA are separately performed. These conventional j~ proposals indicate that the adsorbents have a large C0 ' ~IZ69089 adsorption amount near room temperature. However, the C2 adsorption amount is larger than the C0 adsorption amount. In order to separate C0 from a gas mixture containing C02, C02 is separated from the gas mixture in the pretreatment, and then Co is separated by the C0-PSA process.
It is a first object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein C0 can be selectively separated from a gas mixture containing mainly C0, C02, and N2 by a single step at a PSA temperature closer to room temperature, so that the separated C0 can be condensed.
It is a second object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein a large amount of gas can be treated by a smaller amount of adsorbent.
It is a third object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein an adsorption tower and a treating gas need not be heated, thus reducing the operation cost.
It is a fourth object of the present invention to provide an adsorbent and a method of manufacturing the same, wherein a material for a switching valve and the like in a PSA apparatus need not be a heat-resistant material.
According to an aspect of the present invention, lZ69089 there is provided a selective adsorbent for C0, comprising: mainly Cu(I) carried in an ion exchange site of zeolite having a silica/alumina ratio of not more than 10 at an ion exchange ratio of not less than 50% and preferably not less than 70%; and a salt of at least one metal selected from the group consisting of Cu(I), Fe, Zn, Ni, and Mg, the salt being dispersed and carried in pores of the zeolite, the salt being more preferably a Cu(I) salt and most preferably a salt containlng as a major constituent a halide such as a Cu(I) chloride, and the metal salt being contained in a total amount of 0.8 mmol to 2.5 mmol and more preferably l.û mmol to 2.û mmol per gram of ion-exchange Cu(I) zeolite. Carbon monoxide can be selectively separated by the adsorbent at a temperature of 40 to I00C.
According to another aspect of the present invention, there is provided a method of manufacturing the above adsorbent, comprising the steps of:
ion-exchanging and carrying Cu(II) in a cation exchange site of the zeolite; dispersing and carrying mainly a Cu(II) salt in pores of the zeolite by an impregnation method; and reducing the Cu(II) and the Cu(II) salt with a reducing gas such as H2 or C0 to obtain mainly Cu(I) and a Cu(I) salt. After Cu(II) is carried by ion exchanging, the Cu(II) salt is preferably dispersed and carried by the impregnation method.
A method of manufacturing an improved adsorbent 1~69089 comprises the steps of: ion-exchanging and carrying Cu(II) in a cation exchange site of the zeolite;
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method; heating the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing Cu~II) and the remaining Cu(II) salt with a reducing gas such as H2 or C0 to obtain Cu(I) and a Cu(I) salt. After Cu(II) is carried by ion exchanging, the Cu(II) salt is preferably dispersed and carried by the impregnation method.
This invention can be more fully ùnderstood from the following detailed description when taken in con~unction with the accompanying drawings, in which:
Fig. 1 is a graph showing the relationship between the temperature and the adsorption amount in an experiment in Reference Example 1:
Figs. 2 and 3 are graphs showing the relationships between the temperatures and the adsorption amounts in experiments in Examples 1 and 2 respectively:
Fig. 4 is a graph showing the relationship be-tween the temperature and the adsorption amount in an experiment in Comparative Example 1:
Fig. 5 is a graph showing the relationship between the MC12 impregnation amount and C0 and C02 adsorption amounts in Cu(I)Y + MC12 in Example 3:
Fig. 6 is a graph showing the relationship between the CuCl impregnation amount and C0 and C02 adsorption :, :
" ' , ' , lZ690~9 amounts in Cu(I)Y + CuCl in Example 4;
Fig 7 is a graph showing the relationship be-tween the Cû recovery ratio and the Cû purity in the experiments in Reference Examples 2 to 4; and Fig. 8 is a graph showing the relationship between the C0 recovery ratio and the C0 purity in experiments in Examples 6 to 8.
A zeolite carrier may be of A, X, Y, or mordenite type if it has a silica/alumina ratio of 10 or less.
If the silica/alumina ratio is decreased, the amount of a metal carried by an ion exchange method is increased, so that a C0 adsorption amount tends to be increased.
However, the resultant zeolite has poor resistance to acids and a high hydrophilic level. As a result, a moisture adsorption amount and hence a C02 adsorption amount tend to be increased. Since the zeolite has poor resistance to acids if the silica/alumina ratio is reduced, a pH of a solution must be controlled to prepare an adsorbent by the ion exchange method and then the impregnation method. In consideration of the chemical properties of zeolite, the silica/alumina ratio must be 10 or less. A preferable zeolite is a Y type zeolite with a silica/alumina ratio of about 5.
Cu(I), to be carried by the ion exchange method on a cation exchange site of zeolite, has an ion exchange ratio of 50% or more, and preferably 70% or more because an increase in ion exchange ratio increases the C0 , ~
.~,.~,, , ,. ~ .
lZ69089 adsorption amount. A small amount of Cu(II) or Cu in addition to Cu(I) may be contained in the cation exchange site.
A metal salt carried in the pores of zeolite by an impregnation method is selected from salts of Cu(I), Fe, Zn, Ni, and Mg. When the amount of the metal salt carried in zeolite is increased, the C02 adsorption amount is reduced. As a result, a ratio of the C0 adsorption amount to the C02 adsorption amount is larger lû than that of the basic Cu(Y) zeolite. The metal salt is preferably a halide, and more preferably a chloride such as CuCl, FeC13, ZnCl2, NiCl2, or MgCl2. CuCl may be obtained by reducing CuC12 with a reducing gas.
Alternatively, CuC12 is heated and decomposed to produce CuCl.
CuCl has a Cû/C02 adsorption amount ratio exceeding 1 at room temperature and is most preferable. If zeolite is impregnated with CuCl, the amount of CuCl is approximately in proportion to the C02 adsorption amount. However, in association with the C0 adsorption amount, an increase in Cu increases the C0 adsorption amount, and the pores are covered by the impregnation of CuCl to reduce the surface area of zeolite. The impregnation amount of CuCl falls within the range where the equilibrium adsorption amounts of C0 and C02 at 20C
are equal for 1 9 of thq ion exchange Cu(I) zeolite, i.e., preferably 0.8 to 2.5 mmol/g, and most preferably :
.~. .
~Z69089 1.0 to 2.0 mmol/g wherein a C0/C02 ratio is 1.1 or more. Fig. 6 is a graph showing an impregnation amount ratio of CuCl/CuY and the C0 and C02 adsorption amounts (20C) in Cu(I)Y + CuCl. Cu(I)Y + CuCl is prepared by reducing Cu(II)Y + CuC12 in a C0 gas atmosphere at a temperature of 250C for an hour.
The present inventors assumed methods o~ carrying a salt in zeolite having a silica/alumina ratio of 10 or less:
(1) an ion exchange method utilizing an ion exchange function as a property of zeolite; and
(2) the ion exchange method and an impregnation method widely used in catalyst preparations.
According to the extensive studies of the present inventors, by only the ion exchange method, the metal ions were exchanged with cations such as Na , K , or Ca 2 present to reinforce the charge at the Al point in the atoms constituting the zeolite crystal. Although the metal ions were uniformly dispersed, the amount thereof was limited by the silica/alumina ratio. An ion exchange ratio was 7û to 9û% by normal manipulation.
As a result, it was found that the adsorption characteristics could not be much improved as compared with those of the conventional proposals.
By only the impregnation method, some of cations such as Na , K , and Ca2 were exchanged with the metal ions described above. However, most of the cations were . ~
, ~ ~
, .
il26908g left in the crystal lattice of zeolite to fail utilization of the ion exchange function of the zeolite. and at the same time, the metal ions were not uniformly dispersed, as compared with the ion exchange method Irregular dispersion on the outer surface and pores of the zeolite influenced the adsorption properties The carrying amount of the metal ions could be easily controlled as compared with that according to the ion exchange method. However, the adsorption properties were found to be worse than those obtained by the ion exchange method.
Based upon the above experiment results, the present inventors combined the ion exchange method and the impregnation method and found an adsorbent capable of selectively separating C0 in one step at a temperature closer to room temperature under the condition (Cû adsorption amount) > (C02 adsorption amount).
Extensive studies were made by using the resultant adsorbent and a PSA test apparatus, assuming a normal converter gas in a steelmaking plant. It was found that an operation temperature required for 90 to 95% of product C0 purity and 70~0 or more of C0 recovery is 40C or more. Similarly, in order to obtain 98% or more of purity and 70% or more of C0 recovery, the required operation temperature was found to fall within the temperature range of 60C to 100C.
