CN85107325A - The production of oxyethane - Google Patents
The production of oxyethane Download PDFInfo
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- CN85107325A CN85107325A CN85107325.5A CN85107325A CN85107325A CN 85107325 A CN85107325 A CN 85107325A CN 85107325 A CN85107325 A CN 85107325A CN 85107325 A CN85107325 A CN 85107325A
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- nitropropane
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- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
With ethene and oxygen in the presence of chloride reaction control agent and nitropropane and silver-containing catalyst contact preparation oxyethane.Nitropropane has improved the selectivity of this method.
Description
The present invention has narrated the production of oxyethane.
We have disclosed the production method of alkene oxide in European patent 3642, this method comprises alkene is contacted with oxygen in the presence of silver-containing catalyst and the reaction control agent that contains chlorine, wherein catalyzer also be present in gas phase in nitrate or nitrite resultant contact, improved the performance of catalyzer thus.Disclose many employed nitrate or nitrite resultant, but be to use NO and oxygen, NO
2Or N
2O
4Better.
Consider these materials (NO particularly from many aspects
2) may be best.But because the existence of water vapor under the real reaction condition, equipment has the tendency that is corroded, when particularly having given birth to the smog that contains nitric acid.
We find that also ethene can generate 2-oxazolines that stain feeding line with the nitrogen oxide reaction under certain conditions.And the trouble part of control production process is be difficult to analyze the nitrogenous oxide compound and the logistics of water, and this is that nitrogen oxide leaves logistics as condensation product because during the cooling logistics.Therefore, if having aqueous recycle stream body (this industrial be generalized case), just be difficult in and accurately analyze nitrogen oxide under the physical condition in the ingress of reactor.
Nitropropane is added in the production process, rather than adds in the nitrogen oxide, can alleviate the problems referred to above.
Our European patent 3642 has disclosed and has used rudimentary nitroparaffins, has mentioned Nitromethane 99Min. especially.But Nitromethane 99Min. unavoidably exists the problem in the keeping.In the brochure that is entitled as " itroparaffin and harm thereof " that the fire prevention of the fire-insurance chamber of commerce of country (1959, the U.S.) and the council of engineering specification research department publish, commented the handling problem of Nitromethane 99Min..Nitromethane 99Min. is the theme that people discuss dangerous explosive substance always, and in general, the danger always of rudimentary itroparaffin.Although there is above-mentioned shortcoming, up to date, the way that we would rather take is still with NO, NO
2Or N
2O
4Directly be added in the operating process, and do not add the material that we mention in European patent 3642, by with such material oxidation, can be indirectly with nitrate and/nitrite ion is added on the catalyzer.
We have found that nitropropane has significant effect, can reduce corrosion on the whole, do not form 2-oxazolines, and easier analysis of sample of taking out from Reactor inlet.We find that also processing and keeping nitropropane are safer.Three carbon atoms in necessary each molecule of oxidation this shows that nitropropane has surprising high-level efficiency in this technology before nitropropane generates nitrate and nitrite.
Present invention resides under the existence of the reaction control agent that contains chlorine, with the method for ethene and oxygen and silver-containing catalyst contact preparation oxyethane, wherein catalyzer also contacts with nitropropane, has improved the performance of catalyzer thus.What adopted is 1-nitropropane and/or (better) 2-nitropropane.
The effect of nitropropane is the selectivity of increase process generally.
Selectivity of catalyst is meant the ratio that is consumed the ethene that is transformed into oxyethane in the technology.Along with increase duration of service, the selectivity of silver-containing catalyst can reduce in the technology.Used catalyst contacted with nitropropane can improve or recover selectivity of catalyst at least in part.Catalyzer generally can be improved selectivity of catalyst with the nitropropane Continuous Contact in technological process, or the reduction catalyzer loses selective rate.If desired, can repeatedly carry out the regeneration step of catalyst selectivity.
