CN1162416C - Silver catalyst for epoxyethane production, its preparation method and application - Google Patents

Silver catalyst for epoxyethane production, its preparation method and application Download PDF

Info

Publication number
CN1162416C
CN1162416C CNB011443448A CN01144344A CN1162416C CN 1162416 C CN1162416 C CN 1162416C CN B011443448 A CNB011443448 A CN B011443448A CN 01144344 A CN01144344 A CN 01144344A CN 1162416 C CN1162416 C CN 1162416C
Authority
CN
China
Prior art keywords
silver catalyst
silver
catalyst
carrier
gross weight
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
Application number
CNB011443448A
Other languages
Chinese (zh)
Other versions
CN1426835A (en
Inventor
陈建设
金积铨
张志祥
高政
李金兵
梁汝军
萨茜
代武军
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Research Institute of Beijing Yanshan Petrochemical Corp
Original Assignee
Beijing Research Institute of Beijing Yanshan Petrochemical Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Beijing Research Institute of Beijing Yanshan Petrochemical Corp filed Critical Beijing Research Institute of Beijing Yanshan Petrochemical Corp
Priority to CNB011443448A priority Critical patent/CN1162416C/en
Publication of CN1426835A publication Critical patent/CN1426835A/en
Application granted granted Critical
Publication of CN1162416C publication Critical patent/CN1162416C/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/52Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Landscapes

  • Catalysts (AREA)

Abstract

The present invention relates to a silver catalyst for preparing epoxy ethane by oxidating ethylene. The silver catalyst is obtained through the following methods that a porous alpha-alumina carrier produced by baking at high temperature is impregnated by a solution prepared from silver-contained compounds, organic amine and various auxiliary agents; after leached and dried, the porous alpha-alumina carrier is activated with a gas mixture containing oxygen firstly; then, a catalyst precursor is processed with inert gases at proper temperature. The silver catalyst of the present invention has high and stable activity and selectivity.