~Z690B9 g Even if the PSA is performed at a temperature of 100C or more by using the resultant adsorbent, no problems occur from the viewpoint of the desorption function. On the contrary, the CO desorption function is improved. However, if the operation temperature exceeds lOûC, the CO adsorption amount is gradually reduced, and the adsorption amount per unit amount of the gas to be treated is increased. In addition, energy for heating an adsorption tower and/or the gas to be treated is required. The amount of energy must be increased upon an increase in operation temperature.
From an economical viewpoint, it is not suitable to set the operation temperature to be 100C or more.
By using the resultant adsorbent, CO desorption can be achieved at a temperature of less than 40C.
However, this temperature is not practical. If the operation temperature is less than 40C, the adsorption properties are not degraded. However, properties in purging and desorption steps repeated in the PSA process are degraded. As a result, the purity and the recovery ratio of CO are impaired very much. A gas to be treated is adiabatic compressed by a compressor at the inlet port of the PSA apparatus in the range of 0.5 kg/cm3G
to 7 kg/cm3G to increase a temperature of the gas, thereby setting the gas at a predetermined adsorption temperature and hence the absorbent within the range of 40C to 100C.
lZ6908g According to this method, an external heating device can be eliminated, thus achieving an inexpensive process. Since the PSA operation temperature is closer to room temperature, energy for heating the adsorption tower and/or the gas to be treated need not be used, thereby greatly reducing the operation cost.
One method of manufacturing a selective adsorbent for CO comprises the steps of carrying Cu(II) in a cation exchange site of the zeolite by an ion exchange method, dispersing and carrying a salt of at least one metal selected from the group consisting of CutII), Fe, Zn, Ni, ano Mg in pores of the zeolite, and reducing Cu(II) and a CutII) salt with a reducing gas such as H2 or CO to obtain Cu(I) and a CutI) salt. Impregnation preferably follows ion-exchanging.
According to this method, it is preferable that chemically stable Cu(II) is carried in the zeolite.
A method of manufacturing an improved adsorbent comprises the steps of: ion-exchanging and carrying CutII) in a cation exchange site of the zeolite:
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method: heating the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing Cu(II) and the remaining Cu(II) salt with a reducing gas such as H2 or CO to obtain Cu(I) and a Cu(I) salt. Impregnation preferably follows ion-exchanging.
.
; , . ~ :
- ' :12t~gO89 Acco~ding to this method, the Cu(II) salt carried by impregnation is heated in a temperature range where Cu(II) salt is decomposed into a Cu(I) salt.
Thereafter, the Cu(II) salt is reduced with a reducing gas. Therefore, the Cu(II) salt can be easily converted into the Cu(I) salt stable in air. In the reduction step, generation of a toxic gas such as halogenated hydrogen is limited. ~t the same time, the Cu(II) carried by ion exchanging in the zeolite is reduced, thereby easily performing reduction. CuC12 carried by Cu(II)Y is heated in the temperature range of a temperature higher than a temperature at which a chemical reaction CuC12 ~ CuCl + C12 is initiated to a temperature at which a vapor pressure of CuC12 is 760 mmHg, i.e., in the range of 350C to 590C, and preferably 400C to 500C.
The adsorbent prepared by ion-exchanging and impregnatlon has a larger C0 adsorption amount and a smaller C02 adsorption amount than those of the absorbent prepared by only ion-exchanging or impregna-tion, For this reason, the C0 adsorption amount is larger than the C02 adsorption amount at room temperature (about 20C). This tendency typically occurs when the temperature is increased to 6ûC
and preferably 100C. Therefore, the C0 selective adsorption function is greatly improved, and the desorption function is also improved. The N2 adsorption ~'' '' '' ~ ~ ' .
: - :
- - :
~Z69089 amount in this temperature range is very small and dûes not adversely affect the C0 selective adsorption function.
The adsorbent of the present invention has the following effects:
(1) In the temperature range where the C0 adsorption amount is larger than the C02 adsorption amount, C0 can be separated from a gas containing both C0 and C02 in a single step, thus improving the desorption property.
t2) Since the C0 adsorption amount is large, the required adsorbent amount per unit amount of gas to be treated is reduced.
According to the extensive studies of the present inventors, by only the ion exchange method, the metal ions were exchanged with cations such as Na , K , or Ca 2 present to reinforce the charge at the Al point in the atoms constituting the zeolite crystal. Although the metal ions were uniformly dispersed, the amount thereof was limited by the silica/alumina ratio. An ion exchange ratio was 7û to 9û% by normal manipulation.
As a result, it was found that the adsorption characteristics could not be much improved as compared with those of the conventional proposals.
By only the impregnation method, some of cations such as Na , K , and Ca2 were exchanged with the metal ions described above. However, most of the cations were . ~
, ~ ~
, .
il26908g left in the crystal lattice of zeolite to fail utilization of the ion exchange function of the zeolite. and at the same time, the metal ions were not uniformly dispersed, as compared with the ion exchange method Irregular dispersion on the outer surface and pores of the zeolite influenced the adsorption properties The carrying amount of the metal ions could be easily controlled as compared with that according to the ion exchange method. However, the adsorption properties were found to be worse than those obtained by the ion exchange method.
Based upon the above experiment results, the present inventors combined the ion exchange method and the impregnation method and found an adsorbent capable of selectively separating C0 in one step at a temperature closer to room temperature under the condition (Cû adsorption amount) > (C02 adsorption amount).
Extensive studies were made by using the resultant adsorbent and a PSA test apparatus, assuming a normal converter gas in a steelmaking plant. It was found that an operation temperature required for 90 to 95% of product C0 purity and 70~0 or more of C0 recovery is 40C or more. Similarly, in order to obtain 98% or more of purity and 70% or more of C0 recovery, the required operation temperature was found to fall within the temperature range of 60C to 100C.
~Z690B9 g Even if the PSA is performed at a temperature of 100C or more by using the resultant adsorbent, no problems occur from the viewpoint of the desorption function. On the contrary, the CO desorption function is improved. However, if the operation temperature exceeds lOûC, the CO adsorption amount is gradually reduced, and the adsorption amount per unit amount of the gas to be treated is increased. In addition, energy for heating an adsorption tower and/or the gas to be treated is required. The amount of energy must be increased upon an increase in operation temperature.
From an economical viewpoint, it is not suitable to set the operation temperature to be 100C or more.
By using the resultant adsorbent, CO desorption can be achieved at a temperature of less than 40C.
However, this temperature is not practical. If the operation temperature is less than 40C, the adsorption properties are not degraded. However, properties in purging and desorption steps repeated in the PSA process are degraded. As a result, the purity and the recovery ratio of CO are impaired very much. A gas to be treated is adiabatic compressed by a compressor at the inlet port of the PSA apparatus in the range of 0.5 kg/cm3G
to 7 kg/cm3G to increase a temperature of the gas, thereby setting the gas at a predetermined adsorption temperature and hence the absorbent within the range of 40C to 100C.
lZ6908g According to this method, an external heating device can be eliminated, thus achieving an inexpensive process. Since the PSA operation temperature is closer to room temperature, energy for heating the adsorption tower and/or the gas to be treated need not be used, thereby greatly reducing the operation cost.
One method of manufacturing a selective adsorbent for CO comprises the steps of carrying Cu(II) in a cation exchange site of the zeolite by an ion exchange method, dispersing and carrying a salt of at least one metal selected from the group consisting of CutII), Fe, Zn, Ni, ano Mg in pores of the zeolite, and reducing Cu(II) and a CutII) salt with a reducing gas such as H2 or CO to obtain Cu(I) and a CutI) salt. Impregnation preferably follows ion-exchanging.
According to this method, it is preferable that chemically stable Cu(II) is carried in the zeolite.
A method of manufacturing an improved adsorbent comprises the steps of: ion-exchanging and carrying CutII) in a cation exchange site of the zeolite:
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method: heating the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing Cu(II) and the remaining Cu(II) salt with a reducing gas such as H2 or CO to obtain Cu(I) and a Cu(I) salt. Impregnation preferably follows ion-exchanging.
.
; , . ~ :
- ' :12t~gO89 Acco~ding to this method, the Cu(II) salt carried by impregnation is heated in a temperature range where Cu(II) salt is decomposed into a Cu(I) salt.
Thereafter, the Cu(II) salt is reduced with a reducing gas. Therefore, the Cu(II) salt can be easily converted into the Cu(I) salt stable in air. In the reduction step, generation of a toxic gas such as halogenated hydrogen is limited. ~t the same time, the Cu(II) carried by ion exchanging in the zeolite is reduced, thereby easily performing reduction. CuC12 carried by Cu(II)Y is heated in the temperature range of a temperature higher than a temperature at which a chemical reaction CuC12 ~ CuCl + C12 is initiated to a temperature at which a vapor pressure of CuC12 is 760 mmHg, i.e., in the range of 350C to 590C, and preferably 400C to 500C.