Should note following points when being added to nitropropane in the technological process:
1. the pump of Shi Yonging should be a positive-displacement pump, and this pump has security device, can prevent that pressure from surpassing 50 crust.The temperature of nitropropane can not surpass 80 ℃ in the pump, is lower than 50 ℃ better, is preferably lower than 30 ℃.
2. when being added to nitropropane in the technology, the temperature of its feeding point should be at least 50 ℃ (causing rapid evaporation), is up to 100 ℃, and (because along with temperature increases, the danger of blast also increases), pressure is up to 40 crust absolute pressures.
3. the liquid nitropropane can not contact with the oxygenant that comprises air under the pressure greater than 40 crust.Therefore, suitable way is that air can not advance pump together with nitropropane, is less than 40 crust unless this pump is adjusted to pressure.
Nitropropane can not can be reduced its stable alkali, and strong acid or other similar substance pollute.
In order to be dispersed in nitropropane in the process gases rapidly, and don't use supplementary pressure, and the possibility that occurs obstruction when eliminating from nozzle ejection nitropropane small droplet, way is under alap pressure preferably, nitropropane is introduced a kind of inertia porous material, keep the base speed of gas in the technology thus.Porous material itself should not limit very much flowing of air-flow, can use stainless (steel) wire.
If desired, can will be added in the nitropropane such as desensitization thinners such as toluene or lower aliphatic alcohols, the nitropropane that enters production process should be not moisture substantially yet.
As long as when handling nitropropane, conscientiously note all problems, and treat above-mentioned item with being doubly cautious that can think, its danger can reduce to feasible degree.But user of the present invention must watch out for all secure side to problem, make full use of at present or can improve in the future the technology of security.
The catalyzer that is suitable for contains the silver that is stated from the porous thermal resistance carrier, and according to Brunauer, the specific surface area scope that Emmett and Teller method are measured carrier is 0.05 to 10 meter
2/ gram, 0.1 to 5 meter
2/ gram is better, preferably 0.3 to 3 meter
2/ gram.Catalyzer can be by the method preparation that discloses in the European patent 3642.
The apparent porosity of support of the catalyst preferably is at least 20% by the mercury absorptionmetric determination, and for example 25～70%, 30～65% is better, and the mean pore size of measuring by mercury porosity meter method is 0.1 to 20 micron, and 0.3 to 4 micron better.It can be two types or three types that the pore of carrier distributes, and wherein diameter reaches the hole that 2 microns Kongzui accounts for 30% to 70%, 2 to 20 micron diameters of total pore volume well and is preferably 0 to 50% of total pore volume, and bigger Kongzui accounts for 20% to 50% of total pore volume well.
Silver in most of catalyzer preferably with the form of dispersed particle attached on the carrier, its equivalent diameter is less than 10,000A, 20 to 10, in the 000A scope better, 40 to 8,000A is best, for example 100～5,000A.Equivalent diameter means the diameter of identical silver particles spheroid.
Preferably contain 80% silver particles at least, its equivalent diameter is in above-mentioned scope, and silver-colored amount can be regulated according to the granule number that falls into above-mentioned diameter range.Most of silver is considered to exist with the form of argent.Retouch the specification that electron microscope can be measured silver particles by copying.
Carrier can be an aluminium sesquioxide, silicon carbide, silicon-dioxide, zirconium white, titanium dioxide or silicon-dioxide/alumina carrier, but preferably can be with aggregate such as material fusion such as silicon-dioxide or barium oxide or mutual cementitious α-aluminium sesquioxide particle.
Catalyzer preferably contains the silver of 3 to 50% weight, contain 3 to 30% more excellent, for example 6 to 28%.
Catalyzer is preferably answered cation, for example with corresponding nitrate or nitrite, or can react alkali and/or the alkaline earth metal cation that the form that generates nitrate and nitrite exists.If handle catalyzer off and on nitrate or nitrite resultant, in the hope of recovering selectivity, then above-mentioned way is suitable especially.These cationic effects be considered to than do not exist the time, more nitrate radical and/or nitrite ion can be remained on the catalyzer, or keep the longer time.But we do not wish with the cationic effect of any one theory.
