CN1171677C - Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas - Google Patents
Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas Download PDFInfo
- Publication number
- CN1171677C CN1171677C CNB011389087A CN01138908A CN1171677C CN 1171677 C CN1171677 C CN 1171677C CN B011389087 A CNB011389087 A CN B011389087A CN 01138908 A CN01138908 A CN 01138908A CN 1171677 C CN1171677 C CN 1171677C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- content
- hours
- total amount
- noble metal
- 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 - Lifetime
Links
Abstract
The present invention relates to a noble metal catalyst for the selective oxidation and purification of micro carbon monoxide in methanol reformed gases. The present invention is characterized in that the catalyst is a loading type catalyst with composite carriers and multiple active components, and the general formula of the catalyst is M1M2 / S1S2, wherein the M1 is a noble metal Pt which is used as the main active component; the M2 is one or several kinds of metallic elements of Fe, Co, Ni, Cu and Zn; the S1 is an MD-shaped molecular sieve; the S2 is one or two of ZrO2 and TiO2; the content of the M1 is from 0.2 wt% to 1.0 wt% of the total content of the catalyst; the content of the M2 is from 0.2 wt% to 5.0 wt% of the total content of the catalyst; the content of carriers is from 94.0 wt% to 99.6 wt% of the total content of the catalyst, and the ratio of the S1 and the S2 is equal to 1 to 3.5. The catalyst of the present invention has the characteristics of high reaction activity, high stability and good selectivity. In a reducing atmosphere, the prereduction does not require before the catalyst is reacted, the ventilation protection does not require after the catalyst is reacted, and the multiple starting performance can not decay. The temperature range of the operation of the catalyst is wide, and the operation control of the purification of vehicle-mounted hydrogen sources is easy.
Description
Technical field:
The present invention relates to the methanol recapitalization technology, a kind of noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO is provided especially.
Background technology:
CO is the poisonous substance of proton exchange membrane fuel cell electrode catalyst.External report current battery electrode can the content of anti-CO be 100～1000ppm, and domestic research level has determined that fuel cell can only anti-CO be below the 10ppm.For adapting to present situation, must invent a kind of practical technique that trace amounts of CO in the fuel cell hydrogen source can be reduced to below the 10ppm, its key is Study of Catalyst.According to reported in literature, at present, adopt the noble metal supported catalyst, but bullion content is up to about 5% more.Once on Applied Catalysis A (General 159 (1997) 159-169), delivered one piece of article as people such as Hiroshi Igarashi, be intended to remove the kinetic reaction of catalyst, investigate the selection of catalysts oxidation susceptibility by micro CO to the fuel cell enriched gas source.The author is with Pt/ zeolite and Pt/Al
2O
3, catalyst contrasts, and the catalyst Pt loading is 6.0 ± 0.2% (wt%), catalyst loading amount 0.1 gram, it is CO=1%, O that unstripped gas is formed (vol%)
2=0.5～3%, H
2=96～98.5%.As a result, at H
2Excessive and O
2Under the very low situation of content, the CO oxidation selectivity ratios Pt/Al of Pt/ zeolite catalyst
2O
3Catalyst height, selectivity depend on O in catalyst carrier and the gas
2Content, selectivity is along with O
2The reduction of content and improving.In all Pt/ zeolite catalysts, the Pt/ mordenite catalyst has the highest CO conversion ratio.When adopting two-stage reactor, O
2It is minimum that addition can reduce to.
Technology contents:
The invention provides a kind of noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO, it is characterized in that: this catalyst is the supported catalyst of complex carrier multiple active components, and general formula is M
1M
2/ S
1S
2Wherein
M
1Be main active component precious metals pt, M
2Be one or more of metallic element Fe, Co, Ni, Cu, Zn; S
1Be MD type molecular sieve, S
2Be ZrO
2, TiO
2One or both;
M
1Content is 0.2～1.0%wt of catalyst total amount, is good with 0.4～1.0wt%, M
2Content is 0.2～5.0%wt of catalyst total amount, is good with 0.5～4.5wt%, and vector contg is 94.0～99.6%wt of catalyst total amount, wherein S
1/ S
2=1～3.5, be good with 2～3.0.
The present invention also provides a kind of above-mentioned preparation method who is used for the noble metal catalyst of methanol reformed gas selective oxidation cleaning of micro CO, it is characterized in that preparation process is as follows:
Take by weighing 120～160 order S respectively according to weight proportion
1, S
2Powder mixes it, and adding forming agent, to be rolled onto φ 1～3mm spherical, and room temperature was placed after 4～5 hours, placed 110 ℃ of dryings of drying box 4～5 hours, and 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature;
Carrier is poured in the maceration extract, stir 1 hour at a slow speed under the room temperature condition after, placed 48 hours, placed 110 ℃ of dryings of drying box 4～5 hours, 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature, promptly make catalyst.
