CN108358752A - A kind of method of acetic acid hydrogenation ethyl alcohol - Google Patents
A kind of method of acetic acid hydrogenation ethyl alcohol Download PDFInfo
- Publication number
- CN108358752A CN108358752A CN201810348973.2A CN201810348973A CN108358752A CN 108358752 A CN108358752 A CN 108358752A CN 201810348973 A CN201810348973 A CN 201810348973A CN 108358752 A CN108358752 A CN 108358752A
- Authority
- CN
- China
- Prior art keywords
- acetic acid
- catalyst
- ethyl alcohol
- weight
- hydrogen
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/835—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with germanium, tin or lead
-
- 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
- Y02P20/584—Recycling of catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a kind of method of acetic acid hydrogenation ethyl alcohol, the method is：In 150~250 DEG C of temperature, 0.1~3.0MPa of pressure, mass space velocity 10~12 hours‐1, hydrogen and acetic acid feed substance the ratio between amount 1:1~20:Under conditions of 1, acetic acid and hydrogen are mixed, the Fe-Sn/Al with support type2O3Catalyst contact carries out hydrogenation reaction, obtains ethyl alcohol, and catalyst price can obtain ethyl alcohol under conditions of low-temp low-pressure high-speed, reduce ethyl alcohol and obtain production cost compared with low activity height.
Description
Technical field
The present invention relates to organic chemical industry field more particularly to a kind of methods of acetic acid hydrogenation ethyl alcohol.
Background technology
Ethyl alcohol is a kind of good liquid fuel, and sulphur content and ash content are relatively low, and combustibility is similar to gasoline, has higher contain
Oxygen amount and octane number, burning compared with regular gasoline, complete, CO emission is low, and burning can be significantly decreased using ethanol petrol
Environmental pollution caused by gasoline, ethyl alcohol are referred to as 21 century " green energy resource ".With oil supply and demand aggravation of contradictions, environmental pressure
Increasingly heavy, common concern fungible energy source in countries in the world has pushed the development of alcohol fuel.Existing ethyl alcohol production technology is most
It using crops as raw material, is limited by raw material, production cost is higher, it is difficult to meet the needs of alcohol fuel.Acetic acid catalysis adds
Hydrogen is the feasible path of ethanol production, and the effective way by the indirect preparing liquid fuel of coal.With Development of Coal Chemical Industry, acetic acid supplies
More than asking.It can not only solve the problems, such as that ethyl alcohol produces by acetic acid hydrogenation ethyl alcohol, moreover it is possible to effectively solve the problems, such as acetic acid excess capacity,
Thus the technique has become the hot spot studied both at home and abroad.
Numerous studies are carried out about the hydrogenation catalyst and reaction process of acetic acid hydrogenation ethyl alcohol both at home and abroad.Hydrogenation catalyst
Agent is mainly urged using load type palladium or platinum catalyst, the load type palladium containing other metals or platinum catalyst and copper support type
Agent.Since palladium and platinum are noble metal, load type palladium or platinum catalyst are expensive, and ethyl alcohol production cost is higher.In addition, due to
Copper loaded catalyst stability is poor, which is difficult to commercial Application.The base metal that development cost is low, performance is stablized adds
Hydrogen catalyst and acetic acid hydrogenation technique are important developing direction.
The key of acetic acid direct hydrogenation ethyl alcohol technology is to develop the catalysis of high acetic acid conversion ratio, high ethano selectivity
Agent, less due to studying, so development difficulty is larger, but in recent years, this respect is making important progress.Related document report
A kind of load type bimetal catalyst Pt-Fe/SiO2.The bimetallic can increase the reduction of Fe relative to single-metal reforming catalyst
Ability, eliminates decomposition induction time and avoids Fe from generating cementite during the reaction and cause to react intensified response activity
Inactivation.But the key reaction product of this catalyst is acetaldehyde, ethanol selectivity is only up to 40%.
US20100197485A1 is disclosed is added CaSiO3 in Pt-Sn/SiO2 catalyst systems, 250 DEG C, 22bar,
Under the conditions of GHSV2500h-1, the selectivity of ethyl alcohol can reach 92%, but the conversion ratio of acetic acid only has 24%.