Positively charged ion can be before adding silver compound, among or add silver compound after be added on the carrier.It is on the carrier that exists with metallic forms that positively charged ion preferably is added to silver wherein, and is incorporated as suitable with the aqueous solution and/or organic solution form.Dipping has been used for alkene is oxidized to olefin oxide and deactivated catalyzer if desired, also can adopt above-mentioned way, this cationoid is being existed by the form that water extracts, its suitable concn can be to contain 50 to 5 in the basic metal of for example per 100 ten thousand parts of weight, 000 part (weight), and/or 50 to 20,000 parts in the alkaline-earth metal (weight) of per 100 ten thousand parts of weight.
Positively charged ion can be provided by the compound that exemplifies below: nitrate, and oxyhydroxide, carbonate, supercarbonate or carboxylate salt, as lactic acid salt, oxalate preferably.
Urge mixture preferably to contain rubidium, caesium, lithium, cadmium, calcium, magnesium, strontium, barium and/or sodium and/or potassium, wherein potassium is best, and these elements exist with the form of compound, and compound then can be extracted from catalyzer by water.
The method according to this invention, the dividing potential drop of ethene can be within the scope of 0.1 to 30 crust, and 1 to 30 crust is better.Stagnation pressure can be within 1 to 100 crust (pounds per square inch absolute (psia)) scope, and 3 to 100 crust (pounds per square inch absolute (psia)) are better.The mole ratio of oxygen and ethene can be in 0.05 to 100 scope.The dividing potential drop of oxygen can be within the scope of 0.01 to 20 crust, and 0.1 to 20 crust is better, and 1 to 10 crust is better.Oxygen can be provided by air or the form that is preferably commodity oxygen.Thinner is helium for example, and nitrogen, argon gas, carbonic acid gas and/or methane, its ratio can account for the 10 to 80%, 40 to 70% better of cumulative volume.Suitable diluent contains above-mentioned methane and ethane, and for example per 100 ten thousand parts of volumes contain 100 to 20,000 parts ethane, and thinner preferably contains methane and a spot of following material, and for example per 100 ten thousand parts of volumes contain 10 to 10,000 parts of C
3To C
6Alkane, naphthenic hydrocarbon or alkene, propylene preferably wherein, cyclopropylene, or iso-butylene.Gas mixing ratio during operation is necessary to be controlled at outside the limits of explosion.
Suitable temperature range is 180 to 320 ℃, and 200 to 300 ℃ better, preferably 220 to 290 ℃.Should be enough to duration of contact 0.5～70%, (for example 2 to 20%, 5～20% conversion of ethylene preferably.After product separation went out, the unconverted ethene that suitably circulates also can be selected this to circulate in and remove portion C O
2Unconverted oxygen carry out under existing.The CO that in micropore, (promptly contacts) with catalyzer
2Content preferably should be 1% to 7%(volume) or higher, 2% to 5%(volume) better.
Chloride reaction control agent can be known kind, preferably should be C
1To C
10Compound, the while is hydrogen also.For example, conditioning agent can be 1, the 1-ethylene dichloride, and 1, the 2-ethylene dichloride is better, but recommend to adopt monochloro methane, vinylchlorid preferably, the chlorating aromatics also is fit to, for example chlorobenzene, dichlorobenzene and chlorotoluene.The concentration of chloride reaction control agent should be within the scope of 0.1 to 500 part of the reaction medium of per 100 ten thousand parts of weight, with 1 to 50 part better.
Nitropropane can be added in the technological process on a small quantity continuously, 1 to 200 part of the process gas of for example per 100 ten thousand parts of volumes, and 5 to 100 parts are better.Super regeneration catalyzer if desired, the gas of then desiring contact catalyst can contain more substantial nitropropane and enough oxygen, so that generate needed nitrate or nitrite.This gas preferably passes from catalyzer.
Lose in reaction optionally that catalyzer can optionally improve or recover, its temperature range is very wide, for example 150 to 350 ℃, with 200 to 300 ℃ for well.Pressure range can be 0.1 to 100 crust, preferably 1 to 50 crust (pounds per square inch absolute (psia)).