Catalyst of the present invention is a kind of supported catalyst of complex carrier multiple active components, and its catalytic action is respectively: M
1Be main catalyst component; M
2For helping catalyst component, mainly be to improve CO oxidation selectivity; S
1Be molecular sieve, mainly act as the decentralization that improves noble metal; S
2Mainly act as the stability that improves catalyst.
Catalyst of the present invention is used for 5KW level fuel cell hydrogen source, and (gas production is 12m
3/ hr)---and the cleaning system of trace amounts of CO in the preparing hydrogen by reforming methanol gas, catalyst loading amount 3～6 liters, it is H that unstripped gas is formed (vol%)
2: 46～49; N
2: 29～32; CO:0.6～1.60; CH
4: 0.09～0.26; CO
2: 20～21; Except said components, also contain methyl alcohol, dimethyl ether and the C of trace in the unstripped gas
2,, C
3, C
4Deng hydrocarbons, its content changes with the condition of oxidation and reformation of methanol reaction.Reaction condition is: system pressure 0.24MPa, 56～230 ℃ of reaction temperatures, air speed 2000～12000h
-1Reaction result: tail gas CO content is below the 10ppm, H
2Content (vol%) is 43～46.Up to now, do not see the report of the catalyst that this kind performance is arranged.
Catalyst selectivity of the present invention is good, and consumption hydrogen is few, suppresses the hydrogen-oxygen oxidation reaction, improves the CO oxidation activity.
Catalyst of the present invention does not need prereduction before the reaction under reducing atmosphere, the protection of need not ventilating after the reaction, and repeatedly startability does not have decay, is applicable to the gas purification of onboard hydrogen source.
The temperature range of catalyst operation of the present invention is wide, is easy to the operation control that on-board hydrogen source CO purifies.The good stability of catalyst of the present invention has passed through the life test more than 1000 hours, and activity is not found to descend.
In a word, the present invention has developed a kind of well behaved methanol reformed gas selective oxidation cleaning of micro CO catalyst that is used for, and this catalyst has reactivity height, good stability, the characteristics that selectivity is good.Catalyst of the present invention does not need prereduction before the reaction under reducing atmosphere, the protection of need not ventilating after the reaction, and repeatedly startability does not have decay.The temperature range of catalyst operation of the present invention is wide, is easy to the operation control that on-board hydrogen source purifies.
The specific embodiment:
Preparation of Catalyst all adopts following method preparation in the embodiment of the invention, and do not limit the present invention certainly: used catalyst component is except that Pt, and all the other nitrate that adopt them substantially are raw material, and the activity of such catalysts component is a step impregnation.Be specially the preparation of (1) carrier: take by weighing a certain amount of S respectively according to above-mentioned weight proportion
1, S
2Powder (through 500 ℃ of roastings 1 hour, 120～160 orders) mixes it, add forming agent and be rolled onto that spherical (φ 1～3mm), and room temperature was placed after 4～5 hours, placed 110～120 ℃ of dryings of drying box 4～5 hours, 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature.(2) Preparation of catalysts: 1. take by weighing a certain amount of carrier,, calculate the content of Pt, calculate the weight of corresponding salt then, it is dissolved in a certain amount of deionized water according to above-mentioned active component content ratio.2. maceration extract is adjusted to PH6～8, carrier is poured in the maceration extract, stir 1 hour at a slow speed under 100 ℃ of water bath condition after, placed 48 hours, placed 110～120 ℃ of dryings of drying box 4～5 hours, 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature.3. calculate the various content that help catalyst component by the carrier amount, calculate the weight of corresponding nitrate then, it is dissolved in a certain amount of deionized water.Pour the catalyst that 2. makes in the maceration extract (incipient impregnation), room temperature condition was placed 48 hours down, placed 110～120 ℃ of dryings of drying box 4～5 hours, and 500 ℃ of roastings of baking oven 4 hours are reduced to take out after the room temperature and promptly made catalyst.
Embodiment 1
Make catalyst according to above-mentioned preparation method.M wherein
1(precious metals pt) content is 0.2% (wt) of catalyst total amount; M
2(metal Ni) content is 0.2% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 99.6% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be ZrO
2, S
1/ S
2=1.