The adsorbent prepared by ion-exchanging and impregnatlon has a larger C0 adsorption amount and a smaller C02 adsorption amount than those of the absorbent prepared by only ion-exchanging or impregna-tion, For this reason, the C0 adsorption amount is larger than the C02 adsorption amount at room temperature (about 20C). This tendency typically occurs when the temperature is increased to 6ûC
and preferably 100C. Therefore, the C0 selective adsorption function is greatly improved, and the desorption function is also improved. The N2 adsorption ~'' '' '' ~ ~ ' .
: - :
- - :
~Z69089 amount in this temperature range is very small and dûes not adversely affect the C0 selective adsorption function.
The adsorbent of the present invention has the following effects:
(1) In the temperature range where the C0 adsorption amount is larger than the C02 adsorption amount, C0 can be separated from a gas containing both C0 and C02 in a single step, thus improving the desorption property.
t2) Since the C0 adsorption amount is large, the required adsorbent amount per unit amount of gas to be treated is reduced.
(3) Energy for heating the adsorption tower and/or the gas to be treated need not be used to greatly reduce the operation cost.
(4) Since the treatment is carried out in a temperature range close to normal temperature, heat resistance of a switching valve and the like of the PSA apparatus need not be considered.
The selective adsorbent for C0 according to the present invention is applicable to: natural gases containing C0, C02, N2, or ~2: modified gases such as naphtha: gases refined from coal, coke, or heavy oil: steelmaking plant gases, especially a blast furnace gas and a converter gas; byproduct gases in an oil refining plant and a petrochemical plant.
~269089 _ 13 -The present invention will be described in more detail by way of reference examples, comparative examples, and examples.
Reference Example 1 A lN CuC12 solution was prepared. lû 9 cf Na Y
type zeolite (pellets having a diameter of 1.5 mm and a length of 5 mm and containing 20% of a binder) and 50 mQ of the lN CuCl solution were added to a 100-mQ
round-bottom flask. A condenser was mounted on the flask, and the mixture was heated by a mantle heater.
The mixture was refluxed at a temperature of 100C
for 2 hours. After the heated mixture was left to stand, the supernatant liquid was recovered by decantation. 50 m~ of lN CuC12 solution were added to the residue to repeat reflux. The reflux was repeated a total of five times. The zeolite was sufficiently washed with distilled water and was dried at llûC. The dried zeolite was baked in an electrical furnace at 550C for 2 hours to prepare an adsorbent.
2û The recovered supernatant liquid and a filtered liquid were mixed, and the resultant mixture was subjected to emission spectroanalysis so as to calculate the amount of Na, thereby measuring an ion exchange ratio of 86.5%.
The amount of Cu carried in the zeolite was 8.87%.
ûne gram of the resultant adsorbent was put into a 20-mQ sampling bottle and set in a constant-pressure ~; adsorption amount-measuring apparatus. The sampling ....
... , , : .
~Z6gO89 _ 14 -bottle was placed in a silicone oil tank and evacuated to a vacuum of 10 3 mmHg at a temperature of 250C for 2 hours, thereby drying the adsorbent. C0 gas ~99.9~
or more of purity) was supplied to the sampling bottle, and reduction was performed at atmospheric pressure and at 250C for an hour. After the reduction, the sampling bottle containing the reduced adsorbent was evacuated again to a vacuum of 10 3 mmHg at 250C for 2 hours.
The sampling bottle was cooled and placed in the silicone oil tank. The bottle was kept at a measuring temperature in the tank for 20 to 30 minutes.
He gas (99.9% or more of purity) at the atmospheric pressure was supplied to the sampling bottle to measure an adsorption amount and hence the capacity until adsorption equilibrium was reached. After the adsorption equilibrium was measured from 20C to 150C, the temperature was increased. After the measurement was completed, the adsorbent was heated at 250C and 10 3 mmHg for an hour to remove the absorbed gases, and was left to cool. The adsorption amounts of C0, C02, and N2 at atmospheric pressure were measured by using a gas to be measured. The adsorbent was then heated in a vacuum to remove the absorbed gases and was accurately measured. By using the measured weight, the equilibrium adsorption amount per unit weight was measured.
~26908g The test results are shown in Fig. 1. The C0 adsorption amount is larger than the C02 adsorption amount at temperatures higher than 50C. The ratio Co/Co2 is increased, and the C0 adsorption amount is gradually decreased according to an increase in temperature.
Example 1 Ten grams of Cu(II)Y type zeolite, ion-exchanged by the method described in Reference Example 1, were measured and put into a 100-mQ eggplant-type flask.
The flask was set in a rotary vacuum evaporator and evaporated at 95C or more. After the evaporation, the sample was cooled to room temperature.
Meanwhile, 8.3 9 of CuC12-2H20 were dissolved in water at room temperature to prepare a 20-mQ solution.
This solution was a substantially CuC12 saturated solution.
A capillary was mounted on a leak cock of the rotary vacuum evaporator, and the above solution was dripped 2 or 3 droplets at a time into the adsorbent while the eggplant-type flask was kept in a vacuum.
When the adsorbent was uniformly wet, dripping of the solution was stopped, and the internal pressure of the flask was set at atmospheric pressure. The sample impregnated with the solution was placed in a suction filter with a metal net. The remaining solution was poured on the sample. The sample was subjected to .lZ69085~
suction filtering for about 30 minutes, and then placed on a magnetic tray. The sample was dried naturally for 24 hours. After drying, the sample was dried in a vacuum drier at 110 for 3 hours, thereby preparing an adsorbent of the present invention. The amount of Cu carried in the adsorbent was 15.96 wt%.
Following the same procedures as in Reference Example 1), the resultant adsorbent (to be described as CutII)Y + CuC12) was reduced, and equibrium adsorption amounts of Cû, C02, and N2 were measured within the temperature range of 20C to lOûC.
The reduction reaction converted Cu(II)Y + CuC12 into Cu(I)Y + CuCl.
The results are shown in Fig. 2. The C0 and C02 equilibrium adsorption amounts of the adsorbent in Example 1 are respectively larger and smaller than those of the adsorbent of Reference Example 1 prepared by only ion-exchanging. Therefore, the sufficient C0 selective adsorption capacity is obtained in the temperature range up to 100C.
Example 2 Following the same procedures as in Example 1 except that CuBr2 was used in place of CuC12-2H20, 11.2 9 of CuBr2 were dissolved in water at room temperature to prepare a 20-m2 solution. The resultant adsorbent (Cu(II)Y + CuBr2: the amount of Cu carried in a zeolite was 16.42 wt%) was reduced in the same manner ~z6soas as described above in Reference Example ~. C0 and C2 equilibrium adsorption amounts were measured.
The reduction reaction converted Cu(II)Y + CuBr2 into Cu~I)Y + CuBr.
The test results are shown in Fig. 3. As is apparent from these results, a sufficient C0 selective adsorption capacity is realized in the temperature range of room temperature to 100C in the same manner as in Example 1.
Comparative Example 1 Following the procedures as in Example 1, an Na Y type zeolite carrying CuC12, not by ion-exchanging as in Reference Example 1 but by impregnation as in Example 1 to prepare an adsorbent (NaY + CuC12; the amount of Cu carried in the zeolite was 11.93 wt%), was reduced by the same method as in Reference Example 1.
C0 and C02 equilibrium adsorption amounts were measured.
The reduction reaction converted NaY + CuC12 into NaY + CuCl.
The results are shown in Fig. 4, The C0 selective adsorption capacity of the adsorbent prepared by only impregnation was insufficient and is poorer than that of the adsorbent prepared by only ion-exchanging in Reference Example 1.
Example 3 Cu(II)Y was impregnated with predetermined amounts of FeC13, ZnC12, NiC12, and MgC12 and was reduced by 12690l99 the same method as in Reference Example 1. CO and C02 adsorption amounts and a CO/C02 ratio were measured.