Description

Be used to produce silver catalyst, its preparation method and the application thereof of oxyethane
Technical field
The present invention relates to a kind of silver catalyst and preparation method thereof, more particularly the present invention relates to a kind of silver catalyst of producing by oxidation of ethylene in oxyethane and preparation method thereof that is used for, also relate to this catalyzer and produce purposes in the oxyethane at oxidation of ethylene.
Background technology
Oxidation of ethylene mainly generates oxyethane under the silver catalyst effect, side reaction takes place simultaneously generate carbonic acid gas and water, and wherein activity, selectivity and stability are the main performance index of silver catalyst.So-called activity is meant temperature of reaction required when process for ethylene oxide production reaches certain reaction load.Temperature of reaction is low more, and activity of such catalysts is high more.So-called selectivity is meant that conversion of ethylene in the reaction becomes the ratio of the total reaction mole number of the mole number of oxyethane and ethene.So-called stability then is expressed as active and fall off rate optionally, and the fall off rate stability of small catalyst more is good more.The silver catalyst that uses high reactivity, highly selective and have good stability in the process of oxidation of ethylene production oxyethane can be increased economic efficiency greatly, and the silver catalyst of therefore making high reactivity, highly selective and good stability is the main direction of silver catalyst research.The performance of silver catalyst has the important relationship except that composition and the preparation method with catalyzer, and also the performance and the preparation method of the carrier that uses with catalyzer have important relationship.
In the prior art preparation method of silver catalyst comprise the preparation and administration to active ingredient of porous support (as aluminum oxide) and auxiliary agent to as described in this two processes on the carrier.
The ordinary method that active ingredient silver and auxiliary agent are applied on the carrier mainly is an immersion reduction method, promptly at first with the solution impregnating carrier that contains silver salt, organic amine and various auxiliary agents, then soaked carrier is carried out activation treatment so that silver salt is reduced into active ingredient silver in thermal medium, and excessive reductive agent is decomposed.
The activation phenomenon of introducing in the disclosed patent has air, contains oxygen gas mixture and inert atmosphere, and activation temperature is in 100~950 ℃ wide region.EP0038446A (EC ErdoelchemieGmbh, 1981) uses the method that progressively heats up to make silver compound resolve into active ingredient silver; The reduction temperature that US4400308A (EC Erdoelchemie Gmbh, 1983) uses is 400~500 ℃, and reducing atmosphere is the gas mixture that contains oxygen 4~21%; US4389338A (NipponShokubai Kagaku Kogyo Co., Ltd., 1983) oxygen level less than 3% inert atmosphere in, temperature is to handle soaked carrier under 600~800 ℃ the condition to make catalyzer in 20~90 minutes; The silver catalyst preparation process of JP62083041A report is to handle the shape of a saddle carrier of remaining silent that floods with silver salt, basic metal under inert atmosphere, 400~950 ℃ of conditions; US4837347A (Halcon SD Group, 1983) prepares silver catalyst in handling soaked carrier more than 400 ℃ in air; EP0161930A (Scientific Design Co., 1985) and EP0349229A (Scientific Design Co., 1990) flood auxiliary agents such as basic metal after proposing to handle the carrier of dipping silver in oxygen-containing atmosphere again; US5602070A (ScientificDesign Co., 1997) think and in being no more than 300 ℃ inert atmosphere, handle the performance that catalyzer helps improving catalyzer, US5736483A (Scientific Design Co., 1998) proposition activation temperature in air should not surpass 300 ℃, and activation temperature can be 400 ℃ in the inert atmosphere.
