CN110357836A - A kind of ethylene oxide production method - Google Patents
A kind of ethylene oxide production method Download PDFInfo
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- CN110357836A CN110357836A CN201810252748.9A CN201810252748A CN110357836A CN 110357836 A CN110357836 A CN 110357836A CN 201810252748 A CN201810252748 A CN 201810252748A CN 110357836 A CN110357836 A CN 110357836A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/04—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen
- C07D301/08—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase
- C07D301/10—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase with catalysts containing silver or gold
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
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- 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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Abstract
The invention belongs to catalyst fields, and in particular to a kind of ethylene oxide production method, comprising the following steps: (1) by the reaction gas containing ethylene, oxygen under conventional ethylene epoxidation reaction condition with silver catalyst haptoreaction；(2) when catalyst choice is lower than the first preset value, reaction condition is adjusted, air speed 6000-10000h is made‑1, space-time yield is 270-450Kg EO/h/m3- cat, the reaction was continued；(3) when catalyst choice is higher than the second preset value, restore to conventional ethylene epoxidation reaction condition, the reaction was continued；(4) optional repetition step (2)-(3)；Second preset value is higher than first preset value.Method of the invention can improve the selectivity of silver catalyst especially bigger serface rhenium-containing silver catalyst, it is made to have more application prospect, improve the economy of ethylene oxide production.
Description
Technical field
The invention belongs to catalyst fields, more particularly, to a kind of ethylene oxide production method.
Background technique
Ethylene oxide is a kind of important petrochemicals and organic synthesis intermediate, currently, mainly gas-solid by ethylene
The production of phase catalytic epoxidation, used catalyst are Alpha-alumina carried metal silver catalyst.As a kind of important petroleum
Chemical catalyst, so far, silver catalyst are the epoxidation of ethylene production the only effective catalyst of ethylene oxide.
In vapor solid ethylene catalyst epoxidation reaction system, main reaction is that (1) ethylene selectivity is oxidized to ethylene oxide
(EO) it reacts, main side reaction is that (2) ethylene complete oxidation is that carbon dioxide and water reaction and (3) EO depth (complete) are oxidized to
Carbon dioxide and water reaction；Three reactions are irreversible exothermic reaction.EO is the purpose product of the reaction system, generates EO's
Selectivity is largely fixed the economy of entire production technology, so, developing more highly selective silver catalyst becomes
The Main way of research.Currently, the highest of ethylene catalyst epoxidation reaction selectively reaches 90% or so, silver catalyst master used
It will be there are two types of type: (1) rhenium-containing silver catalyst；(2) the not rhenium-containing silver catalyst of oxides of nitrogen gas auxiliary agent is added.
The not rhenium-containing silver catalyst system for adding oxides of nitrogen gas auxiliary agent produces more due to introducing gas auxiliary agent
Byproduct, post-reaction treatment technique is more complex, reduces its economy, this is its major defect.In contrast, rhenium-containing silver is catalyzed
Agent equally can reach 90% or so highest selectivity, and reaction process and subsequent processing are simpler, so being industrially widely available
Using.
Since epoxidation of ethylene system is strongly exothermic reaction, to avoid transmittance process (mass transfer and diabatic process) from dropping
The selectivity that low EO is generated, industrial silver catalyst answer multiselect specific surface area 1.0m2The alpha-oxidation of the low specific surface area of/g or so
Alumina supporter carried metal silver ((1) Gates B.C.Catalytic Chemistry, New York:John Wiley&Sons,
Inc.1992:392-396；(2)Mao C F,Vannice M A.High surface area α-aluminas
III.Oxidation of ethylene,ethylene oxide,and acetaldehyde over silver
dispersed on high surface areaα-alumina[J].Applied Catalysis A:General,1995,
122(122):61-76.).The specific surface area of industrial silver catalyst and carrier is not higher than 1.6m mostly2/g。
When the specific surface area of carrier and silver catalyst is larger, due to catalyst inner duct and the metal silver granuel ruler of load
Very little smaller, silver catalyst shows the phenomenon that activity is higher and selectivity is lower, causes ethylene material consumption high, reduces EO production
Economy limits the application of such catalyst.The highly selective silver catalyst of rhenium-containing equally exists such problems.