Embodiment 2
Get embodiment 1 catalyst 10ml (8.5 gram), the internal diameter of packing into is the reactor constant temperature zone of 12mm.Methanol reformed gas feeds reactor, and it is H that unstripped gas is formed (vol%)
2: 49～52; N
2: 23～28; CO:0.5～2.2; CH
4: 0.2～0.3; CO
2: 20～23; Except above-mentioned product, also contain methyl alcohol, dimethyl ether and the C of trace in the gas
2, C
3, C
4Deng hydrocarbons, its content changes with the condition of oxidation and reformation of methanol reaction.Methyl alcohol and C
2, C
3, C
4Lower Deng hydrocarbons content, be about tens to hundreds of ppm, dimethyl ether content is higher relatively, is about 1.2～1.5%.System pressure is normal pressure 0.2MPa; Air speed is 2200～3000h
-1When reaction temperature is 80～160 ℃ the outlet tail gas in CO content be below the 10ppm.When reaction temperature was 125 ± 3 ℃, reaction was through tens of inferior tests that stop, open, and accumulative total is after more than 1000 hour, and catalyst activity does not reduce trend, has good stability.
Embodiment 3
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 0.2% (wt) of catalyst total amount; M
2(metal Cu) content is 0.2% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 99.6% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be ZrO
2, S
1/ S
2=1.
Embodiment 4
Get embodiment 3 catalyst 1ml (0.84 gram), the internal diameter of packing into is the reactor constant temperature zone of 6mm.The steel cylinder distribution feeds reactor, and it is H that unstripped gas is formed (vol%)
2: 41.59; N
2: 27.47; CO:1.53; CH
4: 1.10; CO
2: 28.13; CH
3OCH
3: 0.4010; O
2/ CO:1.21.System pressure is normal pressure 0.1MPa; Air speed is 4000h
-1When reaction temperature is 80～160 ℃ the outlet tail gas in CO content be below the 10ppm.When reaction temperature was 145 ± 3 ℃, reaction stopped, opens test through tens times, and accumulative total is after nearly 120 hours, and catalyst activity does not reduce trend, has good stability.
Embodiment 5
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 0.2% (wt) of catalyst total amount; M
2(metal Ni) content is 5.0% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 94.8% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be ZrO
2, S
1/ S
2=3.5.
Embodiment 6
Get embodiment 5 catalyst 1ml (0.85 gram), carry out catalyst performance evaluation, export when reaction temperature is 85～154 ℃ that CO content is below the 10ppm in the tail gas with example 4 same reaction devices.When reaction temperature was 125 ± 3 ℃, reaction stopped, opens test through tens times, and accumulative total is after nearly 100 hours, and catalyst activity does not reduce trend, has good stability.
Embodiment 7
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 0.2% (wt) of catalyst total amount; M
2(metal Ni) content is 5.0% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 94.8% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be ZrO
2, S
1/ S
2=3.5.
Embodiment 8
Get embodiment 7 catalyst 1ml (0.83 gram), carry out catalyst performance evaluation, export when reaction temperature is 105～174 ℃ that CO content is below the 10ppm in the tail gas with example 4 same reaction devices.
Embodiment 9
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 1.0% (wt) of catalyst total amount; M
2(metal Ni) content is 0.2% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 98.8% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be TiO
2, S
1/ S
2=1.
Embodiment 10
Get embodiment 9 catalyst 1ml (0.87 gram), carry out catalyst performance evaluation, export when reaction temperature is 79～143 ℃ that CO content is below the 10ppm in the tail gas with example 4 same reaction devices.When reaction temperature was 120 ± 4 ℃, reaction was through stopping, open test several times, and accumulative total is after nearly 60 hours, and catalyst activity does not reduce trend, has good stability.
Embodiment 11
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 0.2% (wt) of catalyst total amount; M
2(metal Cu) content is 0.2% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 99.6% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be TiO
2, S
1/ S
2=1.
Embodiment 12
Get embodiment 11 catalyst 1ml (0.85 gram), carry out catalyst performance evaluation, export when reaction temperature is 83～153 ℃ that CO content is below the 10ppm in the tail gas with example 4 same reaction devices.
Embodiment 13
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 1.0% (wt) of catalyst total amount; M
2(metal Ni) content is 5.0% (wt) of catalyst total amount; Carrier S (S
1+ S
2) content is 94.0% (wt), wherein S of catalyst total amount
1Be molecular sieve MD, S
2Be TiO
2, S
1/ S
2=3.5.
Embodiment 14
Get embodiment 13 catalyst 1ml (0.86 gram), carry out catalyst performance evaluation, export when reaction temperature is 105～173 ℃ that CO content is below the 10ppm in the tail gas with example 4 same reaction devices.When reaction temperature was 145 ± 3 ℃, reaction was through stopping, open test several times, and accumulative total is after nearly 60 hours, and catalyst activity does not reduce trend, has good stability.