During catalyst regeneration, the catalyzer of per 100 ten thousand parts of weight added be at least 20 parts, preferably be at least 300 parts of nitrate and/or nitrite.
Regeneration can be in the presence of reaction reagent, by normal reaction conditions, by being added in the reaction, nitrate or nitrite resultant undertaken, preferably keeping concentration in the catalyzer is that the catalyzer of per 100 ten thousand parts of weight is at least 20 parts of nitrate and/or nitrite, is excellent to be at least 300 parts of nitrate and/or nitrite.
Embodiment 1
((being provided by Norton company), surface-area are 0.5 meter to the porous alumina carrier
2/ gram, pore volume are 0.43 milliliter/gram, SiO
2Content is 0.38%, and sodium content is 121pmm) be immersed in the silver nitrate solution that is dissolved in moisture Isopropylamine with annular form (7.8 millimeters of external diameters, 3.1 millimeters of internal diameters (hole), thickness are 7.8 times diameter).Impregnated wet solid heats pyrolysis in nitrogen gas stream, temperature reaches 240 ℃.Product hot wash after drying.The exsiccant catalyzer is again with potassium formiate aqueous solution dipping, discard aqueous solution after drying it.Final catalyst contains 16%(W/W) silver and the potassium that increases of 500ppm.
Catalyzer is through pulverizing, and sieving and obtaining 112 gram specifications is 1 to 3.35 millimeter loose material.Put it into internal diameter and be 10.8 millimeters, length and be in 2.58 meters the stainless steel reactor.Contain ethene (30%), oxygen (8%), CO
2(2.5%), vinylchlorid (12ppm), monochlorethane (3ppm), it is 252 ℃ catalyzer that the gaseous mixture of 2-nitropropane (20ppm) and nitrogen (polishing to 100%) is depressed by temperature at 15 crust tables.The space-time speed that gas passes through is 3070/ hour.Reaction obtains oxyethane and carbonic acid gas.Oxygen conversion is 20%, and oxyethane synthetic selectivity is to have 87 moles of ethylene oxide to generate in the ethene of the i.e. 100 moles of conversions of 87%().
Example 2
Preparation of catalysts
Catalyst carrier particle comprises porous high-purity alpha-aluminium sesquioxide, wherein contains 250 ± 50ppm, by the silicon-dioxide that silicon is represented, and the potassium compound that the sodium compound that 40 ± 10ppm represents with sodium and 12 ± 3ppm represent with potassium.This catalyst carrier particle is shaped as 8 mm dias, the right cylinder of 9 millimeters long axially crosses 7 diameters and is 1.22 millimeters hole on the right cylinder, a hole is in central authorities, it is that the center of circle is the axis of carrier granule on 4.39 millimeters the circle that remaining hole is arranged in diameter equably.Press following mode to the carrier granule coating with metallic silver corpuscle.The mean pore size of porous alumina is the 2-3 micron, and the porosity of estimating by absorption water is 0.36 ± 0.03 a milliliter/gram, and surface-area is about 0.5
2/ gram.
Under 70 ℃ Silver Nitrate (4,418) is being dissolved in the distilled water (896 milliliters), and the solution that generates is being cooled to 50 ℃.Under stirring and cooling off, slowly add single Isopropylamine to this solution.Add amine and want enough slow, too high to avoid temperature rise.Temperature remains on 40 to 60 ℃ scope.The clear liquid that generates is cooled to room temperature.
Carrier granule (4,200 gram) is vacuumized, add the solution (5,000 milliliters) of Silver Nitrate-single Isopropylamine mixture.After contacting 30 minutes with solution, from raffinate, isolate the particle of dipping, and elimination liquid.
The wet carrier granule that is impregnated with complex solution is put in the porous basket, and then the reactor of packing into.The carrier of heating dipping in the nitrogen gas stream of heat, initial temperature is 100 ℃, rises to 240 ℃ between 18 hours gradually.The mixture of dipping decomposes, and stays dispersive silver, is evenly distributed on porous α-aluminium sesquioxide particulate surface.The resistates that also has carbon containing and nitrogen on the particle.