Therefore, bigger serface (especially specific surface area >=2.0m how is improved2/ g or more) rhenium-containing silver catalyst choosing
Selecting property is an important technical problem.Economy for improving EO production is of great significance.
Summary of the invention
Based on above-mentioned prior art scenario, the present inventor is studied by a large number of experiments, discovery regulation reaction process
Condition can improve the selectivity of silver catalyst especially bigger serface rhenium-containing silver catalyst, it is thus found that a kind of feasible reality
EO production method.
Specifically, the present invention provides a kind of ethylene oxide production method, comprising the following steps:
(1) by the reaction gas containing ethylene, oxygen under conventional ethylene epoxidation reaction condition with silver catalyst haptoreaction；
(2) when catalyst choice is lower than the first preset value, reaction condition is adjusted, air speed 6000-10000h is made-1,
Space-time yield is 270-450Kg EO/h/m3- cat, preferably 290-420Kg EO/h/m3- cat, the reaction was continued；
(3) when catalyst choice is higher than the second preset value, restore to conventional ethylene epoxidation reaction condition, continue anti-
It answers；
(4) optional repetition step (2)-(3)；
Second preset value is higher than first preset value.
According to the method for the present invention, air speed and space-time yield, catalyst choice are improved in lower catalyst choice
The selectivity of catalyst can be improved after progress is one or many by restoring conventional ethylene epoxidation reaction condition after raising.Wherein,
As long as improving air speed and space-time yield in lower catalyst choice, restore conventional ethylene ring when catalyst choice is higher
Said effect can be realized in oxidation reaction condition.Therefore, first preset value of catalyst choice can be set as needed
With the second preset value, as long as second preset value be higher than first preset value.
In actual industrial production, to obtain ideal catalyst choice and as energy-saving as possible, described first in advance
If value and second preset value are preferably provided with certain big difference, it is preferable that catalyst choice is in terms of percentage, and described second
More than preset value one percentage point higher than first preset value, preferably described second preset value is higher by two than first preset value
Percentage point or more.
Particularly preferably, first preset value is 82%-86%, and second preset value is 84%-92%；Further
Preferably, first preset value is 83%-85%, and second preset value is 86%-92%.
In the present invention, the measuring method of the catalyst choice is as follows: under certain process conditions, when under stable reaction
Come, and reach setting reaction condition after, METHOD FOR CONTINUOUS DETERMINATION reactor inlet and exit gas composition.Measurement result carries out volume contraction
Selectivity (S) is calculated after correction as follows:
Wherein, Δ EO is reactor outlet gas and inlet gas ethylene oxide concentration difference, Δ CO2For reactor outlet gas with
Gas concentration lwevel is poor in inlet gas.The response data for choosing multiple groups (such as ten groups or more) daily, was averaged as the same day
Reaction temperature and selective data.
The method that method of the invention is not limited to above-mentioned calculating selectivity.As long as first preset value and described second
Preset value uses unified calculation.
In method of the invention, step (2)-(3) can be repeated according to actual needs and determine duplicate number.When repetition walks
Suddenly when (2)-(3), duplicate first preset value and the first preset value before are identical or different；Duplicate second preset value is therewith
The second preceding preset value is identical or different.It can flexibly determine that first preset value and described second is preset according to actual needs
Value, as long as meeting second preset value higher than the first preset value or preferably satisfying above-mentioned difference.
Step (1) the catalytic time is not particularly limited in the present invention, even can be 0, that is, reaction is at the beginning
It is just carried out under higher air speed and space-time yield, according to the specific condition of production, normally, when catalytic in step (1)
Between can be 0-200 days, preferably 0.1-130 days, in a specific embodiment, the catalytic time was preferably 3-40
It；The time that the reaction was continued in step (2) can be 5-150 days, and in a specific embodiment, the time that the reaction was continued is excellent
It is selected as 7-60 days.Method of the invention may be selected that reaction is adjusted within the above-mentioned time, and specific regulating time point can root
According to above-mentioned standard and combine determining needed for actual production.