The reduction reaction converted Cu(II)Y + MC12 into Cu(I)Y + MC12. MCl2 was a metal chloride. The results with adsorbents containing metal chlorides MnC12, CaC12, and BaC12 excluded from those of the present invention and an adsorbent without a metal chloride are shown in Table 1 and Fig. 5. The selectivity ratio of CO/C02 of the present invention is higher than that of Cu(I)Y not impregnated with a metal chloride, as is apparent from Table 1.
lZ69089 - lg -Table 1 Measurement Representing Amounts of Various Metal Chlorides Impregnated into Cu(I)Y and C0/C02 Adsorption Amounts Metal Impreg- C0 Adsorp- C0 Chloride nation tion Amount Adsorp- Selec Amount at 20C ption tivity MC12 (NmQ/g) Amount Cu(I)Y at 20C
(mmol/g) (Nm~/g) Present FeCl 1.533 25.70 34.73 0.740 Invention 3 Present ZnC12 1.580 31.58 36.18 0.873 Invention _ Present NiCl 1.424 27.98 38.45 0.728 Invention 2 Present MgC12 2.158 22.04 26.75 0.824 Invention Compar- MnC12 1.475 27.54 41.88 0.658 Example _ Compar- CaC12 1.292 23.45 43.02 0.545 Example ative BaC12 0.933 23.46 46.83 0.501 Example ence Cu(I)Y _ 38.24 57.99 0.659 Example _ Example 4 A CuC12 impregnation amount per gram of Cu(II)Y
was changed. Following the same procedures as in Reference Example 1, reduction was performed, and C0 and C02 adsorption amounts (20C) of Cu(I)Y ~ CuC12 were measured. The results are shown in Fig. 6.
1~:69089 The Co adso~ption amount exceeds the C02 adso~ption amount when 0.~ mmol/g to 2.5 mmol/g of CuC12 is contained. The CO/C02 ratio is 1.1 or more when 1.0 to 2.0 mmol/g of CuC12 is contained.
Example 5 Ten grams of CUtII)y + CuC12 prepared by the same procedures as in Example 1 were filled in a glass tube having a diameter of ~2 mm, and the glass tube was set in an annular electric furnace. The height of the Cu(II)Y + CuC12 in the glass tube was about 2 cm.
N2 gas was supplied at a flow rate of l.û NQ/min, and the Cu(II)Y + CuC12 was heated to a predetermined temperature and kept thereat for an hour. After heating, the Cu(II)Y + CuC12 was cooled to room temperature, and the resultant adsorbent was removed.
One gram of the adsorbent was placed in a 20-m~
sampling bottle, and the bottle was set in a constant pressure adsorption amount-measuring apparatus.
The adsorbent was heated to a temperature of 250C
in a vacuum of 10 3 mmHg for 2 hours.
Subsequently, the sampling bottle was placed in a silicone oil tank and kept at 20C. He gas (99.9% or more of purity) at the atmospheric pressure was supplied to the bottle. The adsorption amounts and hence the capacity were measured until adsorption equilibrium was reached. After measurement, the bottle was heated at 250C and 10 3 mmHg for an hour. The sample was then ,. . .
lZ690~5~
cooled, and the sampling bottle was placed in the silicone oil tank at 20C. C0 gas (99.9% or more) was supplied to the sampling bottle to measure the equilibrium adsorption amount at the atmospheric pressure. This adsorption amount was the one before reduction.
The silicone oil tank was heated and kept at 250C, and the sample was reduced in the C0 atmosphere for 60 minutes. After reduction, C0 was removed from the sample such that the sample was heated to 250C
in a vacuum of 10 3 mm Hg for 2 hours. The sample was then left to cool. The cooled sample in the bottle was placed in the silicone oil tank and kept at 2ûC. Under this condition, C0 gas ~99.9% or more of purity) was supplied to the bottle, and the C0 equilibrium adsorp-tion amount at atmospheric pressure was measured. This adsorption amount was the one after reduction. Simi-larly, the sample was heated in a vacuum to remove C0, and then C02 equilibrium adsorption amount at 20C and the atmospheric pressure was measured. After the sample was heated in a vacuum to remove C02, the sample was weighed. The equilibrium adsorption amount per unit weight was calculated by using the measured weight.
C0 equilibrium adsorption amounts before and after the reduction, C02 equilibrium adsorption amounts after the reduction, and selectivity ratio of C0/C02 at temperatures of 35û, 400, 450, 5ûû, and 550C are shown in Table 2. For comparison, the measurement results at 600C and 250C (the latter is the pretreatment temperature of equilibrium adsorption amount measurement) are also shown. As is apparent from Table 2, when the heating temperature is increased, the C0 equilibrium adsorption amount before the reduction is increased, and the impregnated and carried CuC12 is gradually converted into CuCl having a C0 adsorption capacity.
Up to the heating temperature of 5ûûC, the C0 equilibrium adsorption amounts before and after the reduction are increased. However, when the heating temperature exceeds 500C, the C0 equilibrium adsorption amount is decreased, and the C02 equilibrium adsorption amount after the reduction is increased. It is thus found that the impregnated and carried CuC12 and the converted CuCl are evaporated from the adsorbent.
12~gOB9 Table 2 Equilibrium Adsorption Amount Measurement Data After Heating of Cu(II)Y + CuC12 Heating C0 Adsorp- C0 Adsorp- C02 C0/C02 Temper- tion tion Adsorp- Selec-ature Amount Amount tion tivity (C) at 20C at 20C Amount After After After at 20C Reduc-Reduction Reduction After tion (Nm~/g) (Nm/g) RteidOnc-(NmQ/g) Present 35014.56 49.53 39.22 1.263 Invention Present 40020.59 51.95 ¦42.54 1.221 Invention l Present 45025.27 53.14 42.32 1.256 Invention .
Present 50033.27 55.41 43.42 1.276 Invention Present 55023.58 53.89 43.65 1.235 Invention Compar-ative 2508.43 44.64 35.36 1.262 Example Compar-ative 60018.53 52.11 47.05 1.108 ~ample Reference Example 2 A PSA test apparatus having four adsorption towers made of SUS 304 stainless steel each having a size of 2" x 800 mm was used to obtain a relationship between the recovery ratio and the C0 purity of the recovered gas by using the adsorption temperature as a parameter.
Each tower comprised a mantle heater with a thermostat 12690~9 _ ~4 _ to keep the interior temperature within the range of 10C cf the preset temperature.
A lN CuC12 solution was prepared, and 10 9 of NaY
type zeolite (in the form of pellets having a diameter of 1.5 mm and a length of 5 mm and including 20% of a binder) and 50 m~ of lN CuC12 solution were poured in a 100-m~ round-bottom flask. A condenser was mounted on the round-bottom flask, and the flask was heated by a mantle heater at 100C for 2 hours to reflux the mixture therein. After the flask was left to stand, the supernatant liquid was removed by decantation.
Thereafter, another 50 mQ of the lN CuC12 solution were added to the round bottom flask, and the mixture was refluxed again, following the same procedures as described above. The reflux was repeated a total of five times. The zeolite was sufficiently washed with distilled water, dried at 110C, and pulverized.
The zeolite powder was then sintered in an electric furnace at 550C for 2 hours to prepare an adsorbent.
The recovered supernatant and filtered solutions were mixed, and the solution mixture was subjected to emission spectroanalysis, thereby measuring the Na amount and hence an ion exchange ratio of 86.5%.
The amount of Cu carried per unit weight of adsorbent was 8.87 wt%.
One kilogram of 1/16" granular pellets (including 20% of a granulating agent) of the resultant Cu(II) ~Z69089 Y type zeolite were filled in each tower and gases were desorbed from the zeolite by heating at 250 and 50 Torr for about 5 hours. Pure C0 gas was filled in each tower and then supplied thereto at a flow rate of about 1 Q/min for about 2 hours, thereby reducing Cu(II)Y
into Cu(I)Y. The 4-tower PSA apparatus generally repeats a cycle of adsorption, purging, desorption, and compression.
Desorption and refinement of a gas sample assumed as a converter gas having the following composition were tested by using the 4-tower PSA apparatus.
Gas Composition: C0 : 74.5%
C2 : 14.0%
H2 : 1.0%
N2 : 10.5%
An adsorption temperature was 165 + 10C, an adsorp-tion pressure was 1 kg/cm2G, and a gas desorbing pressure was 50 Torr. A ratio of the purge gas to the gas to be removed, and a source gas flow rate were changed, and a gas flow speed in the tower was kept substantially constant. A relationship between the C0 recovery ratio and the C0 purity of the recovered gas was determined.
As an example, if the supply gas flow rate was 0.76 Q/min, and the purge amount/desorbing amount ratio was 0.73, the C0 recovery ratio was 73%, and the recovered gas composition was as follows:
126908g C0 : 96.2%
C2 : 3 0%
N2 : 0-7%
H2 : 0.1%
The relationship between the C0 purity and the C0 recovery ratio is indicated by the broken line in Fig. 7.
Reference Example 3 Following the same procedures with the same apparatus as in Reference Example 2, except that an adsorption temperature was set at 210 + 10C, the relationship between the recovery ratio and the product C0 purity was determined.
As an example, if the supply gas flow rate was 0.70 ~/min, and the purge amount/desorbing amount ratio was 0.74, the C0 recovery ratio was 72%, and the recovered gas composition was as follows:
C0 : 98.5%
2 : 1.0%
; 20 N2 0-4%
H2 : 0.1%
The relationship between the product C0 purity and the recovery ratio is indicated by the solid line in Fig. 7.