CN103170337A disclose it is a kind of for producing catalyst of ethyl alcohol and preparation method thereof, it is a kind of using bimetallic catalyst
Metal is noble metal platinum, ruthenium or palladium, and another metal is iron, cobalt or tin.But bullion content is relatively high, is 2%.
Invention content
It is an object of the present invention to provide a kind of methods of acetic acid hydrogenation ethyl alcohol, that is, use the Fe-Sn/Al of support type2O3Catalyst
The method of acetic acid hydrogenation ethyl alcohol solves load type palladium or platinum catalyst expensive caused ethanol synthesis temperature and pressure
The problems such as power is high, air speed is low.
The present invention provides a kind of Fe-Sn/Al with support type2O3The method of catalyst acetic acid preparation of ethanol by hydrogenating, the side
Method is：In 150~250 DEG C of temperature, 0.1~3.0MPa of pressure, mass space velocity 10~12 hours‐1, hydrogen and acetic acid feed substance
The ratio between amount 1:1~20:Under conditions of 1, acetic acid and hydrogen are mixed, the Fe-Sn/Al with support type2O3Catalyst contact carries out
Hydrogenation reaction obtains ethyl alcohol；It regenerates, recycles after catalyst inactivation；
The Fe-Sn/Al of the support type2O3Catalyst uses base metal Fe and Sn as active component, can be effectively
Improve acetic acid conversion, ethanol selectivity and the yield in acetic acid hydrogenation ethanol synthesis.Particularly, in the catalyst Fe and
The content of Sn within the above range when, catalyst is more preferable to the improvement of acetic acid hydrogenation ethanol synthesis.Under preferable case, Fe
Weight ratio with Sn is 1：0.1‐10；Preferably, the weight ratio of Fe and Sn is 1：0.3‐8.The weight ratio for regulating and controlling Fe and Sn can be with
Preferably improve selectivity, the yield of the conversion ratio and ethyl alcohol of acetic acid.
The present invention also provides a kind of method for the catalyst preparing acetic acid hydrogenation ethyl alcohol provided by the invention, this method
Including：(1) in carrier Al2O3Middle introducing compound containing Fe and compound containing Sn, obtain catalyst precarsor；(2) by the catalyst
Precursor restores under hydrogen atmosphere, obtains the catalyst of acetic acid hydrogenation ethyl alcohol.
There is provided in method provided by the invention in carrier Al2O3Middle introducing compound containing Fe and compound containing Sn, it is therefore an objective to
Finally in order to introduce active component, specially Fe and Sn into the catalyst of the acetic acid hydrogenation ethyl alcohol of preparation.
In the case of, according to the invention it is preferred to, the compound containing Fe, compound containing Sn and carrier Al2O3Addition make
To the acetic acid hydrogenation ethyl alcohol catalyst in, on the basis of the total weight of the catalyst of the acetic acid hydrogenation ethyl alcohol,
The content of Fe is that the content of 1-25 weight %, SN are 5-25 weight % and the content of carrier is 50-94 weight %；Preferably,
The content of Fe is that the content of 7-23 weight %, Sn are 5-20 weight % and the content of carrier is 57-88 weight %.
According to the present invention, the compound containing Fe can be that carrier Al can be added2O3Obtain catalyst precarsor and in step
(2) substance of Fe can be changed under conditions of the reduction in；Under preferable case, the compound containing Fe is ferric nitrate, chlorination
At least one of iron, frerrous chloride, ferrous nitrate.
According to the present invention, the compound containing Sn can be that carrier can be added to obtain catalyst precarsor and in step (2)
In reduction under conditions of can be changed into the substance of Sn.Under preferable case, the compound containing Sn is butter of tin or chlorination
Stannous.
The regeneration method of the Fe-Sn/Al2O3 catalyst of the support type is off into acetic acid raw material, continues to be passed through hydrogen
Gas is 100~1000h in 300 DEG C~600 DEG C of temperature, 0.8~6.0MPa of pressure, hydrogen volume air speed‐1Under the conditions of to inactivation urge
Agent carry out reactor in plus hydrogen regeneration 3~for 24 hours.