According to the present invention, the conventional ethylene epoxidation reaction condition can be the various conventional ethylene epoxidation reactions in this field
Condition, generally, the conventional ethylene epoxidation reaction condition include: that reaction temperature is 200-280 DEG C, system pressure 1-
3MPa, air speed 2500-6000h-1, space-time yield is 145-260Kg EO/h/m3-cat。
There is no particular limitation for the composition of method of the invention to reaction gas, can routinely form for this field, normally, with
On the basis of the total volume of reaction gas, ethylene contents are 10vol%-40vol%, oxygen content 5vol%- in the reaction gas
10vol%.In addition, reaction gas can also contain carbon dioxide, inhibitor and Balance Air, the inhibitor is usually chloralkane,
Balance Air is usually nitrogen.In the reaction gas, carbon dioxide content can be 0mol%-2.0mol%, and inhibitor content can be
0.2-2.0ppmv, surplus are Balance Air.
According to the present invention, it in step (3), when space-time yield and air speed, which require, to be reduced, preferably realizes step by step described extensive
Again to conventional ethylene epoxidation reaction condition: first reducing space-time yield (preferably by first reducing EO concentration), then reduce air speed.From
And operational safety is improved, reduce fuel factor bring temperature runaway phenomenon.
In the present invention, increases or decreases space-time yield and preferably pass through adjusting outlet EO concentration realization.
Recovery described in step (3) is not meant to be restored to step (1) one to conventional ethylene epoxidation reaction condition
The condition of cause, as long as restoring to conventional ethylene epoxidation reaction condition.
Method of the invention is suitable for various silver catalysts, is particularly suitable for Large ratio surface (>=2.0m2/ g) silver catalyst,
Especially suitable for Large ratio surface (>=2.0m2/ g), the silver catalyst of high rhenium constituent content, such catalyst can be significantly improved
Selectivity.
Particularly preferably, silver catalyst of the present invention includes the silver and alkali gold of alpha-alumina supports and load thereon
Category, alkaline-earth metal, rhenium auxiliary agent and optional rhenium collaboration auxiliary agent；With the total weight of silver catalyst, the content of rhenium element is
300-2000ppmw, preferably 400-1800ppmw, further preferably 500-1500ppmw, more preferably 600-
1200ppmw；The specific surface area of the silver catalyst is 2.0-4.0m2/ g, preferably 2.1-3.5m2/g。
In addition, the silver catalyst further preferably has at least one of following characteristics:
The average pore diameter of the silver catalyst is 0.5-3.0 μm, preferably 0.6-2.0 μm；
The content of the silver is 10-40wt%, with the total weight of silver catalyst；
The alkali metal is selected from least one of lithium, sodium, potassium, rubidium and caesium, content 10-2000ppmw, preferably
100-1600ppmw, with the total weight of silver catalyst；
The alkaline-earth metal is selected from least one of magnesium, calcium, strontium and barium, content 10-10000ppmw, preferably
10-4000ppmw, with the total weight of silver catalyst；
The collaboration auxiliary agent of the rhenium in boron, fluorine, sulphur, cerium, chromium, molybdenum, tungsten, titanium, zirconium, cobalt, nickel, copper and zinc at least
One kind, content 10-2000ppmw, preferably 20-1500ppmw, with the total weight of silver catalyst.
The content of each metal component of catalyst is with elemental metal in the present invention.
Above-mentioned catalyst is commercially available, or is made using the preparation method of this field routine.The preparation method example
Such as: alpha-alumina supports being immersed in the solution of silver compound, organic amine compound and auxiliary agent, then filtered and activated heat
The catalyst is made in processing；The auxiliary agent includes the collaboration auxiliary agent of alkali metal, alkaline-earth metal, rhenium auxiliary agent and optional rhenium.Its
In, the rhenium auxiliary agent is soluble rhenium salt, preferably potassium perrhenate and/or ammonium perrhenate.