There is patent report under special conditions, to handle catalyzer and can obtains the ideal effect.JP56108533A (Nippon Shokubai Kagaku Kogyo Co., Ltd., 1981) propose in air, under 100~400 ℃ of conditions, to reduce silver compound, handle obtaining activity, selectivity and all higher catalyzer of stability again with carbonic acid gas in 50~400 ℃ down; US5502020A (Mitsubishi Petrochemical Co., Ltd., 1994) and EP0764464A2 (Mitsubishi Petrochemical Co., Ltd., 1997) propose in the impregnated carrier process, about 150 ℃, to handle carrier 15 minutes with superheated vapo(u)r, make the silver granuel uniform distribution, thermal treatment soaked carrier then prepares silver catalyst, and claims that this processing has improved activity of such catalysts, selectivity and stability.
Although above-mentioned patent documentation is all in the activity, selectivity and the stability that have improved the gained silver catalyst in varying degrees, this area still needs a kind of silver catalyst that comprehensively is improved and preparation method thereof on activity, selectivity and stability.
Summary of the invention
Situation in view of above-mentioned prior art, the present inventor has carried out research extensively and profoundly in the silver catalyst field, found that the solution that dipping is mixed with by silver compound, organic amine, various auxiliary agent on the porous heat-resistant carrier, through air or oxygen level less than 21% nitrogen oxygen atmosphere in behind the thermal treatment intermediate, use rare gas element once more the activity of the prepared silver catalyst of thermal treatment in ethylene oxidation reactions, selectivity and active and optionally stability all be improved.
Therefore, the purpose of this invention is to provide a kind of novel silver catalyst, it demonstrates good activity, selectivity and active and optionally stable in the process of oxidation of ethylene production oxyethane.
Another object of the present invention provides a kind of preparation method of above-mentioned silver catalyst.
A further object of the present invention provides the application of above-mentioned silver catalyst in oxidation of ethylene production oxyethane.
These and other purposes of the present invention, feature and advantage will become more clear after reading this specification sheets in conjunction with the accompanying drawings.
The accompanying drawing summary
Fig. 1 produces the graphic representation that concerns between the oxyethane total amount of temperature of reaction and generation in the process of oxyethane for the explanation sample of the embodiment of the invention and control sample at oxidation of ethylene; With
Fig. 2 produces the graphic representation that concerns between the oxyethane total amount of selectivity and generation in the process of oxyethane for the explanation sample of the embodiment of the invention and control sample at oxidation of ethylene.
Detailed Description Of The Invention
One aspect of the present invention provides a kind of Novel silver catalyst, and described catalyst is prepared by a method comprising the following steps:
1) usefulness contains the solution impregnation porous heat-resistant carrier of silver compound, organic amine and the various auxiliary agents of q.s;
2) elimination maceration extract, dry impregnated carrier;
3) in containing oxygen gas mixture to step 2) the gained carrier carries out primary activation;
4) directly or after cooling with inert gas to step 3) product heat-treat, make described silver catalyst.
The present invention relates to the application of above-mentioned novel silver catalyst in oxidation of ethylene production oxyethane on the other hand.
Porous heat-resistant carrier used according to the invention can be aluminum oxide, silicon carbide, silicon-dioxide or silica-alumina.Preferred main ingredient is α-Al 2O 3(α-Al for example 2O 3Account for more than 90%) porous α-Al 2O 3Carrier.