Be coated with silver-colored particle and contact with warm air, method is the nitrogen gas stream that will contain 5% air by being heated to 150 ℃ particle.Respectively air content in the air-flow and temperature of reactor are risen to 100% and 280 ℃ gradually then.It is enough slow that these two paces of change are wanted, to avoid owing to process heat release particle temperature uncontrolledly being raise.When temperature reaches 280 ℃, be coated with silver-colored particle and contact 2 hours again, then cooling with airflow.
The silver-colored particle that is coated with that obtains is substantially free of resistates in Silver Nitrate-single Isopropylamine decomposition course.This particle is contacted 16 hours with hot water flow within 90 to 100 ℃ of scopes, cooling drains water then, and with 150 ℃ flow of warm nitrogen gas contact drying.Product is a catalyst Precursors, and its feature is clean substantially, and surfaces externally and internally evenly scribbles the dry dispersion of silver-colored particulate porous α-aluminium sesquioxide.
Catalyst Precursors (4945 milligrams) is flooded with potassium, and method is that catalyst Precursors is at room temperature contacted with the methanol aqueous solution that contains potassium formiate.This aqueous methanol solution contains water and 17.9 milligrams of potassium formiates of 0.2% volume.Potassium formiate solution is got to and finished above-mentioned contact with pump, collect effluent liquid, cycled through the parent bed 16 hours by the catalyst Precursors bed.After steeping process is finished, to the granules of catalyst discharge opeing, and dry in 150 ℃ flow of warm nitrogen gas.Final catalyst contains 500 to 600ppm potassium.
Repeat said procedure, refabrication goes out two batches of catalyzer, mixes these three batches of catalyzer and measures it.
Catalyzer is measured as follows.With the catalyzer internal diameter of packing into is in 39 millimeters the reaction tubes, bed long 10.7 meters (bed volume 12.81), the long filling of 3 mitrons on catalyzer inertia alumina particle.Flow around the heat exchange fluid that is used for controlled temperature around the pipe.Begin the feeding gas of following composition is dropped into reactor: 6%O
2, 27% C
2H
4, 6 ppm vinylchlorid, 0.1% ethane, 20 ppm 2-nitropropanes, all the other are methane and small amounts of inert gas substantially.Feeding temperature is 75 ℃, and pressure is 18.5 crust, and gas space-time speed is 3600/ hour.Raise the then temperature of reactor, initiation reaction.Press required feed composition with oxygenous, ethene, ethane, methane, 2-nitropropane and vinylchlorid feeding gas mix with recycle gas.After turning round 26 days, with 1.03 meters
3/ hour oxygen, 1.4 meters
3/ hour ethene, 6.8 liter/hour ethane and be present in 36 milliliters of/hour vinylchlorid (all numerical value all are illustrated in the gas under the standard temperature and pressure (STP)) in the methane, and the discontinuous methane fluid and the 2-nitropropane of enough operating device pressure mix with recycle gas.The 2-nitropropane is introduced by with positive discharge capacity micropump liquid 2-nitropropane being squeezed in the flow process, and this pump has the safety valve that begins middle release when 30 crust.The temperature of 2-nitropropane is about 20 ℃ in the pump, does not wherein contain air, oxygenant, alkali, acid and water substantially.The 2-nitropropane temperature at feed points place on stream is 70 ℃, pressure be 18 the crust (pounds per square inch absolute (psia)), amount of liquid is 3.7 milliliters/hour, material by all gas in the flow process all the braiding stainless (steel) wire of process enter system.