As is apparent from the above test results, when ; 25 the adsorption temperature is increased, the product C0 ~ impurity is increased with respect to an identical C0 ; recovery ratio. At the same time, by decreasing the C0 "
, ' :
, ;.
lZ69089 recovery ratio to about 50%, the product C0 purity is increased to 99% or more.
Reference Example 4 Following the same procedures with the same apparatus as in Reference Example 2, except that an adsorption temperature was set at 135 + 10C, the relationship between the recovery ratio and the product C0 purity was determined.
As an example, if the supply gas flow rate was 0.72 ~/min, and the purge amount/desorbing amount ratio was 0.73, the C0 recovery ratio was 72%, and the recovered gas composition was as follows:
C0 : 93.1%
C2 : 5.2%
N2 1.4%
. H2 0-3%
: The relationship between the product C0 purity and the recovery ratio is indicated by the alternate long and short dashed line in Fig. 7.
As is apparent from the above results, when the adsorption temperature is 150C or less, the product ~ C0 purity is decreased below 95% with respect to the : recovery ratio of about 70%. In order to maintain the product C0 purity to be about 98%, the recovery ratio must be reduced to about 30%.
Example 6 ~ Ten grams of Cu(II) Y type zeolite (pellets having ':~
~6go8~
a diameter of 1.5 mm and a length of 5 mm) ion-exchanged by the method described in Reference Example 2 were measured and put into a lOû-mQ eggplant-type flask.
The flask was set in a rotary vacuum evaporator and evaporated at 95C or more. After the evaporation, the sample was cooled to room temperature.
Meanwhile, 8.3 9 of CuC12-2H2û were dissolved in water at room temperature to prepare a 20-mQ solution.
This solution was a substantially CuC12 saturated solution. A capillary was mounted on a leak cock of the rotary vacuum evaporator, and the abbve solution was dripped 2 or 3 droplets at a time into the adsorbent while the eggplant-type flask was kept in a vacuum.
When the adsorbent was uniformly wet, dripping of the solution was stopped. The internal pressure of the flask was set at atmospheric pressure. The sample impregnated with the solution was placed in a suction filter with a metal net. The remaining solution was poured on the sample. The sample was subjected to suction filtering for about 3û minutes, and then placed on a magnetic tray. The sample was dried naturally for 24 hours. After drying with air, the sample was dried in a vacuum drier at 110 for 3 hours, thereby preparing an adsorbent of the present invention. The amount of Cu carried in the adsorbent was 15.96 wt%.
Thereafter, 1,250 9 of 1/16" granular pellets (containing 20% of a granulating agent) of the adsorbent ~z~g~
(referred to as Cu(II)Y + CuC12) were filled in each tower in the same apparatus as in Reference Example 2, and an adsorption temperature was set to be 90 ~ 10C.
Following the same procedures as in Reference Example 2
The selective adsorbent for C0 according to the present invention is applicable to: natural gases containing C0, C02, N2, or ~2: modified gases such as naphtha: gases refined from coal, coke, or heavy oil: steelmaking plant gases, especially a blast furnace gas and a converter gas; byproduct gases in an oil refining plant and a petrochemical plant.
~269089 _ 13 -The present invention will be described in more detail by way of reference examples, comparative examples, and examples.
Reference Example 1 A lN CuC12 solution was prepared. lû 9 cf Na Y
type zeolite (pellets having a diameter of 1.5 mm and a length of 5 mm and containing 20% of a binder) and 50 mQ of the lN CuCl solution were added to a 100-mQ
round-bottom flask. A condenser was mounted on the flask, and the mixture was heated by a mantle heater.
The mixture was refluxed at a temperature of 100C
for 2 hours. After the heated mixture was left to stand, the supernatant liquid was recovered by decantation. 50 m~ of lN CuC12 solution were added to the residue to repeat reflux. The reflux was repeated a total of five times. The zeolite was sufficiently washed with distilled water and was dried at llûC. The dried zeolite was baked in an electrical furnace at 550C for 2 hours to prepare an adsorbent.
2û The recovered supernatant liquid and a filtered liquid were mixed, and the resultant mixture was subjected to emission spectroanalysis so as to calculate the amount of Na, thereby measuring an ion exchange ratio of 86.5%.
The amount of Cu carried in the zeolite was 8.87%.
ûne gram of the resultant adsorbent was put into a 20-mQ sampling bottle and set in a constant-pressure ~; adsorption amount-measuring apparatus. The sampling ....
... , , : .
~Z6gO89 _ 14 -bottle was placed in a silicone oil tank and evacuated to a vacuum of 10 3 mmHg at a temperature of 250C for 2 hours, thereby drying the adsorbent. C0 gas ~99.9~
or more of purity) was supplied to the sampling bottle, and reduction was performed at atmospheric pressure and at 250C for an hour. After the reduction, the sampling bottle containing the reduced adsorbent was evacuated again to a vacuum of 10 3 mmHg at 250C for 2 hours.
The sampling bottle was cooled and placed in the silicone oil tank. The bottle was kept at a measuring temperature in the tank for 20 to 30 minutes.
He gas (99.9% or more of purity) at the atmospheric pressure was supplied to the sampling bottle to measure an adsorption amount and hence the capacity until adsorption equilibrium was reached. After the adsorption equilibrium was measured from 20C to 150C, the temperature was increased. After the measurement was completed, the adsorbent was heated at 250C and 10 3 mmHg for an hour to remove the absorbed gases, and was left to cool. The adsorption amounts of C0, C02, and N2 at atmospheric pressure were measured by using a gas to be measured. The adsorbent was then heated in a vacuum to remove the absorbed gases and was accurately measured. By using the measured weight, the equilibrium adsorption amount per unit weight was measured.
~26908g The test results are shown in Fig. 1. The C0 adsorption amount is larger than the C02 adsorption amount at temperatures higher than 50C. The ratio Co/Co2 is increased, and the C0 adsorption amount is gradually decreased according to an increase in temperature.
Example 1 Ten grams of Cu(II)Y type zeolite, ion-exchanged by the method described in Reference Example 1, were measured and put into a 100-mQ eggplant-type flask.
The flask was set in a rotary vacuum evaporator and evaporated at 95C or more. After the evaporation, the sample was cooled to room temperature.
Meanwhile, 8.3 9 of CuC12-2H20 were dissolved in water at room temperature to prepare a 20-mQ solution.
This solution was a substantially CuC12 saturated solution.
A capillary was mounted on a leak cock of the rotary vacuum evaporator, and the above solution was dripped 2 or 3 droplets at a time into the adsorbent while the eggplant-type flask was kept in a vacuum.
When the adsorbent was uniformly wet, dripping of the solution was stopped, and the internal pressure of the flask was set at atmospheric pressure. The sample impregnated with the solution was placed in a suction filter with a metal net. The remaining solution was poured on the sample. The sample was subjected to .lZ69085~
suction filtering for about 30 minutes, and then placed on a magnetic tray. The sample was dried naturally for 24 hours. After drying, the sample was dried in a vacuum drier at 110 for 3 hours, thereby preparing an adsorbent of the present invention. The amount of Cu carried in the adsorbent was 15.96 wt%.
Following the same procedures as in Reference Example 1), the resultant adsorbent (to be described as CutII)Y + CuC12) was reduced, and equibrium adsorption amounts of Cû, C02, and N2 were measured within the temperature range of 20C to lOûC.
The reduction reaction converted Cu(II)Y + CuC12 into Cu(I)Y + CuCl.
The results are shown in Fig. 2. The C0 and C02 equilibrium adsorption amounts of the adsorbent in Example 1 are respectively larger and smaller than those of the adsorbent of Reference Example 1 prepared by only ion-exchanging. Therefore, the sufficient C0 selective adsorption capacity is obtained in the temperature range up to 100C.
Example 2 Following the same procedures as in Example 1 except that CuBr2 was used in place of CuC12-2H20, 11.2 9 of CuBr2 were dissolved in water at room temperature to prepare a 20-m2 solution. The resultant adsorbent (Cu(II)Y + CuBr2: the amount of Cu carried in a zeolite was 16.42 wt%) was reduced in the same manner ~z6soas as described above in Reference Example ~. C0 and C2 equilibrium adsorption amounts were measured.
The reduction reaction converted Cu(II)Y + CuBr2 into Cu~I)Y + CuBr.
The test results are shown in Fig. 3. As is apparent from these results, a sufficient C0 selective adsorption capacity is realized in the temperature range of room temperature to 100C in the same manner as in Example 1.