Porous α-the Al that is used for silver catalyst of the present invention 2O 3Carrier can be the porous alumina carrier through high-temperature roasting commonly used in the prior art.For example described porous α-Al 2O 3Carrier can be made as follows:
I) preparation has the mixture of following composition:
A) based on the mixture total weight amount be the low sodium three water α-Al of 30-64% weight 2O 3
B) based on the mixture total weight amount be the vacation one water α-Al of 5-39% weight 2O 3
C) based on the mixture total weight amount be the carbonaceous material of 5-30% weight;
D) based on the mixture total weight amount be the fusing assistant of 0.01-2.0% weight;
E) based on the mixture total weight amount be the fluoride-mineralization agent of 0.01-2.0% weight;
F) based on the mixture total weight amount be the binding agent of 25-59% weight; And
G) water of surplus;
Ii) with i) in the mixture that obtains mediate evenly and extrusion moulding; With
The iii) dry product that obtains in ii), at high temperature roasting becomes α-Al then 2O 3
In order to make carrier that enough intensity and good surface properties be arranged, preferably between 1250 ℃~1550 ℃, temperature is too high can to influence activity of such catalysts and the selectivity of making to maturing temperature, and the too low then support strength of maturing temperature is relatively poor.
The adding of fusing assistant is in order to make carrier have good intensity under low maturing temperature.The example of fusing assistant comprises magnesium compound, for example the mixture of one or more in magnesium oxide, sal epsom, magnesium nitrate and the magnesiumcarbonate.
The adding of carbonaceous material is in order to make macropore, thereby makes carrier have proper pore structure and specific surface.Described carbonaceous material comprises a kind of or its mixture in refinery coke, carbon dust, graphite, polyethylene, polypropylene, the rosin etc.Carbonaceous material is oxidation in roasting process, generates gas evolution, forms macropore in carrier.Granularity according to carbonaceous material of the present invention is 20~200 orders, and add-on is 5~30% weight of mixture total weight amount, preferred 10~25% weight, and adding too much can make the intensity of carrier obviously descend.
The fluoride-mineralization agent that the present invention selects for use comprises hydrogen fluoride, Neutral ammonium fluoride, aluminum fluoride, magnesium fluoride, sodium aluminum fluoride etc., and the crystal formation that its role is to promote the oxidation aluminium transforms, and eliminates the following pore of 5 μ m.
By adding binding agent, the vacation one water α-Al in it and the mixture 2O 3Generation aluminium colloidal sol bonds together each component, but becomes the paste of extrusion moulding.Used binding agent comprises acid, as nitric acid, formic acid, acetate, propionic acid and hydrochloric acid etc., and aluminium colloidal sol.When using acid as binding agent, salpeter solution preferably, wherein the weight ratio of nitric acid and water is 1: 1.25~10.
Can be dried to moisturely below 10% after the extrusion moulding of gained paste, support shapes can be annular, spherical, cylindricality or porous cylindricality.Drying temperature is 80~120 ℃, and be controlled at 1 hour~24 hour according to moisture content time of drying.
Dried paste makes aluminum oxide all be converted into α-Al 1250~1550 ℃ of following roastings 2~6 hours 2O 3The crushing strength of this carrier is 20N/ grain~120N/ grain, preferred 40N/ grain~80N/ grain; Specific surface is 0.1~2.0m 2/ g, preferred 0.5~1.5m 2/ g; Water-intake rate is not less than 40%, preferably is not less than 60%; Pore volume is 0.3-1.0ml/g, preferred 0.5-0.8ml/g; The aperture accounts for more than 90% of total pore volume greater than the hole of 1 μ m.
Silver catalyst of the present invention is by preparing with the above-mentioned alumina supporter of the solution impregnation of a kind of Ag-containing compound, organic amine and various auxiliary agents.