Embodiment 15
Press embodiment 1 same quadrat method, make catalyst.M wherein
1(precious metals pt) content is 1.0% (wt) of catalyst total amount; M
2(metal Cu) content is 5.0% (wt) of catalyst total amount; Carrier S content is 94.0% (wt), wherein S of catalyst total amount
1/ S
2=3.5.
Embodiment 16
Get embodiment 15 catalyst 6L (5.1 kilograms), the internal diameter of packing into is the reactor constant temperature zone of 150mm.Preparing hydrogen by reforming methanol gas feeds reactor, and it is H that unstripped gas is formed (vol%)
2: 46～49; N
2: 29～32; CO:0.6～1.60; CH
4: 0.09～0.26; CO
2: 20～21; In addition, the methyl alcohol, dimethyl ether and the C that also contain trace in the gas
2, C
3, C
4Deng hydrocarbons, reactor takes segmentation to advance O
2Method.System pressure is 0.24MPa; Air speed is 2000～4000h
-1Reaction temperature is 132～230 ℃.Reaction result: CO content is below the 2ppm in the outlet tail gas.Reaction is through stopping, open test several times, and accumulative total is after nearly 90 hours, and catalyst activity does not reduce trend, has good stability.H before and after purifying in the gas
2Reduce by 3 percentage points, selection of catalysts is better.
Claims (5)
1, a kind of noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO is characterized in that: this catalyst is the supported catalyst of complex carrier multiple active components, and general formula is M
1M
2/ S
1S
2Wherein
M
1Be main active component precious metals pt, M
2Be one or more of metallic element Fe, Co, Ni, Cu, Zn; S
1Be MD type molecular sieve, S
2Be ZrO
2, TiO
2One or both;
M
1Content is 0.2～1.0%wt of catalyst total amount, M
2Content is 0.2～5.0wt of catalyst total amount, and vector contg is 94.0～99.6%wt of catalyst total amount, wherein S
1/ S
2=1～3.5.
2, according to the described noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO of claim 1, it is characterized in that: M
1Content is 0.4～1.0wt% of catalyst total amount.
3, according to the described noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO of claim 1, it is characterized in that: M
2Content is 0.5～4.5%wt of catalyst total amount.
4, according to the described noble metal catalyst that is used for the methanol reformed gas selective oxidation cleaning of micro CO of claim 1, it is characterized in that: S in the carrier
1/ S
2=2～3.0.
5, the described Nobel-metal catalyst preparation method that is used for the methanol reformed gas selective oxidation cleaning of micro CO of a kind of claim 1 is characterized in that preparation process is as follows:
Take by weighing 120～160 order S respectively according to weight proportion
1, S
2Powder mixes it, and adding forming agent, to be rolled onto Φ 1～3mm spherical, and room temperature was placed after 4～5 hours, placed 110 ℃ of dryings of dry case 4～5 hours, and 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature;
Carrier is poured in the maceration extract, stir 1 hour at a slow speed under the room temperature condition after, placed 48 hours, placed 110 ℃ of dryings of drying box 4～5 hours, 500 ℃ of roastings of baking oven 4 hours are taken out after reducing to room temperature, promptly make catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011389087A CN1171677C (en) | 2001-12-25 | 2001-12-25 | Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011389087A CN1171677C (en) | 2001-12-25 | 2001-12-25 | Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1428198A CN1428198A (en) | 2003-07-09 |
| CN1171677C true CN1171677C (en) | 2004-10-20 |
Family
ID=4674860
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011389087A Expired - Lifetime CN1171677C (en) | 2001-12-25 | 2001-12-25 | Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1171677C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101193163B1 (en) | 2005-10-21 | 2012-10-19 | 삼성에스디아이 주식회사 | Catalyst for oxidizing carbon monoxide and method of producing the same |
| CN101121502B (en) * | 2006-08-11 | 2011-11-16 | 比亚迪股份有限公司 | System for preparing hydrogen from methanol and fuel battery device containing the same |
| FR2958185B1 (en) * | 2010-03-30 | 2012-04-20 | Arkema France | PROCESS FOR SELECTIVE OXIDATION OF CARBON MONOXIDE |
| CN104923220A (en) * | 2015-06-13 | 2015-09-23 | 常州大学 | Method for removing carbon monoxide by using oxidized graphene loading gold platinum catalyst |
| CN111036233B (en) * | 2018-10-12 | 2022-11-29 | 中国石油化工股份有限公司 | Wide-temperature methanol synthesis catalyst and preparation method and application thereof |
-
2001