Method of the invention can improve the selectivity of silver catalyst especially bigger serface rhenium-containing silver catalyst, make it
More application prospect improves the economy of ethylene oxide production.
Other features and advantages of the present invention will then part of the detailed description can be specified.
Specific embodiment
The preferred embodiment of the present invention is described in more detail below.
In following embodiment and comparative example, catalytic perfomance evaluates the stainless steel tubular microreactors in internal diameter about 4mm
Middle progress, the catalyst that filling 1mL 12-22 purpose is crossed after crushing and screening in reaction tube.A certain amount of reaction gas passes through when reaction
The reactor of heating, the gas composition of quantitative analysis mass spectral analysis unstripped gas and reaction end gas, the content with purpose product EO are
Target, the temperature of serials control heating furnace.
In following embodiment and comparative example, popular response condition includes:
Reaction gas forms (mol%):
Under certain process conditions, when stable reaction is got off, and after reaching setting reaction condition, METHOD FOR CONTINUOUS DETERMINATION reactor inlet
It is formed with exit gas.Measurement result calculates selectivity (S) after carrying out volume contraction correction as follows:
Wherein, Δ EO is reactor outlet gas and inlet gas ethylene oxide concentration difference, Δ CO2For reactor outlet gas with
Gas concentration lwevel is poor in inlet gas.The response data for choosing ten groups or more daily, is averaged the reaction temperature as the same day
And selective data.
In following embodiment and comparative example, the specific surface area (S of catalystBET) using the nitrogen physisorption side BET of standard
Method measurement, catalyst average pore diameter use 4V/SBET(V is pore volume, using mercury injection method) is calculated.Silver contains in catalyst
Amount is measured using x-ray fluorescence analysis (XRF), and other elements content uses inductively coupled plasma atomic emission spectrometry method
(ICP-AES) it determines.
The silver catalyst can be prepared by following conventional silver catalyst preparation method:
(1) a certain amount of ethylenediamine and/or ethanol amine and deionized water are added in the glass flask of belt stirrer, obtains
Mixed liquor；A certain amount of powdery silver oxalate is slowly added in mixed liquor while stirring, keeps solution temperature at 0-15 DEG C, makes
Silver oxalate all dissolves.Caesium, strontium, rhenium and in boron, fluorine, sulphur, cerium, chromium, molybdenum, tungsten, titanium, zirconium, cobalt, nickel, copper, zinc are added later
One or more of rheniums collaboration auxiliary agent, acquired solution is uniformly mixed, argentiferous maceration extract is obtained；
(2) a certain amount of porosity alpha-alumina supports (specific surface area 1.8-3.5m is taken2/ g) it immerses in above-mentioned acquired solution,
30min is impregnated under vacuumized conditions；
(3) leaching removes redundant solution, thermally decomposes 5min in 250 DEG C of air streams.
Above-mentioned (1)~(3) step is repeated, the silver catalyst for requiring constituent content is obtained.
Comparative example 1
The silver catalyst CAT1 for weighing 1mL (about 0.8g), is fitted into the microreactor of internal diameter 0.4mm, in popular response
Condition carries out catalysis reaction using reaction process process as shown in table 1.Evaluation results are shown in Table 1 for catalytic perfomance.
The silver catalyst CAT1 is alpha-alumina supports carried silver catalyst, using the total weight of silver catalyst CAT1 as base
It is quasi-, wherein silver content 35wt%, rhenium content are 660ppmw, and caesium content is 360ppmw, and alkaline earth metal content is
2300ppmw, Ti content 260ppmw, the specific surface area of the catalyst are 2.1m2/ g, average pore diameter are 1.30 μm.
Embodiment 1
Using silver catalyst CAT1 described in comparative example 1, the condition with comparative example 1 is formed in reaction condition and reaction gas
Under, catalysis reaction is carried out using reaction process process as shown in table 1, evaluation results are shown in Table 1 for catalytic perfomance.
