CN1287885A - Catalyst and process for prodn. of alkyl benzene - Google Patents
Catalyst and process for prodn. of alkyl benzene Download PDFInfo
- Publication number
- CN1287885A CN1287885A CN99113813A CN99113813A CN1287885A CN 1287885 A CN1287885 A CN 1287885A CN 99113813 A CN99113813 A CN 99113813A CN 99113813 A CN99113813 A CN 99113813A CN 1287885 A CN1287885 A CN 1287885A
- Authority
- CN
- China
- Prior art keywords
- zeolite
- catalyst
- alkylbenzene
- propylene
- reaction
- 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.)
- Granted
Links
Classifications
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The present invention relates to catalyst used in the production of alkylbenzene and its use method. The present invention uses catalyst of palladium loaded on zeolite and reaction technology under conditions of liquid phuse, 150-250 deg.C reaction temperature and 0.7-4.0 HPa reaction pressure, so as to overcome the demerits of poor stability, short regeneration period and low spacevelocity. It can be used in the production of alkylbenzene.
Description
The present invention relates to the method that is used to produce the catalyst of alkylbenzene and adopts this Catalyst Production alkylbenzene, more particularly, the present invention relates to the zeolite catalyst of carried metal palladium and adopt it to produce the method for alkylbenzene.
Isopropylbenzene is a kind of important Organic Chemicals, belongs to the substituted arene compound.It is a main intermediate compound of producing phenol, acetone and AMS, also is simultaneously the auxiliary element as aviation gasoline, to increase the octane number of gasoline.The catalyst of propylene and benzene synthesizing iso-propylbenzene has multiple, traditional catalyst that crystallization and noncrystalline silica, boron fluoride, aluminium oxide and phosphoric acid, alchlor and solid phosphoric acid catalyst are arranged.All there are shortcomings such as seriously corroded, equipment investment is big, the three wastes are many in these conventional catalyst technologies.In recent years, deep day by day along with molecular sieve research, people are conceived to develop the new technology that zeolite catalyst is produced isopropylbenzene.Reported the new technology of utilizing the y-type zeolite molecular sieve to produce isopropylbenzene among the patent documentation EP0272830.This patented technology has overcome the deficiency of using traditional catalyst to exist, but also there is the poor stability of catalyst in it, the regeneration period short (just needed in 700 hours for example driving regeneration); Reaction velocity is low (for example in propylene air speed 0.10hr only
-1), shortcoming such as plant capacity is low.
One of purpose of the present invention is the shortcoming that has poor catalyst stability in the above-mentioned document in order to overcome, and a kind of new catalyst that is used to produce alkylbenzene is provided, and this catalyst has the characteristics of good stability.
Two of purpose of the present invention is short in order to overcome in the above-mentioned document regeneration period, and the shortcoming that reaction velocity is low provides a kind of new method that is used to produce alkylbenzene, and this method has production capacity and can improve, the characteristics that the catalyst regeneration cycle is long.
One of purpose of the present invention is to realize by following technical scheme: a kind of catalyst that is used to produce alkylbenzene, form by following component:
A) silica alumina ratio is 2～20 zeolite and is stated from the zeolite;
B) be 0.003～0.05% Metal Palladium by weight percentage.
The silica alumina ratio of technique scheme mesolite is 2～8, and zeolite is Y zeolite, β zeolite, modenite or ZSM-5 zeolite, and its preferred version is the Y zeolite, and alkylbenzene is ethylbenzene or isopropylbenzene.
Two of purpose of the present invention is to realize by following technical scheme: a kind of method that is used to produce alkylbenzene, with propylene or ethene and benzene is raw material, in reaction temperature is 150～250 ℃, reaction pressure is 0.7～4.0MPa, benzene/olefin molar ratio is that liquid phase is synthetic under 4～20 conditions, and catalyst system therefor is made up of following component:
A) silica alumina ratio is 2～20 zeolite and is stated from the zeolite;
B) be 0.003～0.05% Metal Palladium by weight percentage.
The reaction temperature preferred version is 180～210 ℃ in the technique scheme, and the reaction pressure preferred version is 2.0～3.5MPa.