Further, the reaction is carried out in the reactor of two or more serial or parallel connections, each reactor
The identical or different catalyst of interior filling.
The optional fixed bed of reactor, expanded bed, fluid bed, stirred-tank reactor used by present invention reaction, and
Catalytic distillation reactor.Reaction unit can have multiple reactors to operate in parallel or series.Material in reactor can be taken
Upstriker can also use downstriker.
A kind of advantageous effect of the method for acetic acid hydrogenation ethyl alcohol of the present invention is mainly reflected in：
(1) the Fe-Sn/Al2O3 catalyst price of support type, can be under conditions of low-temp low-pressure high-speed compared with low activity height
Ethyl alcohol is obtained, ethyl alcohol is reduced and obtains production cost；
(2) catalyst activity stability is good, and the device stable operation time is long, can avoid reactor reaction and regeneration is frequently cut
Change operation；
(3) catalyst is renewable, can avoid a large amount of dead catalyst post-processings, and effect on environment is small.
Specific implementation mode
The following is a clear and complete description of the technical scheme in the embodiments of the invention, it is clear that described embodiment
Only a part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, the common skill in this field
The every other embodiment that art personnel are obtained without making creative work belongs to the model that the present invention protects
It encloses.
【Embodiment 1】
A certain amount of ferric nitrate and butter of tin and deionized water are mixed evenly, it is molten to obtain the dipping containing Fe-Sn
Liquid；A certain amount of α-Al are added in above-mentioned dipping solution2O3Carrier stands aging for 24 hours at room temperature, then through 80 DEG C of dry 4h,
700 DEG C of roasting 4h, are made catalyst precarsor；
Catalyst precarsor is restored, reduction temperature is 400 DEG C, recovery time 10h, and hydrogen contains in hydrogen atmosphere
Amount is 15 volume %, and the volume space velocity of hydrogen atmosphere is 2000h‐1, obtain catalyst I.By adjusting active component and carrier
Dosage so that the group of catalyst I becomes：9.3 weight %, the α-Al of content of content 11.5 the weight %, Sn of Fe2O3Content
79.2 weight %.
【Embodiment 2】
A certain amount of ferric nitrate and butter of tin and deionized water are mixed evenly, it is molten to obtain the dipping containing Fe-Sn
Liquid；A certain amount of γ-Al are added in above-mentioned dipping solution2O3Carrier stands aging for 24 hours at room temperature, then through 80 DEG C of dry 4h,
700 DEG C of roasting 4h, are made catalyst precarsor；
Catalyst precarsor is restored, reduction temperature is 400 DEG C, recovery time 10h, and hydrogen contains in hydrogen atmosphere
Amount is 15 volume %, and the volume space velocity of hydrogen atmosphere is 2000h‐1, obtain catalyst II.By adjusting active component and carrier
Dosage so that the group of catalyst II becomes：8.8 weight %, the γ-Al of content of content 13.2 the weight %, Sn of Fe2O3Contain
Measure 78 weight %.
【Embodiment 3】
A certain amount of ferric nitrate and butter of tin and deionized water are mixed evenly, it is molten to obtain the dipping containing Fe-Sn
Liquid；A certain amount of γ-Al are added in above-mentioned dipping solution2O3Carrier stands aging for 24 hours at room temperature, then through 80 DEG C of dry 4h,
700 DEG C of roasting 4h, are made catalyst precarsor；
Catalyst precarsor is restored, reduction temperature is 400 DEG C, recovery time 10h, and hydrogen contains in hydrogen atmosphere
Amount is 15 volume %, and the volume space velocity of hydrogen atmosphere is 2000h‐1, obtain catalyst III.By adjusting active component and load
The dosage of body so that the group of catalyst III becomes：12.1 weight %, the γ-Al of content of content 8.6 the weight %, Sn of Fe2O3's
79.3 weight % of content.