Comparative Example 1 Following the procedures as in Example 1, an Na Y type zeolite carrying CuC12, not by ion-exchanging as in Reference Example 1 but by impregnation as in Example 1 to prepare an adsorbent (NaY + CuC12; the amount of Cu carried in the zeolite was 11.93 wt%), was reduced by the same method as in Reference Example 1.
C0 and C02 equilibrium adsorption amounts were measured.
The reduction reaction converted NaY + CuC12 into NaY + CuCl.
The results are shown in Fig. 4, The C0 selective adsorption capacity of the adsorbent prepared by only impregnation was insufficient and is poorer than that of the adsorbent prepared by only ion-exchanging in Reference Example 1.
Example 3 Cu(II)Y was impregnated with predetermined amounts of FeC13, ZnC12, NiC12, and MgC12 and was reduced by 12690l99 the same method as in Reference Example 1. CO and C02 adsorption amounts and a CO/C02 ratio were measured.
The reduction reaction converted Cu(II)Y + MC12 into Cu(I)Y + MC12. MCl2 was a metal chloride. The results with adsorbents containing metal chlorides MnC12, CaC12, and BaC12 excluded from those of the present invention and an adsorbent without a metal chloride are shown in Table 1 and Fig. 5. The selectivity ratio of CO/C02 of the present invention is higher than that of Cu(I)Y not impregnated with a metal chloride, as is apparent from Table 1.
lZ69089 - lg -Table 1 Measurement Representing Amounts of Various Metal Chlorides Impregnated into Cu(I)Y and C0/C02 Adsorption Amounts Metal Impreg- C0 Adsorp- C0 Chloride nation tion Amount Adsorp- Selec Amount at 20C ption tivity MC12 (NmQ/g) Amount Cu(I)Y at 20C
(mmol/g) (Nm~/g) Present FeCl 1.533 25.70 34.73 0.740 Invention 3 Present ZnC12 1.580 31.58 36.18 0.873 Invention _ Present NiCl 1.424 27.98 38.45 0.728 Invention 2 Present MgC12 2.158 22.04 26.75 0.824 Invention Compar- MnC12 1.475 27.54 41.88 0.658 Example _ Compar- CaC12 1.292 23.45 43.02 0.545 Example ative BaC12 0.933 23.46 46.83 0.501 Example ence Cu(I)Y _ 38.24 57.99 0.659 Example _ Example 4 A CuC12 impregnation amount per gram of Cu(II)Y
was changed. Following the same procedures as in Reference Example 1, reduction was performed, and C0 and C02 adsorption amounts (20C) of Cu(I)Y ~ CuC12 were measured. The results are shown in Fig. 6.
1~:69089 The Co adso~ption amount exceeds the C02 adso~ption amount when 0.~ mmol/g to 2.5 mmol/g of CuC12 is contained. The CO/C02 ratio is 1.1 or more when 1.0 to 2.0 mmol/g of CuC12 is contained.
Example 5 Ten grams of CUtII)y + CuC12 prepared by the same procedures as in Example 1 were filled in a glass tube having a diameter of ~2 mm, and the glass tube was set in an annular electric furnace. The height of the Cu(II)Y + CuC12 in the glass tube was about 2 cm.
N2 gas was supplied at a flow rate of l.û NQ/min, and the Cu(II)Y + CuC12 was heated to a predetermined temperature and kept thereat for an hour. After heating, the Cu(II)Y + CuC12 was cooled to room temperature, and the resultant adsorbent was removed.
One gram of the adsorbent was placed in a 20-m~
sampling bottle, and the bottle was set in a constant pressure adsorption amount-measuring apparatus.
The adsorbent was heated to a temperature of 250C
in a vacuum of 10 3 mmHg for 2 hours.
Subsequently, the sampling bottle was placed in a silicone oil tank and kept at 20C. He gas (99.9% or more of purity) at the atmospheric pressure was supplied to the bottle. The adsorption amounts and hence the capacity were measured until adsorption equilibrium was reached. After measurement, the bottle was heated at 250C and 10 3 mmHg for an hour. The sample was then ,. . .
lZ690~5~
cooled, and the sampling bottle was placed in the silicone oil tank at 20C. C0 gas (99.9% or more) was supplied to the sampling bottle to measure the equilibrium adsorption amount at the atmospheric pressure. This adsorption amount was the one before reduction.
The silicone oil tank was heated and kept at 250C, and the sample was reduced in the C0 atmosphere for 60 minutes. After reduction, C0 was removed from the sample such that the sample was heated to 250C
in a vacuum of 10 3 mm Hg for 2 hours. The sample was then left to cool. The cooled sample in the bottle was placed in the silicone oil tank and kept at 2ûC. Under this condition, C0 gas ~99.9% or more of purity) was supplied to the bottle, and the C0 equilibrium adsorp-tion amount at atmospheric pressure was measured. This adsorption amount was the one after reduction. Simi-larly, the sample was heated in a vacuum to remove C0, and then C02 equilibrium adsorption amount at 20C and the atmospheric pressure was measured. After the sample was heated in a vacuum to remove C02, the sample was weighed. The equilibrium adsorption amount per unit weight was calculated by using the measured weight.
C0 equilibrium adsorption amounts before and after the reduction, C02 equilibrium adsorption amounts after the reduction, and selectivity ratio of C0/C02 at temperatures of 35û, 400, 450, 5ûû, and 550C are shown in Table 2. For comparison, the measurement results at 600C and 250C (the latter is the pretreatment temperature of equilibrium adsorption amount measurement) are also shown. As is apparent from Table 2, when the heating temperature is increased, the C0 equilibrium adsorption amount before the reduction is increased, and the impregnated and carried CuC12 is gradually converted into CuCl having a C0 adsorption capacity.
Up to the heating temperature of 5ûûC, the C0 equilibrium adsorption amounts before and after the reduction are increased. However, when the heating temperature exceeds 500C, the C0 equilibrium adsorption amount is decreased, and the C02 equilibrium adsorption amount after the reduction is increased. It is thus found that the impregnated and carried CuC12 and the converted CuCl are evaporated from the adsorbent.
12~gOB9 Table 2 Equilibrium Adsorption Amount Measurement Data After Heating of Cu(II)Y + CuC12 Heating C0 Adsorp- C0 Adsorp- C02 C0/C02 Temper- tion tion Adsorp- Selec-ature Amount Amount tion tivity (C) at 20C at 20C Amount After After After at 20C Reduc-Reduction Reduction After tion (Nm~/g) (Nm/g) RteidOnc-(NmQ/g) Present 35014.56 49.53 39.22 1.263 Invention Present 40020.59 51.95 ¦42.54 1.221 Invention l Present 45025.27 53.14 42.32 1.256 Invention .
Present 50033.27 55.41 43.42 1.276 Invention Present 55023.58 53.89 43.65 1.235 Invention Compar-ative 2508.43 44.64 35.36 1.262 Example Compar-ative 60018.53 52.11 47.05 1.108 ~ample Reference Example 2 A PSA test apparatus having four adsorption towers made of SUS 304 stainless steel each having a size of 2" x 800 mm was used to obtain a relationship between the recovery ratio and the C0 purity of the recovered gas by using the adsorption temperature as a parameter.
Each tower comprised a mantle heater with a thermostat 12690~9 _ ~4 _ to keep the interior temperature within the range of 10C cf the preset temperature.
A lN CuC12 solution was prepared, and 10 9 of NaY
type zeolite (in the form of pellets having a diameter of 1.5 mm and a length of 5 mm and including 20% of a binder) and 50 m~ of lN CuC12 solution were poured in a 100-m~ round-bottom flask. A condenser was mounted on the round-bottom flask, and the flask was heated by a mantle heater at 100C for 2 hours to reflux the mixture therein. After the flask was left to stand, the supernatant liquid was removed by decantation.
Thereafter, another 50 mQ of the lN CuC12 solution were added to the round bottom flask, and the mixture was refluxed again, following the same procedures as described above. The reflux was repeated a total of five times. The zeolite was sufficiently washed with distilled water, dried at 110C, and pulverized.
The zeolite powder was then sintered in an electric furnace at 550C for 2 hours to prepare an adsorbent.
The recovered supernatant and filtered solutions were mixed, and the solution mixture was subjected to emission spectroanalysis, thereby measuring the Na amount and hence an ion exchange ratio of 86.5%.
The amount of Cu carried per unit weight of adsorbent was 8.87 wt%.
One kilogram of 1/16" granular pellets (including 20% of a granulating agent) of the resultant Cu(II) ~Z69089 Y type zeolite were filled in each tower and gases were desorbed from the zeolite by heating at 250 and 50 Torr for about 5 hours. Pure C0 gas was filled in each tower and then supplied thereto at a flow rate of about 1 Q/min for about 2 hours, thereby reducing Cu(II)Y
into Cu(I)Y. The 4-tower PSA apparatus generally repeats a cycle of adsorption, purging, desorption, and compression.