In the preparation of silver catalyst of the present invention, at first make the aqueous solution and the ammonium oxalate or the oxalic acid aqueous solution reaction of Silver Nitrate, separate out the silver oxalate precipitation, after the filtration, use deionized water wash, until no nitrate ion, then silver oxalate is dissolved in organic amine such as pyridine, butylamine, quadrol, 1, in the aqueous solution of 3-propylene diamine, thanomin or its mixture, add auxiliary agent, be made into dipping solution.Flood above-mentioned alumina supporter with the gained dipping solution then, drain, in being not more than 21% nitrogen oxygen atmosphere, airflow or oxygen level in 200~700 ℃, preferred 200-500 ℃ temperature range, kept 1 minute~120 minutes, and preferred 1 minute~60 minutes, to carry out thermolysis.Also available silver suboxide replaces Silver Nitrate, and silver oxalate also can not analysed filter, direct and organic amine complexing, impregnated carrier then.The amount of the silver compound that uses in the steeping process of the present invention should be enough to make argentiferous 1-30% weight in the finally prepd catalyzer, and preferred 5~25% weight are in total catalyst weight.
Auxiliary agent among the present invention can be compound or its mixture of alkali metal compound such as lithium, sodium, potassium, rubidium or caesium, and alkali-metal content is 100~1000ppm in the final catalyzer.Alkali metal promoter can be before dipping silver, simultaneously or be applied to afterwards on the carrier, also can after silver compound is reduced, be immersed on the carrier.
Auxiliary agent also can be the compound of alkaline earth metal compound such as calcium, strontium or barium, and the content of alkaline-earth metal is 50~1000ppm in the final catalyzer.Base earth metal promoter can be before dipping silver, simultaneously or be applied to afterwards on the carrier, also can after silver compound is reduced, be immersed on the carrier.
Impregnated in after silver compound on the carrier is heated decomposition, auxiliary agent also is applied on the carrier simultaneously, it is to heat-treat once more under 150~350 ℃ the condition in temperature that intermediate is placed rare gas element, treatment time is 1 minute~480 minutes, preferred 2 minutes~300 minutes, to improve catalyst performance.Described rare gas element is a pure inert gas, as nitrogen, helium or argon etc.
Various silver catalyst of the present invention is tested its performance with laboratory reaction device (to call " little anti-" in the following text) evaluating apparatus.Micro anti-evaluation device reaction device internal diameter 4mm, catalyst loading volume 1ml.The appreciation condition that the present invention uses is as follows:
Reactant gases is formed (mol%)
Ethene (C 2H 4) 20~32
Oxygen (O 2) 6.5~7.5
Carbonic acid gas (CO 2)<10
Cause steady gas (N 2) surplus
Inhibitor ethylene dichloride 0.1ppm~7.0ppm
Reaction pressure 2.1MPa
Air speed 7000/h
Reactor outlet EO concentration 1.35% or 2.4%
Space-time yield 185 or 330kgEO/lCat./h
When stable reach above-mentioned reaction conditions after the METHOD FOR CONTINUOUS DETERMINATION reactor go into, exit gas forms.Measurement result carries out calculating as follows after volumetric shrinkage is proofreaied and correct selectivity:
Figure C0114434400101
Wherein Δ EO be work off one's feeling vent one's spleen poor with the inlet gas ethylene oxide concentration.Get the test-results of the mean number of 10 groups of above testing datas as the same day.
The present invention compares with prior art has following advantage: silver catalyst of the present invention is specially adapted to the reaction that oxidation of ethylene is produced oxyethane, shows higher, stable activity and selectivity in process of the test.
Embodiment
The present invention is described further below in conjunction with example, but scope of the present invention is not limited to these embodiment.
The preparation of carrier:
Get three water α-Al 2O 3312g, a false water α-Al 2O 392kg, refinery coke 81g, NH 4F7g, Mg (NO 3) 28.5g.