The analytical results that reactor feed is formed is: 7.5% O
2, 27%C
2O
4, 7.2ppm vinylchlorid, the 0.9ppm monochlorethane, 0.1% ethane, 20ppm 2-nitropropane, 0.12% water vapor is estimated to be about the 3ppm nitrogen oxide, and all the other are methane substantially.Analyze from Reactor inlet, find because the condensation of water is used the 2-nitropropane than using NO and NO
2Resulting analytical results is more accurate.The reactor feed temperature is 75 ℃, and pressure is 18.5 crust, and gas space-time speed is 3600/ hour.Oxygen is 28% through the transformation efficiency of reactor.Transforming selectivity of ethylene in the reaction is 87%.The temperature of average catalyst is 255 ℃.Gaseous product is cooled to 75 ℃ earlier, is 20 ℃ with temperature again, and 250.1 liters/hour water contact absorbs product of ethylene oxide.Separate the air-flow obtain, wherein a part in carbon dioxide scrubber with 250 liters/hour, the 0.5%(w/w) the contact of caustic soda solution.The gaseous product that scrubber comes out and that another part bypass gas flow are assembled, and are collapsed into circulating current then.The reaction that nitropropane and ethene take place does not cause deposition of solids.(under certain conditions, adopt NO/NO
2With ethene even at room temperature also deposit.) do not observe that reactor feed partly has the corrosion situation in the equipment.
Example 3
The catalyzer of measuring by following mode is similar to the catalyzer of example 2, but the content of potassium is 330ppm.Filling internal diameter with catalyzer is 39 millimeters reaction tubes, and packed bed length is 10 meters (11.92 liters of bed volumes), the long inertia aluminium sesquioxide particle of filling of 3 mitrons on the catalyzer.Flow around the heat exchange fluid that is used for controlled temperature around the pipe.During entry into service.The gas composition that enters reactor is: 6%O
2, 27%C
2O
4, 6ppm vinylchlorid, 0.1% ethane, 41ppm 2-nitropropane, all the other are methane and small amounts of inert gas substantially.The reactor feed temperature is 75%, and pressure is 18.5 crust, and gas space-time speed is 3600/ hour.Then temperature of reactor is improved initiation reaction.By required feed composition, with oxygen, ethene, ethane, methane, 2-nitropropane and vinylchlorid raw material mix with recycle gas.With positive discharge capacity micropump liquid 2-nitropropane is squeezed into system, this pump has the safety valve of starting working when 30 crust.The temperature of 2-nitropropane is about 20 ℃ in the pump, does not contain air, oxygenant, alkali, acid and water substantially.The 2-nitropropane temperature at feed points place on stream is 70 ℃, and pressure is 18 crust (absolute pressure), by flow process all gas braiding stainless (steel) wire of process all, enters flow process with 4.8 milliliters/hour amount of liquid.
After turning round 14 days, the feed composition that analyzes reactor is 8.2%O
2, 27%C
2H
4, 1%CO
2, 5.9ppm vinylchlorid, 0.8ppm monochlorethane, 0.1% ethane, 32ppm 2-nitropropane, 8.3ppm NO
2, 2.0ppm NO, 0.12% water vapor, all the other are methane substantially.Analysis is that the ingress at reactor carries out, and finds thus because the condensation of water is adopted the 2-nitropropane than adopting NO and NO
2The analytical results that obtains is more accurate.The temperature of reaction feed is 75 ℃, and pressure is 18.5 crust, and gas space-time speed is 3340/ hour, and the transformation efficiency of process reactor oxygen is 28%.The selectivity of ethylene that the reaction back is transformed is 84.2%.The average catalyst temperature is 250 ℃.Earlier gaseous product is cooled to 75 ℃, again with its with 20 ℃, 250 liters/hour water contact, absorption product of ethylene oxide.The air-flow of Sheng Chenging divides two-way to walk then, a part in carbon dioxide scrubber with 250 liters/hour, the 0.5%(w/w) caustic soda solution contact.Converge from gaseous product and that another part bypass fluid that scrubber comes out, and be compressed into circulating current.The reaction of nitropropane and ethene does not cause producing deposition of solids.(NO/NO under certain conditions,
2With ethene in addition at room temperature all can cause deposition).Do not observe that reactor feed partly has the corrosion situation in the equipment.