Desorption and refinement of a gas sample assumed as a converter gas having the following composition were tested by using the 4-tower PSA apparatus.
Gas Composition: C0 : 74.5%
C2 : 14.0%
H2 : 1.0%
N2 : 10.5%
An adsorption temperature was 165 + 10C, an adsorp-tion pressure was 1 kg/cm2G, and a gas desorbing pressure was 50 Torr. A ratio of the purge gas to the gas to be removed, and a source gas flow rate were changed, and a gas flow speed in the tower was kept substantially constant. A relationship between the C0 recovery ratio and the C0 purity of the recovered gas was determined.
As an example, if the supply gas flow rate was 0.76 Q/min, and the purge amount/desorbing amount ratio was 0.73, the C0 recovery ratio was 73%, and the recovered gas composition was as follows:
126908g C0 : 96.2%
C2 : 3 0%
N2 : 0-7%
H2 : 0.1%
The relationship between the C0 purity and the C0 recovery ratio is indicated by the broken line in Fig. 7.
Reference Example 3 Following the same procedures with the same apparatus as in Reference Example 2, except that an adsorption temperature was set at 210 + 10C, the relationship between the recovery ratio and the product C0 purity was determined.
As an example, if the supply gas flow rate was 0.70 ~/min, and the purge amount/desorbing amount ratio was 0.74, the C0 recovery ratio was 72%, and the recovered gas composition was as follows:
C0 : 98.5%
2 : 1.0%
; 20 N2 0-4%
H2 : 0.1%
The relationship between the product C0 purity and the recovery ratio is indicated by the solid line in Fig. 7.
As is apparent from the above test results, when ; 25 the adsorption temperature is increased, the product C0 ~ impurity is increased with respect to an identical C0 ; recovery ratio. At the same time, by decreasing the C0 "
, ' :
, ;.
lZ69089 recovery ratio to about 50%, the product C0 purity is increased to 99% or more.
Reference Example 4 Following the same procedures with the same apparatus as in Reference Example 2, except that an adsorption temperature was set at 135 + 10C, the relationship between the recovery ratio and the product C0 purity was determined.
As an example, if the supply gas flow rate was 0.72 ~/min, and the purge amount/desorbing amount ratio was 0.73, the C0 recovery ratio was 72%, and the recovered gas composition was as follows:
C0 : 93.1%
C2 : 5.2%
N2 1.4%
. H2 0-3%
: The relationship between the product C0 purity and the recovery ratio is indicated by the alternate long and short dashed line in Fig. 7.
As is apparent from the above results, when the adsorption temperature is 150C or less, the product ~ C0 purity is decreased below 95% with respect to the : recovery ratio of about 70%. In order to maintain the product C0 purity to be about 98%, the recovery ratio must be reduced to about 30%.
Example 6 ~ Ten grams of Cu(II) Y type zeolite (pellets having ':~
~6go8~
a diameter of 1.5 mm and a length of 5 mm) ion-exchanged by the method described in Reference Example 2 were measured and put into a lOû-mQ eggplant-type flask.
The flask was set in a rotary vacuum evaporator and evaporated at 95C or more. After the evaporation, the sample was cooled to room temperature.
Meanwhile, 8.3 9 of CuC12-2H2û were dissolved in water at room temperature to prepare a 20-mQ solution.
This solution was a substantially CuC12 saturated solution. A capillary was mounted on a leak cock of the rotary vacuum evaporator, and the abbve solution was dripped 2 or 3 droplets at a time into the adsorbent while the eggplant-type flask was kept in a vacuum.
When the adsorbent was uniformly wet, dripping of the solution was stopped. The internal pressure of the flask was set at atmospheric pressure. The sample impregnated with the solution was placed in a suction filter with a metal net. The remaining solution was poured on the sample. The sample was subjected to suction filtering for about 3û minutes, and then placed on a magnetic tray. The sample was dried naturally for 24 hours. After drying with air, the sample was dried in a vacuum drier at 110 for 3 hours, thereby preparing an adsorbent of the present invention. The amount of Cu carried in the adsorbent was 15.96 wt%.
Thereafter, 1,250 9 of 1/16" granular pellets (containing 20% of a granulating agent) of the adsorbent ~z~g~
(referred to as Cu(II)Y + CuC12) were filled in each tower in the same apparatus as in Reference Example 2, and an adsorption temperature was set to be 90 ~ 10C.
Following the same procedures as in Reference Example 2
- 5 except for the adsorption temperature, a product C0 purity and a recovery ratio were calculated. The amount - of pellets filled in each tower was increased by 250 9 as compared with that in Reference Example 2 because Cu(II)Y + CuC12 had a larger apparent specific gravity than that of Cu(II)Y in Reference Example 2.
As an example, if a supply gas flow rate was 1.23 Q/min, a purge amount/desorbing amount ratio was 0.63, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 99.
C2 Tr N2 0.1%
H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the solid line in Fig. 8.
Example 7 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 70 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was , ' " , ~Z690~9 1.10 Q/min, a purge amount/desorbing amount ratio was 0.64, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 98.2%
C2 : 1.7%
N2 : 0.1 H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the alternate long and short dashed line in Fig. 8.
Example 8 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 50 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was 1.03 Q/min, a purge amount/desorbing amount ratio was 0.71, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 95.4%
C2 : 4.4%
N2 : 0.2 H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the broken line in Fig. 8.
:
,~',, ~
~ ~ '"' .
lZ6~085 Example 9 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 30 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was l.û2 ~/min, a purge amount/desorbing amount ratio was 0.71, the C0 recovery ratio was 73% and the recovered gas composition was as follows:
C0 : 87.5%
Cû2 : 12.1%
N2 : 0-4%
H2 : Tr - The relationship between the product C0 purity and the C0 recovery ratio is indicated by the alternate long and two short-dashed line in Fig. 8.
,
As an example, if a supply gas flow rate was 1.23 Q/min, a purge amount/desorbing amount ratio was 0.63, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 99.
C2 Tr N2 0.1%
H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the solid line in Fig. 8.
Example 7 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 70 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was , ' " , ~Z690~9 1.10 Q/min, a purge amount/desorbing amount ratio was 0.64, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 98.2%
C2 : 1.7%
N2 : 0.1 H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the alternate long and short dashed line in Fig. 8.
Example 8 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 50 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was 1.03 Q/min, a purge amount/desorbing amount ratio was 0.71, the C0 recovery ratio was 78% and the recovered gas composition was as follows:
C0 : 95.4%
C2 : 4.4%
N2 : 0.2 H2 : Tr The relationship between the product C0 purity and the C0 recovery ratio is indicated by the broken line in Fig. 8.
:
,~',, ~
~ ~ '"' .
lZ6~085 Example 9 Following the same procedures as in Example 6 except that the adsorption temperature was set to be 30 + 10C, a product C0 purity and a recovery ratio were measured.
As an example, if a supply gas flow rate was l.û2 ~/min, a purge amount/desorbing amount ratio was 0.71, the C0 recovery ratio was 73% and the recovered gas composition was as follows:
C0 : 87.5%
Cû2 : 12.1%
N2 : 0-4%
H2 : Tr - The relationship between the product C0 purity and the C0 recovery ratio is indicated by the alternate long and two short-dashed line in Fig. 8.
,
Claims (20)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS :
1. An adsorbent, for selectively adsorbing carbon monoxide from a gas mixture containing at least carbon monoxide and carbon dioxide, comprising mainly Cu(I), ion-exchanged and carried in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10; and a salt of at least one metal selected from the group consisting of Cu(I), Fe, Zn, Ni, and Mg, the metal salt being dispersed and carried in pores of the zeolite.
2. The adsorbent according to claim 1, wherein the Cu(I) is carried in the cation exchange site of the zeolite at an ion exchange ratio of not less than 70%.
3. The adsorbent according to claim 1, wherein mainly a Cu(I) salt is dispersed and carried in the pores of the zeolite.
4. The adsorbent according to claim 3, wherein the Cu(I) salt is dispersed and carried in the pores in an amount of 0.8 mmol to 2.5 mmol per gram of the ion-exchanged Cu(I) zeolite.
5. The adsorbent according to claim 3, wherein the Cu(I) salt is dispersed and carried in the pores in an amount of 1.0 mmol to 2.0 mmol per gram of an ion-exchanged Cu(I) zeolite.
6. The adsorbent according to claim 3, wherein the Cu(I) salt is Cu(I) halide.
7. The adsorbent according to claim 6, wherein the Cu(I) halide is Cu(I) chloride.
8. The adsorbent according to claim l, wherein the metal salt dispersed and carried in the pores of the zeolite is a halide.