Put into blender and mix, change in the kneader, add rare nitric acid (nitric acid: water=1: 3) 0.18 liter, but be kneaded into the paste of extrusion moulding.Extrusion moulding is the three hole column form objects of external diameter 8.0mm, long 6.0mm, internal diameter 1.0mm, more than 2 hours, free water content is reduced to below 10% 80~120 ℃ of oven dry.
Above-mentioned three hole column form objects are put into top-hat kiln, and through being elevated between 1450 ℃~1550 ℃ from room temperature about 30 hours, constant temperature 2 hours obtains white α-Al 2O 3Support samples.
After measured, the gained carrier has following performance:
Average intensity (N/ grain) 46
Specific surface (m 2/ g) 0.97
Water-intake rate (%) 73.5
Pore volume (ml/g) 0.72
Wherein<1 the hole of μ m is 3.2%
Preparation of catalysts:
Getting the 1.4kg Silver Nitrate is dissolved in the 1.5l deionized water.Get in the deionized water that the 0.65kg ammonium oxalate is dissolved in 0.5l50 ℃.Under vigorous stirring, mix two kinds of solution, generate white silver oxalate precipitation.Aging more than 30 minutes, filter, be precipitated to no nitrate ion with deionized water wash.Filter cake argentiferous about 60%, moisture about 15%.
In the Glass Containers that band stirs, add the 0.6kg quadrol, 0.22kg thanomin, 0.75kg deionized water.Stir following silver oxalate paste that makes and slowly add in the mixed solution, temperature remains on below 40 ℃, and silver oxalate is all dissolved, and the add-on of silver oxalate makes steeping fluid argentiferous 22% weight that makes.Add the 3.5g cesium oxalate then, the 3.5g barium acetate adds the 0.5kg deionized water again, makes solution for later use.
Get support samples and put into the container that can vacuumize.Be evacuated to below the 10mmHg, put into above steeping fluid, the submergence carrier kept 30 minutes.Superfluous solution is removed in leaching.Soaked carrier heated 5 minutes in 200 ℃ airflow, cooling.
The catalyzer that makes above is divided into 3 parts, and a copy of it is sample in contrast, in addition two parts stand-by.
Embodiment 1
One duplicate samples is placed the cast container, feed nitrogen from bottom to top, airflow rate is 100ml/min, and container is heated to 250 ℃, keeps 4 hours, obtains final catalyst prod.
Embodiment 2
A remaining duplicate samples is handled by the same way as of embodiment 1, and different is that the gas and changing that will feed is an argon gas.
Embodiment 3~8
Prepare alumina supporter and silver catalyst as stated above, and be divided into 4 parts, handle by the same way as of embodiment 1, different is treatment time and treatment temp, and actual conditions sees Table 1.
Table 1 silver catalyst heat treatment test result
Sample number into spectrum Handle atmosphere Treatment temp (℃) Treatment time (minute) Test result
Temperature of reaction (℃) Selectivity (%)
Comparative example ?216 ?83.0
Embodiment 1 ?N 2 ?250 ?240 ?214 ?83.7
Embodiment 2 ?Ar ?250 ?240 ?216 ?84.2
Embodiment 3 ?N 2 ?350 ?10 ?217 ?83.4
Embodiment 4 ?N 2 ?300 ?150 ?215 ?83.9
Embodiment 5 ?N 2 ?200 ?300 ?215 ?83.7
Embodiment 6 ?N 2 ?160 ?440 ?214 ?83.6
Embodiment 7 ?N 2 ?350 ?2 ?213 ?83.7
Embodiment 8 ?N 2 ?250 ?40 ?214 ?84.2
The test of catalyst performance:
Above 9 silver catalyst samples are smashed, respectively get 12~18 order sample 0.65g, place the micro anti-evaluation device, carry out the initial performance test under the condition of discharge ring oxidative ethane 1.35% at air speed 7000/h.Test result is listed in table 1.
Place comparative example, embodiment 1 and embodiment 2 the micro anti-evaluation device in air speed 7000/h, carry out stability test under the condition of discharge ring oxidative ethane 2.4%.The temperature of reaction of each catalyzer in the test process and selectivity and the oxyethane total mass mapping of producing, the result as depicted in figs. 1 and 2.
From table 1, Fig. 1 and Fig. 2 as can be seen, the present invention compares with control sample through the heat treated once more silver catalyst sample of rare gas element, and not only active and selectivity is improved, and active in optionally fall off rate is less.