Ppm means, and is the parts by weight of each 1,000,000 parts of weight to liquid or solid; To gas is the volume parts of each 1,000,000 parts of volume.Gas space-time speed is to calculate under 20 ℃ of temperature and normal atmosphere.
All the pressure in the specification is absolute pressure.
Revisal 85107325
After the preceding revisal of the capable revisal of file name page or leaf
Specification sheets 7 falls the right cylinder of 8 millimeters on right cylinder of 39 millimeters long
83 (4,418) (4,418 gram)
85 single Isopropylamines.Add waist and want (4800 milliliters of single Isopropylamines
（mls）〕。
92 methyl alcohol that contain potassium formiate contain 3323 milliliters of potassium formiates
(mls) methyl alcohol
10 3～4 C
2O
4，7.2ppm C
2H
4，0.3%CO
2，7.2
Vinylchlorid ppm vinylchlorid
10 fall 5 for 330ppm be 300-330ppm
10 fall 2 27%C
2O
427%C
2H
4
Claims (11)
1, produce the method for oxyethane, this method is that ethene is contacted with silver-containing catalyst in the presence of chloride reaction control agent with oxygen, wherein by catalyzer is also contacted the performance of having improved catalyzer with nitropropane.
2, method according to claim 1, catalyzer wherein contain the silver that is stated from the porous thermal resistance carrier, and the specific surface area of carrier is determined as 0.05 to 10 meter by Bruauer Emmett and Teller method
2/ gram, apparent porosity is at least 20% by the mercury absorptionmetric determination.
3, method according to claim 1 and 2, wherein catalyzer contains the silver that is deposited on α-alumina carrier, and alkaline-earth metal and/or (better being) basic metal are to exist with the form that water can extract it from catalyzer.
4, according to the described method of aforementioned arbitrary claim, wherein nitropropane is squeezed into system with positive-displacement pump with liquid form being no more than under 80 ℃ of temperature, and this pump has and prevents the security devices of pressure greater than 50 crust.
5, according to the described method of aforementioned arbitrary claim, wherein to enter the feed points place temperature of flow process be 50 to 100 ℃ to nitropropane, and pressure is up to 40 crust.
6, method according to claim 5, nitropropane enters the inertia porous material with alap pressure, and flow process gas is kept a basic flow velocity constantly by this porous material.
7, according to the described method of aforementioned arbitrary claim, the dividing potential drop of therein ethylene is 0.1 to 30 crust, and stagnation pressure is 1 to 100 crust, and oxygen partial pressure is 0.01 to 20 crust, and temperature is 180 to 320 ℃.
8, according to the described method of aforementioned arbitrary claim, wherein chloride reaction control agent comprises ethylene dichloride, monochloro methane or vinylchlorid.
9, according to the described method of aforementioned arbitrary claim, wherein with gas that catalyzer contacts in CO
2Average content be 1% to 7%(volume).
10, according to the described method of aforementioned arbitrary claim, wherein nitropropane is the 2-nitropropane.
11, the oxyethane for preparing by the described method of aforementioned arbitrary claim.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85107325A CN1010585B (en) | 1984-09-12 | 1985-09-30 | Production of ethylene oxide |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB848423044A GB8423044D0 (en) | 1984-09-12 | 1984-09-12 | Production of ethylene oxide |
| CN85107325A CN1010585B (en) | 1984-09-12 | 1985-09-30 | Production of ethylene oxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85107325A true CN85107325A (en) | 1987-04-15 |
| CN1010585B CN1010585B (en) | 1990-11-28 |
Family
ID=25742086
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85107325A Expired CN1010585B (en) | 1984-09-12 | 1985-09-30 | Production of ethylene oxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1010585B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100400524C (en) * | 2003-02-28 | 2008-07-09 | 国际壳牌研究有限公司 | A method of manufacturing ethylene oxide |
-
1985
- 1985-09-30 CN CN85107325A patent/CN1010585B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100400524C (en) * | 2003-02-28 | 2008-07-09 | 国际壳牌研究有限公司 | A method of manufacturing ethylene oxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1010585B (en) | 1990-11-28 |
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