【Embodiment 4】
A certain amount of ferric nitrate and butter of tin and deionized water are mixed evenly, it is molten to obtain the dipping containing Fe-Sn
Liquid；A certain amount of α-Al are added in above-mentioned dipping solution2O3Carrier stands aging for 24 hours at room temperature, then through 80 DEG C of dry 4h,
700 DEG C of roasting 4h, are made catalyst precarsor；
Catalyst precarsor is restored, reduction temperature is 400 DEG C, recovery time 10h, and hydrogen contains in hydrogen atmosphere
Amount is 15 volume %, and the volume space velocity of hydrogen atmosphere is 2000h-1, obtains catalyst IV.By adjusting active component and load
The dosage of body so that the group of catalyst I becomes：9.3 weight %, the α-Al of content of content 11.5 the weight %, Sn of Fe2O3Contain
Measure 79.2 weight %.
【Embodiment 5】
Using fixed-bed reactor, in 220 DEG C of temperature, pressure 0.5MPa, quality of acetic acid air speed 11h‐1, hydrogen and second into
Expect molar ratio 10:Under 1 reaction condition, acetic acid hydrogenation reaction is carried out with catalyst I~IV of above-mentioned preparation, evaluates catalyst
Catalytic performance, experimental result are listed in table 1.
Table 1
Above description has fully disclosed the specific implementation mode of the present invention.It should be pointed out that being familiar with the field
Technical staff is to any change for being done of specific implementation mode of the present invention all without departing from the range of claims of the present invention.
Correspondingly, the scope of the claims of the invention is also not limited only to previous embodiment.
Claims (6)
1. a kind of method of acetic acid hydrogenation ethyl alcohol, it is characterised in that：In 150~250 DEG C of temperature, 0.1~3.0MPa of pressure, matter
Measure air speed 10~12 hours‐1, hydrogen and acetic acid feed substance the ratio between amount 1:1~20:Under conditions of 1, acetic acid and hydrogen are mixed
It closes, the Fe-Sn/Al with support type2O3Catalyst contact carries out hydrogenation reaction, obtains ethyl alcohol, is regenerated after catalyst inactivation, is recycled
It utilizes.
2. the method for acetic acid hydrogenation ethyl alcohol according to claim 1, which is characterized in that the Fe-Sn/ of the support type
Al2O3Catalyst uses base metal Fe and Sn as active component, and the weight ratio of Fe and Sn are 1：0.1‐10；Preferably, Fe and
The weight ratio of Sn is 1：0.3-8, on the basis of the total weight of the catalyst of the acetic acid hydrogenation ethyl alcohol, the content of Fe is 1-25
The content of weight %, SN are 5-25 weight % and the content of carrier is 50-94 weight %；Preferably, the content of Fe is 7-23
The content of weight %, Sn are 5-20 weight % and the content of carrier is 57-88 weight %.
3. the method for acetic acid hydrogenation ethyl alcohol according to claim 2, which is characterized in that the Fe-Sn/ of the support type
Al2O3The preparation method of catalyst is：(1) in carrier Al2O3Middle introducing compound containing Fe and compound containing Sn, obtain catalyst
Precursor；(2) catalyst precarsor is restored under hydrogen atmosphere, obtains the catalyst of acetic acid hydrogenation ethyl alcohol.
4. the method for acetic acid hydrogenation ethyl alcohol according to claim 3, which is characterized in that the compound containing Fe can be
Carrier Al can be added2O3Obtain the substance that can be changed into Fe under conditions of catalyst precarsor and reduction in step (2)；
Under preferable case, the compound containing Fe is at least one of ferric nitrate, iron chloride, frerrous chloride, ferrous nitrate.
5. the method for acetic acid hydrogenation ethyl alcohol according to claim 3, it is characterised in that：The compound containing Sn can be
Carrier can be added and obtain the substance that can be changed into Sn under conditions of catalyst precarsor and reduction in step (2), preferably
In the case of, the compound containing Sn is butter of tin or stannous chloride.