Claims (29)

1. produce the used silver catalyst of oxyethane by oxidation of ethylene for one kind, by the method preparation that may further comprise the steps:
1) usefulness contains the solution impregnation porous heat-resistant carrier of silver compound, organic amine and the various auxiliary agents of q.s;
2) elimination steeping fluid, dry impregnated carrier;
3) being not more than in 21% the nitrogen oxygen atmosphere step 2 in air or oxygen level) the gained carrier carries out primary activation;
4) directly or after cooling, the product of step 3) is heat-treated, make described silver catalyst with rare gas element.
2. silver catalyst as claimed in claim 1, wherein the porous heat-resistant carrier is to contain the porous alumina carrier of Alpha-alumina more than 90%, and has added fusing assistant, carbonaceous material, binding agent and fluoride-mineralization agent in the preparation process of described porous alumina carrier.
3. silver catalyst as claimed in claim 2, wherein said fusing assistant are the magnesium compounds that is selected from magnesium oxide, sal epsom, magnesium nitrate and magnesiumcarbonate, when its add-on is described preparing carriers 0.01%~2.0% of the mixing material gross weight.
4. silver catalyst as claimed in claim 2, wherein said carbonaceous material are refinery coke, carbon dust, graphite, rosin, polyethylene, polypropylene or its mixture, when its consumption is described preparing carriers 5%~30% of the mixing material gross weight.
5. silver catalyst as claimed in claim 2, wherein said fluoride-mineralization agent is one or more the mixture in hydrogen fluoride, aluminum fluoride, Neutral ammonium fluoride, magnesium fluoride, the sodium aluminum fluoride, when its add-on is described preparing carriers 0.01%~2.0% of the mixing material gross weight.
6. silver catalyst as claimed in claim 2, wherein said binding agent are acid or aluminium colloidal sol, the 25-59% of mixing material gross weight when its consumption is described preparing carriers.
7. silver catalyst as claimed in claim 6, wherein said acid are salpeter solution, and wherein the weight ratio of nitric acid and water is 1: 1.25~10.
8. silver catalyst as claimed in claim 2, wherein said porous alumina carrier forms through high-temperature roasting, and maturing temperature is 1250 ℃~1550 ℃.
9. silver catalyst as claimed in claim 2, wherein said porous alumina carrier has following feature: specific surface is 0.1m 2/ g~2.0m 2/ g, pore volume are 0.3~1.0ml/g, water-intake rate 〉=40%, and crushing strength is 20N/ grain~120N/ grain.
10. silver catalyst as claimed in claim 9, wherein said porous alumina carrier has following feature: specific surface is 0.5m 2/ g~1.4m 2/ g, pore volume are 0.5~0.8ml/g, water-intake rate 〉=60%, and crushing strength is 40N/ grain~80N/ grain.
11. silver catalyst as claimed in claim 1, wherein silver compound is silver suboxide, Silver Nitrate or silver oxalate.
12. silver catalyst as claimed in claim 1, wherein should to make the content of silver in described silver catalyst be 1%~30% to the add-on of silver compound, based on the gross weight of described silver catalyst.
13. silver catalyst as claimed in claim 12, wherein the content of silver in described silver catalyst is 5%~25%, based on the gross weight of described silver catalyst.
14. silver catalyst as claimed in claim 1, wherein said auxiliary agent are alkali metal compound and/or alkaline earth metal compound.
15. silver catalyst as claimed in claim 14, wherein said basic metal are selected from lithium, sodium, potassium, rubidium, caesium and any two kinds combination thereof.
16. silver catalyst as claimed in claim 15, wherein said basic metal are caesium.
17. it is 100ppm~1000ppm that silver catalyst as claimed in claim 15, wherein said alkali-metal add-on should make the content of described basic metal in described silver catalyst, based on the gross weight of described silver catalyst.
18. silver catalyst as claimed in claim 14, wherein said alkaline-earth metal is selected from calcium, strontium and barium.
19. silver catalyst as claimed in claim 18, wherein said alkaline-earth metal are barium.
20. it is 50ppm~1000ppm that silver catalyst as claimed in claim 18, the add-on of wherein said alkaline-earth metal should make the content of described alkaline-earth metal in described silver catalyst, based on the gross weight of described silver catalyst.
21. silver catalyst as claimed in claim 14, wherein said auxiliary agent before dipping silver, simultaneously or be applied on the carrier afterwards, or after silver compound is reduced, be immersed on the carrier.
22. silver catalyst as claimed in claim 1, the temperature of wherein said reactivation process are controlled between 200 ℃~700 ℃.
23. silver catalyst as claimed in claim 22, the temperature of wherein said reactivation process are controlled between 200 ℃~500 ℃.
24. silver catalyst as claimed in claim 1, the time of wherein said reactivation process is 1 minute~120 minutes.
25. silver catalyst as claimed in claim 24, the time of wherein said reactivation process is 1 minute~60 minutes.
26. silver catalyst as claimed in claim 1, wherein said heat treatment process is carried out in pure inert gas.
27. silver catalyst as claimed in claim 26, wherein said rare gas element are nitrogen, helium or argon.
28. silver catalyst as claimed in claim 1, the temperature of wherein said heat treatment process are that 150~350 ℃ and time are 1 minute~480 minutes.
29. a method of producing oxyethane by oxidation of ethylene is wherein used as each described silver catalyst in the claim 1~28.
CNB011443448A 2001-12-17 2001-12-17 Silver catalyst for epoxyethane production, its preparation method and application Expired - Lifetime CN1162416C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CNB011443448A CN1162416C (en) 2001-12-17 2001-12-17 Silver catalyst for epoxyethane production, its preparation method and application