Table 1
As can be seen from Table 1, using reaction process method of the present invention, comparative example 1 is compared, height is presented in embodiment 1
Up to 88.5% selectivity, after 180 days reduction air speeds, it is selectively still maintained at 88% or more.
Embodiment 2
The silver catalyst CAT2 for weighing 1mL (0.80g), is fitted into the microreactor of internal diameter 0.4mm, using such as 2 institute of table
Show that reaction process process carries out catalysis reaction.Reactivity worth evaluation result is shown in Table 2.
The silver catalyst CAT2 is alpha-alumina supports carried silver catalyst, using the total weight of silver catalyst CAT2 as base
It is quasi-, wherein metal silver content is 36wt%, and rhenium content is 386ppmw, and alkali metal caesium content is 520ppmw, alkaline earth metal content
For 2060ppmw, nickel content 310ppmw, the specific surface area of the silver catalyst is 3.1m2/ g, average pore diameter are 0.65 μm.
Comparative example 2
Using the silver catalyst CAT2 of embodiment 2, the condition with embodiment 2 is formed in reaction condition and reaction gas
Under, catalysis reaction is carried out using reaction process process as shown in table 2, reactivity worth evaluation result is shown in Table 2.
Embodiment 3
The silver catalyst CAT3 for weighing 1mL (0.80g), is fitted into the microreactor of internal diameter 0.4mm, using such as 2 institute of table
Show that reaction process process carries out catalysis reaction, other reaction conditions and reaction gas composition are the same as embodiment 2.
The silver catalyst CAT3 is alpha-alumina supports carried silver catalyst, using the total weight of silver catalyst CAT3 as base
It is quasi-, wherein metal silver content is 36.1wt%, and rhenium content is 722ppmw, and alkali metal caesium content is 560ppmw, and alkaline-earth metal contains
Amount is 2430ppmw, nickel content 321ppmw, which is 3.2m2/ g, average pore diameter are 0.62 μm.
Reactivity worth evaluation result is shown in Table 2.
Table 2
As can be seen from Table 2, the selectivity of comparative example 2 is compared using the embodiment 2 of reaction process method of the present invention
It is higher, illustrate that method of the invention can be improved silver catalyst especially bigger serface silver catalyst (such as 2.0-4.0m2/g)
Selectivity.
It shows apparent selectivity and improves within embodiment 3 16 days after first time improves air speed and EO concentration, and two
Presented up to after secondary adjusting 88% it is highly selective, show excellent catalytic perfomance.As it can be seen that process of the invention
To promotion bigger serface (such as 2.0-4.0m2/ g), high rhenium content (such as 400ppmw or more) silver catalyst be rapidly achieved high selection
Character state effect is more obvious, and this kind of silver catalyst is made to have bigger practical value.
Various embodiments of the present invention are described above, above description is exemplary, and non-exclusive, and
It is not limited to disclosed each embodiment.Without departing from the scope and spirit of illustrated each embodiment, for this skill
Many modifications and changes are obvious for the those of ordinary skill in art field.
Claims (10)
1. a kind of ethylene oxide production method, comprising the following steps:
(1) by the reaction gas containing ethylene, oxygen under conventional ethylene epoxidation reaction condition with silver catalyst haptoreaction；
(2) when catalyst choice is lower than the first preset value, reaction condition is adjusted, air speed 6000-10000h is made-1, space-time
Yield is 270-450Kg EO/h/m3- cat, preferably 290-420Kg EO/h/m3- cat, the reaction was continued；
(3) when catalyst choice is higher than the second preset value, restore to conventional ethylene epoxidation reaction condition, the reaction was continued；
(4) optional repetition step (2)-(3)；
Second preset value is higher than first preset value.
2. ethylene oxide production method according to claim 1, wherein catalyst choice is in terms of percentage, and described second
More than preset value one percentage point higher than first preset value, preferably described second preset value is higher by two than first preset value
Percentage point or more.