- 2001-12-25 CN CNB011389087A patent/CN1171677C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1428198A (en) | 2003-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1680025A (en) | Low-temperature hydrolyst for high concentrated organosulfur and preparation thereof | |
| CN1083742A (en) | Double-function multi-metal-oxide catalyst | |
| CN1305567C (en) | Catalyst for autothermal reformation of methanol to prepared hydrogen and its prepn process and application | |
| CN101690892A (en) | Method for preparing catalyst for removing CO by selective oxidation | |
| CN114618589B (en) | Preparation method and application of ozone degradation catalyst based on iron-based organic framework | |
| JP2007182336A (en) | Method of generating hydrogen | |
| CN113578316A (en) | Preparation of supported porous nano platinum-ruthenium alloy catalyst and application of supported porous nano platinum-ruthenium alloy catalyst in preparation of chloroaniline by hydrogenation of chloronitrobenzene | |
| CN1171677C (en) | Noble metal catalyst for selective oxidation cleaning of micro CO in methanol reformed gas | |
| RU2304465C2 (en) | N2o decomposition catalyst in ostwald process | |
| CN1291784C (en) | Copper base catalyst in use for preparing hydrogen by reforming vapor of methanol and preparation method | |
| CN1123556C (en) | Process for preparing ketone by dehydrogenating para-alcohol | |
| EP1899264A2 (en) | Hydrogen generation catalysys and system for hydrogen generation | |
| CN1850329A (en) | Load-type nickel-metal catalyst and its use | |
| CN1966143A (en) | Ferric oxide carried palladium catalyst and its preparation method and application | |
| CN111215086A (en) | Application of rare earth oxide loaded transition metal catalyst in ammonia decomposition reaction | |
| CN101062478A (en) | Catalyst for carbon monoxide oxidation in hydrogen and preparation method thereof | |
| CN1282599C (en) | Catalyst for selectively oxidizing CO in condition of high hydrogen content and its preparing process | |
| CN111036199A (en) | Application of rutile type titanium oxide supported catalyst in carbon dioxide hydrogenation reaction | |
| CN111974382B (en) | Application of low-temperature CO oxidation or ADN decomposition platinum-based catalyst | |
| CN1768926A (en) | Catalyst for selective oxidation of CO in hydrogen enriched gas and its preparation method | |
| CN110038565B (en) | High-airspeed catalyst for hydrogen production from methanol water and preparation method and application thereof | |
| WO2001047806A1 (en) | Process for selective oxidation of carbon monoxide in a hydrogen containing stream | |
| CN1113693C (en) | Dehydrogenating catalyst containing more rare-earth elements for CO2 gas used to synthesize urea | |
| CN1772614A (en) | Prepn of nickel-base catalyst for decomposing ammonia | |
| CN111330593A (en) | Preparation method of hydrophobic Pt catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: DALIAN PRATT CHEMICAL TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: DALIAN INST OF CHEMICOPHYSICS, CHINESE ACADEMY OF SCIENCES Effective date: 20081121 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20081121 Address after: No. 161, Zhongshan Road, Liaoning, Dalian Patentee after: Pureite Chemical Tech Co., Ltd., Dalian Address before: No. 457, Zhongshan Road, Liaoning, Dalian Patentee before: Dalian Institute of Chemical Physics, Chinese Academy of Sciences |
|
| C56 | Change in the name or address of the patentee |
Owner name: DALIAN CATALYTIC ENGINEERING TECHNOLOGY LTD. Free format text: FORMER NAME: PUREITE CHEMICAL TECH CO., LTD., DALIAN |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 116012 No. 161, Zhongshan Road, Liaoning, Dalian Patentee after: Dalian Catalytic Engineering Technology Ltd. Address before: 116012 No. 161, Zhongshan Road, Liaoning, Dalian Patentee before: Pureite Chemical Tech Co., Ltd., Dalian |
|
| ASS | Succession or assignment of patent right |
Owner name: DALIAN SAMAT CHEMICALS CO., LTD. Free format text: FORMER OWNER: DALIAN CATALYTIC ENGINEERING TECHNOLOGY LTD. Effective date: 20130807 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 116012 DALIAN, LIAONING PROVINCE TO: 116085 DALIAN, LIAONING PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20130807 Address after: 116085, Huangpu Road, Dalian hi tech park, Liaoning, Dalian, 909A Patentee after: Dalian Shengmai CHemical Co. Ltd. Address before: 116012 No. 161, Zhongshan Road, Liaoning, Dalian Patentee before: Dalian Catalytic Engineering Technology Ltd. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20041020 |
|
| CX01 | Expiry of patent term |