9. The adsorbent according to claim 8, wherein the halide is a chloride.
10. The adsorbent according to claim l, wherein the zeolite having the silica/alumina ratio of not more than 10 is a Y type zeolite.
11. The adsorbent according to claim 1, wherein the adsorbent is treated by pressure swing adsorption at a temperature of not more than 100°C., so that carbon monoxide is selectively desorbed and refined.
12. A method of manufacturing an adsorbent for selectively adsorbing carbon monoxide from a gas mixture containing at least carbon monoxide and carbon dioxide, comprising the steps of:
ion-exchanging and carrying Cu(II) in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10;
dispersing and carrying a salt of at least one metal selected from the group consisting of Cu(II), Fe, Zn, Ni, and Mg in pores of the zeolite according to an impregnation method; and reducing the Cu(II) and the Cu(II) salt with a reducing gas to obtain Cu(I) and a Cu(I) salt.
ion-exchanging and carrying Cu(II) in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10;
dispersing and carrying a salt of at least one metal selected from the group consisting of Cu(II), Fe, Zn, Ni, and Mg in pores of the zeolite according to an impregnation method; and reducing the Cu(II) and the Cu(II) salt with a reducing gas to obtain Cu(I) and a Cu(I) salt.
13. The method according to claim 12, wherein the Cu(II) is ion-exchanged and carried in the cation exchange site of the zeolite at an ion exchange ratio of not less than 70%.
14. The method according to claim 12, where mainly the Cu(II) salt is dispersed and carried in the pores of the zeolite by the impregnation method.
15. The method according to claim 12, wherein the Cu(II) is carried by the zeolite by an ion exchange method, and then the metal salt is dispersed and carried in the pores of the zeolite by the impregnation method.
16. A method of manufacturing an adsorbent for selectively adsorbing carbon monoxide from a gas mixture containing at least carbon monoxide and carbon dioxide, comprising the steps of:
ion-exchanging and carrying Cu(II) in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10;
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method;
heating in an inert atmosphere, the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing the Cu(II) and the residual Cu(II) salt with a reducing gas to obtain mainly Cu(I) and the Cu(I) salt.
ion-exchanging and carrying Cu(II) in a cation exchange site of a zeolite at an ion exchange ratio of not less than 50%, the zeolite having a silica/alumina ratio of not more than 10;
dispersing and carrying a Cu(II) salt in pores of the zeolite by an impregnation method;
heating in an inert atmosphere, the Cu(II) salt dispersed and carried by the impregnation method to obtain a Cu(I) salt; and reducing the Cu(II) and the residual Cu(II) salt with a reducing gas to obtain mainly Cu(I) and the Cu(I) salt.
17. The method according to claim 16, wherein the Cu(II) is ion-exchanged and carried in the ion exchange site of the zeolite at an ion exchange ratio of not less than 70%.
18. The method according to claim 16, wherein the Cu(II) is carried by the zeolite by an ion exchange method, and then the metal salt is dispersed and carried in the pores of the zeolite by the impregnation method.
19. The method according to claim 16, wherein the step of heating is performed in a temperature range of 350° to 550°C.
20. The method according to claim 16, wherein the step of heating is performed in a temperature range of 400°C to 500°C.
Applications Claiming Priority (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60257821A JPS62119106A (en) | 1985-11-19 | 1985-11-19 | Method for separating and purifying co |
| JP25782085 | 1985-11-19 | ||
| JP257820/85 | 1985-11-19 | ||
| JP257821/85 | 1985-11-19 | ||
| JP61233349A JPH0620545B2 (en) | 1985-11-19 | 1986-10-02 | Co selective adsorbent and method for producing the same |
| JP233349/86 | 1986-10-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1269089A true CA1269089A (en) | 1990-05-15 |
Family
ID=27331981
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000523163A Expired CA1269089A (en) | 1985-11-19 | 1986-11-17 | Selective adsorbent for co and method of manufacturing the same |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US4783433A (en) |
| EP (1) | EP0224150B1 (en) |
| CA (1) | CA1269089A (en) |
| DE (1) | DE3684416D1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006047884A1 (en) * | 2004-11-04 | 2006-05-11 | Questair Technologies Inc. | Improved adsorbent material for selective adsorption of carbon monoxide and unsaturated hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01299642A (en) * | 1988-05-30 | 1989-12-04 | Hitachi Zosen Corp | Adsorbent for nitrogen oxide having low concentration |
| US5096470A (en) | 1990-12-05 | 1992-03-17 | The Boc Group, Inc. | Hydrogen and carbon monoxide production by hydrocarbon steam reforming and pressure swing adsorption purification |
| US5329057A (en) * | 1991-04-19 | 1994-07-12 | The Dow Chemical Company | Process for the cyclodimerization of 1,3-butadienes to 4-vinylcyclohexenes |
| US5196621A (en) * | 1991-04-19 | 1993-03-23 | The Dow Chemical Company | Process for the cyclodimerization of 1,3-butadienes to 4-vinylcyclohexenes |
| CN1043311C (en) * | 1993-12-16 | 1999-05-12 | 中国科学院大连化学物理研究所 | Zeolite adsorbing agent for carbon monoxide with high selectivity |
| FR2735992B1 (en) * | 1995-06-29 | 1997-08-14 | Inst Francais Du Petrole | ADSORBENTS FOR USE IN PROCESSES OF PURIFYING ETHYLENE POLLUTED ATMOSPHERES |
| USRE38493E1 (en) | 1996-04-24 | 2004-04-13 | Questair Technologies Inc. | Flow regulated pressure swing adsorption system |
| US6921597B2 (en) | 1998-09-14 | 2005-07-26 | Questair Technologies Inc. | Electrical current generation system |
| EP1005904A3 (en) | 1998-10-30 | 2000-06-14 | The Boc Group, Inc. | Adsorbents and adsorptive separation process |
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| CN115722187A (en) * | 2021-08-27 | 2023-03-03 | 北京北大先锋科技股份有限公司 | High-adsorption-capacity carbon monoxide complex adsorbent and preparation method and application thereof |
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|---|---|---|---|---|
| US3236762A (en) * | 1951-01-28 | 1966-02-22 | Union Carbide Corp | Hydrocarbon conversion process with the use of a y type crystalline zeolite |
| US3185540A (en) * | 1961-12-18 | 1965-05-25 | Union Carbide Corp | Method of removing carbon monoxide from gas mixtures |
| US3346328A (en) * | 1967-03-30 | 1967-10-10 | Francis J Sergeys | Method of treating exhaust gases |
| US3497462A (en) * | 1967-09-20 | 1970-02-24 | Union Carbide Corp | Copper (i) zeolites |
| US3649177A (en) * | 1969-10-13 | 1972-03-14 | Universal Oil Prod Co | Method for preparing copper-exchanged type y zeolite |
| US3755540A (en) * | 1972-01-28 | 1973-08-28 | Universal Oil Prod Co | Method for preparing copper exchanged type x zeolite |
| US4019879A (en) * | 1975-09-26 | 1977-04-26 | Union Carbide Corporation | Selective adsorption of carbon monoxide from gas streams |
| US4034065A (en) * | 1975-09-26 | 1977-07-05 | Union Carbide Corporation | Preparation of CU+ zeolites |
| US4470829A (en) * | 1981-08-31 | 1984-09-11 | Nippon Steel Corporation | Solid adsorbent for carbon monoxide and process for separation from gas mixture |
| US4539020A (en) * | 1983-07-10 | 1985-09-03 | Kawasaki Steel Corporation | Methods for obtaining high-purity carbon monoxide |
| DE3567579D1 (en) * | 1984-07-04 | 1989-02-23 | Nippon Kokan Kk | Method of separating carbon monoxide |
-
1986
- 1986-11-10 US US06/929,089 patent/US4783433A/en not_active Expired - Fee Related
- 1986-11-14 DE DE8686115857T patent/DE3684416D1/en not_active Expired - Fee Related
- 1986-11-14 EP EP86115857A patent/EP0224150B1/en not_active Expired - Lifetime
- 1986-11-17 CA CA000523163A patent/CA1269089A/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006047884A1 (en) * | 2004-11-04 | 2006-05-11 | Questair Technologies Inc. | Improved adsorbent material for selective adsorption of carbon monoxide and unsaturated hydrocarbons |
Also Published As
| Publication number | Publication date |
|---|---|
| DE3684416D1 (en) | 1992-04-23 |
| EP0224150A2 (en) | 1987-06-03 |
| US4783433A (en) | 1988-11-08 |
| EP0224150A3 (en) | 1987-08-19 |
| EP0224150B1 (en) | 1992-03-18 |
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