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CNB011443448A CN1162416C (en) 2001-12-17 2001-12-17 Silver catalyst for epoxyethane production, its preparation method and application

Publications (2)

Publication Number Publication Date
CN1426835A CN1426835A (en) 2003-07-02
CN1162416C true CN1162416C (en) 2004-08-18

Family

ID=4677494

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB011443448A Expired - Lifetime CN1162416C (en) 2001-12-17 2001-12-17 Silver catalyst for epoxyethane production, its preparation method and application

Country Status (1)

Country Link
CN (1) CN1162416C (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004101144A1 (en) 2003-05-07 2004-11-25 Shell Internationale Research Maatschappij B.V., Silver-containing catalysts, the manufacture of such silver­ containing catalysts, and the use thereof
CN103547365B (en) 2011-04-11 2016-03-16 陶氏技术投资有限责任公司 Regulate the method for efficient epoxyethane catalyst
CN103721712B (en) * 2012-10-12 2016-03-30 中国石油化工股份有限公司 A kind of ethylene produces oxirane silver catalyst
CN106693966A (en) * 2016-11-14 2017-05-24 中国海洋石油总公司 Efficient silver catalyst with regular grain size distribution for epoxyethane preparation and preparation method thereof
CN111013614B (en) * 2019-11-06 2023-01-13 浙江师范大学 Catalyst carrier and catalyst for preparing chlorine by oxidizing hydrogen chloride, and preparation method and application thereof

Also Published As

Publication number Publication date
CN1426835A (en) 2003-07-02

Similar Documents

Publication Publication Date Title
CN1301791C (en) Silver catalyst carrier for epoxyethane production, preparation method and application thereof
CN1232349C (en) Carrier for producing silver catalyst for epoxy ethane production, its preparing method and use
CN1093002C (en) Epoxidation catalyst and process
CN100577289C (en) The carrier of ethylene oxide silver catalyst, its preparation method and application thereof
CN101850243B (en) Carrier of silver catalyst for producing ethylene oxide, preparation method thereof, silver catalyst prepared by using same and application thereof in producing ethylene oxide
CN1087191C (en) epoxidation catalyst and process
CN1046433C (en) Catalyst carrier
CN1078818C (en) Epoxidation catalyst and process
CN1159095C (en) Catalyst carrier
CN1803279A (en) Ag catalyst for producing epoxyethane, its preparation method and uses
CN1126750C (en) Ethylene oxide catalyst
CN102145285A (en) Carrier of silver catalyst for producing epoxy ethane, preparation method and application of carrier of silver catalyst
CN1034678A (en) High-efficiency silver catalyst for oxidizing ethylene into epoxy ethane
CN1063239A (en) The preparation method of the solid capture agent of mercury
CN1007702B (en) Silver catalyst for production of ethylene oxide and method for mfr. thereof
CN1084643C (en) Catalysts for preparing chlorine from mydrogen chloride
CN1044416A (en) Produce oxyethane catalyzer and method for making thereof
CN102133545A (en) Carrier for silver catalyst for ethylene oxide production, preparation method and application thereof
CN1035063A (en) Be used to handle the catalyst and the method for handling waste gas of waste gas
CN1802211A (en) Ethylene oxide catalyst
CN1232350C (en) Carrier for producing silver catalyst for epoxy ethane production, its preparing method and use
CN1162416C (en) Silver catalyst for epoxyethane production, its preparation method and application
CN1101272C (en) Mfg. for producing alumina carrier and use thereof
CN1310703C (en) Ethylene oxide catalyst carrier preparation
CN87102701A (en) Argentum-based catalyzer that production oxirane is used and preparation method thereof

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
CI01 Correction of invention patent gazette

Correction item: Inventor

Correct: Xue Qian

False: Sa Qian

Number: 33

Page: 448

Volume: 20

CI03 Correction of invention patent

Correction item: Inventor

Correct: Xue Qian

False: Sa Qian

Number: 33

Page: The title page

Volume: 20

COR Change of bibliographic data

Free format text: CORRECT: INVENTOR; FROM: SACI TO: XUE XI

ERR Gazette correction

Free format text: CORRECT: INVENTOR; FROM: SACI TO: XUE XI

CX01 Expiry of patent term

Granted publication date: 20040818

CX01 Expiry of patent term