3. ethylene oxide production method according to claim 2, wherein first preset value is 82%-86%, described
Second preset value is 84%-92%；Preferably, first preset value is 83%-85%, and second preset value is 86%-
92%.
4. ethylene oxide production method according to claim 1, wherein repeat the first preset value when step (2)-(3)
It is identical or different with the first preset value before；Repeat the second preset value and the second preset value before when step (2)-(3)
It is identical or different.
5. ethylene oxide production method according to claim 1, wherein the catalytic time is 0-200 in step (1)
It；The time that the reaction was continued in step (2) is 5-150 days.
6. ethylene oxide production method according to claim 1, wherein the conventional ethylene epoxidation reaction condition packet
Include: reaction temperature is 200-280 DEG C, system pressure 1-3MPa, air speed 2500-6000h-1, space-time yield 145-260Kg
EO/h/m3-cat。
7. ethylene oxide production method according to claim 1, wherein described anti-on the basis of the total volume of reaction gas
It should ethylene contents be 10-40vol%, oxygen content 5-10vol% in gas.
8. ethylene oxide production method according to claim 1, wherein in step (3), realize described restore to normal step by step
Rule epoxidation of ethylene condition: space-time yield is first reduced, then reduces air speed.
9. ethylene oxide production method according to claim 1, wherein the silver catalyst include alpha-alumina supports and
Load silver thereon and alkali metal, alkaline-earth metal, rhenium auxiliary agent and optional rhenium collaboration auxiliary agent；With the gross weight of silver catalyst
Meter, the content of rhenium element are 300-2000ppmw, preferably 400-1800ppmw, further preferably 500-1500ppmw；
The specific surface area of the silver catalyst is 2.0-4.0m2/ g, preferably 2.1-3.5m2/g。
10. ethylene oxide production method according to claim 9, wherein the silver catalyst has in following characteristics
At least one:
The average pore diameter of the silver catalyst is 0.5-3.0 μm, preferably 0.6-2.0 μm；
The content of the silver is 10-40wt%, with the total weight of silver catalyst；
The alkali metal is selected from least one of lithium, sodium, potassium, rubidium and caesium, content 10-2000ppmw, with silver catalyst
Total weight；
The alkaline-earth metal is selected from least one of magnesium, calcium, strontium and barium, content 10-10000ppmw, with silver catalyst
Total weight；
The collaboration auxiliary agent of the rhenium is selected from least one of boron, fluorine, sulphur, cerium, chromium, molybdenum, tungsten, titanium, zirconium, cobalt, nickel, copper and zinc,
Its content is 10-2000ppmw, with the total weight of silver catalyst.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1060839A (en) * | 1989-10-18 | 1992-05-06 | 联合碳化化学品及塑料有限公司 | The alkylene oxide catalyst that contains high silver content |
| CN102421766A (en) * | 2009-04-21 | 2012-04-18 | 陶氏技术投资有限公司 | Methods for enhancing the efficiency of rhenium-promoted epoxidation catalysts and epoxidation methods utilizing these |
| CN104803953A (en) * | 2014-01-28 | 2015-07-29 | 中国石油化工股份有限公司 | Olefin epoxidation method |
-
2018
- 2018-03-26 CN CN201810252748.9A patent/CN110357836B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1060839A (en) * | 1989-10-18 | 1992-05-06 | 联合碳化化学品及塑料有限公司 | The alkylene oxide catalyst that contains high silver content |
| CN102421766A (en) * | 2009-04-21 | 2012-04-18 | 陶氏技术投资有限公司 | Methods for enhancing the efficiency of rhenium-promoted epoxidation catalysts and epoxidation methods utilizing these |
| CN104803953A (en) * | 2014-01-28 | 2015-07-29 | 中国石油化工股份有限公司 | Olefin epoxidation method |
Non-Patent Citations (1)
| Title |
|---|
| 丁国敏: ""吉林石化公司EO/EG装置节碳减排技术研究"", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
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