6. the method for acetic acid hydrogenation ethyl alcohol according to claim 3, it is characterised in that：The Fe-Sn/ of the support type
The regeneration method of Al2O3 catalyst is off into acetic acid raw material, continues to be passed through hydrogen, in 300 DEG C~600 DEG C of temperature, pressure 0.8
~6.0MPa, hydrogen volume air speed are 100~1000h‐1Under the conditions of to decaying catalyst carry out reactor in plus hydrogen regeneration 3~
24h。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810348973.2A CN108358752A (en) | 2018-04-18 | 2018-04-18 | A kind of method of acetic acid hydrogenation ethyl alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810348973.2A CN108358752A (en) | 2018-04-18 | 2018-04-18 | A kind of method of acetic acid hydrogenation ethyl alcohol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108358752A true CN108358752A (en) | 2018-08-03 |
Family
ID=63008608
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810348973.2A Pending CN108358752A (en) | 2018-04-18 | 2018-04-18 | A kind of method of acetic acid hydrogenation ethyl alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108358752A (en) |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102271805A (en) * | 2009-10-26 | 2011-12-07 | 国际人造丝公司 | Processes for making ethanol from acetic acid |
| CN102333588A (en) * | 2009-10-26 | 2012-01-25 | 国际人造丝公司 | Be used for preparing the catalyst of ethanol by acetate |
| CN102378647A (en) * | 2009-10-26 | 2012-03-14 | 国际人造丝公司 | Processes for making ethanol or ethyl acetate from acetic acid using bimetallic catalysts |
| CN102421735A (en) * | 2010-02-01 | 2012-04-18 | 国际人造丝公司 | Preparation method for making tin- containing catalyst |
| CN102557871A (en) * | 2009-10-26 | 2012-07-11 | 国际人造丝公司 | Catalyst comprising platinum and tin on silica-containing supporter for producing ethanol by adding hydrogen to acetic acid |
| CN102658165A (en) * | 2012-04-06 | 2012-09-12 | 华东理工大学 | Catalyst for preparing ethanol by acetic acid gas phase hydrogenation and preparation method thereof |
| CN102850184A (en) * | 2010-02-02 | 2013-01-02 | 国际人造丝公司 | Process for purifying ethanol |
| CN104039747A (en) * | 2011-12-29 | 2014-09-10 | 国际人造丝公司 | Cobalt and tin catalyst for producing ethanol |
| CN104093484A (en) * | 2012-02-10 | 2014-10-08 | 国际人造丝公司 | A hydrogenation catalyst for converting a mixture comprising acetic acid and ethyl acetate to ethanol |
| CN104275194A (en) * | 2014-10-10 | 2015-01-14 | 上海华谊（集团）公司 | Catalyst used in preparation of alcohol from acetic acid by hydrogenation and preparation method of catalyst |
| CN107321357A (en) * | 2017-05-24 | 2017-11-07 | 沈阳三聚凯特催化剂有限公司 | A kind of preparation method and applications of acetic acid hydrogenation catalyst |
| CN107349947A (en) * | 2017-05-24 | 2017-11-17 | 沈阳三聚凯特催化剂有限公司 | A kind of acetic acid hydrogenation catalyst and its application |
-
2018
- 2018-04-18 CN CN201810348973.2A patent/CN108358752A/en active Pending
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102271805A (en) * | 2009-10-26 | 2011-12-07 | 国际人造丝公司 | Processes for making ethanol from acetic acid |
| CN102333588A (en) * | 2009-10-26 | 2012-01-25 | 国际人造丝公司 | Be used for preparing the catalyst of ethanol by acetate |
| CN102378647A (en) * | 2009-10-26 | 2012-03-14 | 国际人造丝公司 | Processes for making ethanol or ethyl acetate from acetic acid using bimetallic catalysts |
| CN102557871A (en) * | 2009-10-26 | 2012-07-11 | 国际人造丝公司 | Catalyst comprising platinum and tin on silica-containing supporter for producing ethanol by adding hydrogen to acetic acid |
| CN102421735A (en) * | 2010-02-01 | 2012-04-18 | 国际人造丝公司 | Preparation method for making tin- containing catalyst |
| CN103638990A (en) * | 2010-02-01 | 2014-03-19 | 国际人造丝公司 | Preparation method for making tin-containing catalyst |
| CN102850184A (en) * | 2010-02-02 | 2013-01-02 | 国际人造丝公司 | Process for purifying ethanol |
| CN104039747A (en) * | 2011-12-29 | 2014-09-10 | 国际人造丝公司 | Cobalt and tin catalyst for producing ethanol |
| CN104093484A (en) * | 2012-02-10 | 2014-10-08 | 国际人造丝公司 | A hydrogenation catalyst for converting a mixture comprising acetic acid and ethyl acetate to ethanol |
| CN102658165A (en) * | 2012-04-06 | 2012-09-12 | 华东理工大学 | Catalyst for preparing ethanol by acetic acid gas phase hydrogenation and preparation method thereof |
| CN104275194A (en) * | 2014-10-10 | 2015-01-14 | 上海华谊（集团）公司 | Catalyst used in preparation of alcohol from acetic acid by hydrogenation and preparation method of catalyst |
| CN107321357A (en) * | 2017-05-24 | 2017-11-07 | 沈阳三聚凯特催化剂有限公司 | A kind of preparation method and applications of acetic acid hydrogenation catalyst |
| CN107349947A (en) * | 2017-05-24 | 2017-11-17 | 沈阳三聚凯特催化剂有限公司 | A kind of acetic acid hydrogenation catalyst and its application |
Non-Patent Citations (7)
| Title |
|---|
| 何杰: "《工业催化》", 31 August 2014 * |
| 储伟: "《催化剂工程》", 30 September 2006 * |
| 李立权: "加氢催化剂再生技术", 《炼油技术与工程》 * |
| 林丽: "乙酸加氢催化剂的开发", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
| 田树勋: "乙酸选择性加氢制乙醇反应性能研究", 《燃料化学学报》 * |
| 魏家骏: "醋酸直接加氢制乙醇催化剂组成研究进展", 《化工管理》 * |
| 黄新平: "加氢催化剂的失活及其再生技术的发展", 《第八届全国工业催化技术及应用年会论文集》 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105289592B (en) | It is catalyzed method of the levulic acid Hydrogenation for γ valerolactones | |
| CN105561993B (en) | Acetic acid preparation of ethanol by hydrogenating coproduction ethyl acetate catalyst and preparation method | |
| US20230256423A1 (en) | Modified copper-zinc catalysts and methods for alcohol production from carbon dioxide | |
| CN102658165B (en) | Catalyst for preparing ethanol by acetic acid gas phase hydrogenation and preparation method thereof | |
| CN103896769A (en) | Method used for preparing methyl acetate via carbonylation of dimethyl ether | |
| CN103896768A (en) | Method used for preparing methyl acetate | |
| CN104148086B (en) | Prepare the catalyst and method of ethanol | |
| CN103170337A (en) | Catalyst for producing ethanol and preparation method thereof | |
| CN104275194A (en) | Catalyst used in preparation of alcohol from acetic acid by hydrogenation and preparation method of catalyst | |
| JP4953195B2 (en) | Propanediol production method | |
| CN107841332A (en) | The method that aviation kerosine scope alkane is prepared using biomass alcohol compound as hydrogen source | |
| CN104710282B (en) | Method for producing ethanol co-production methanol | |
| CN103664587B (en) | Method for preparing cyclohexyl acetate and method for preparing cyclohexanol ethanol | |
| CN103664529A (en) | Method for coproducing cyclohexanol and ethanol | |
| CN103880598B (en) | A kind of method of coproduction hexalin and ethanol and device | |
| CN102908957A (en) | Method for Fischer-Tropsch synthesis | |
| CN103240095A (en) | Methyl acetate hydrogenation catalyst and preparation method thereof | |
| CN103170338B (en) | A kind of catalyst for being used for 1,2 propane diols and preparation method thereof | |
| CN110498780B (en) | Method for preparing tetrahydrofurfuryl acid by gas-phase hydrogenation of furoic acid | |
| CN103566933B (en) | A kind of acetate preparation of ethanol by hydrogenating catalyst and preparation method thereof | |
| CN105503521B (en) | The method of acetic acid preparation of ethanol through hydrogenation | |
| CN109705069B (en) | Preparation method of 2, 5-furandicarboxylic acid | |
| CN107488457B (en) | A kind of biomass liquid fuel and the preparation method and application thereof | |
| CN108358752A (en) | A kind of method of acetic acid hydrogenation ethyl alcohol | |
| CN107597116A (en) | A kind of method that 1,4 pentanediols are prepared by copper-based catalysts direct hydrogenation levulic acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180803 |
|
| RJ01 | Rejection of invention patent application after publication |