Catalyst of the present invention can prepare as follows:
A) with silica alumina ratio be 2～20 zeolite with acid, ammonium salt exchange, make the content of sodium metal ion in zeolitic frameworks below 0.1% (weight), then oven dry;
B) impregnating metal palladium on zeolite.
The acid and the ammonium salt that are used to handle zeolite can be acid commonly used and ammonium salt, for example hydrochloric acid, nitric acid or phosphoric acid etc., and ammonium chloride, ammonium sulfate or ammonium phosphate etc.
Method of the present invention is carried out in the fixed bed mode usually.
The present invention is 0.003～0.05% Metal Palladium by weight percentage by load on zeolite, suppressed the carbon distribution that reaction mass generates at the catalyst surface dehydrocyclization effectively, thereby improved the reaction stability of catalyst, prolonged the regeneration period of catalyst.Use catalyst of the present invention that the hydrogenation reaction of raw material olefin does not take place in course of reaction in addition, by using two the technical scheme that realizes purpose, making reaction mass is 2.0 hours in weight liquid air speed
-1Reaction is 1000 hours under the condition, uses Y or β zeolite, does not detect propylene or ethene in its product, and activity of such catalysts, selectivity do not descend, and have obtained effect preferably.The reaction mechanism inventor of the present invention still is difficult to get across at present.
The invention will be further elaborated below by embodiment.[embodiment 1]
Getting 100 gram silica alumina ratios is 5.0 NaY type zeolite powder, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.003% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.Is that 90: 10 amount is mediated with the zeolite of carried metal palladium and aluminium oxide with weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 2]
Getting 100 gram silica alumina ratios is 5.0 NaY type zeolite powder, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.02% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.Is that 90: 10 amount is mediated with the zeolite of carried metal palladium and aluminium oxide with weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 3]
Getting 100 gram silica alumina ratios is 5.0 NaY type zeolite powder, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.008% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.Is that 90: 10 amount is mediated with the zeolite of carried metal palladium and aluminium oxide with weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 4]
Getting 100 gram silica alumina ratios is 5.0 NaY type zeolite powder, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.045% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.The zeolite and the aluminium oxide of carried metal palladium are mediated with 90: 10 amount of weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 5]
Getting 100 gram silica alumina ratios is 14.0 the former powder of zeolite beta, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.035% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.The zeolite and the aluminium oxide of carried metal palladium are mediated with 90: 10 amount of weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 6]
Getting 100 gram silica alumina ratios is 20.0 ZSM-type zeolite powder, with the hydrochloric acid exchange, with the ammonium chloride exchange, makes the Na in the zeolite again
+Ion concentration is less than 0.1% (weight).Will be through the zeolite PdCl of above-mentioned processing
2Solution impregnation makes that Metal Palladium content is 0.03% (weight) in the catalyst, after oven dry, the roasting, grinds evenly.The zeolite and the aluminium oxide of carried metal palladium are mediated with 90: 10 amount of weight ratio, and pressure forming is the shape of 1.6 millimeters of φ.[embodiment 7]
Catalyst 21 grams of getting embodiment 1 place fixed bed reactors, under 210 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 702 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 97.5% (calculating with propyl group).[embodiment 8]
Catalyst 21 grams of getting embodiment 2 place fixed bed reactors, under 200 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 585 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 98.0% (calculating with propyl group).[embodiment 9]
Catalyst 21 grams of getting embodiment 3 place fixed bed reactors, under 205 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 670 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 97.7% (calculating with propyl group).[embodiment 10]
Catalyst 21 grams of getting embodiment 4 place fixed bed reactors, under 195 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 468 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 98.0% (calculating with propyl group).[embodiment 11]
Catalyst 21 grams of getting embodiment 5 place fixed bed reactors, under 215 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 702 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 96.0% (calculating with propyl group).[embodiment 12]
Catalyst 84 grams of getting embodiment 6 place fixed bed reactors, under 215 ℃, 2.6MPa condition, benzene and propylene are reacted by beds, wherein the benzene inlet amount is 702 Grams Per Hours, the propylene feed amount is 42 Grams Per Hours, is 2.0 hours with propylene calculated weight liquid air speed
-1This reaction was investigated through 45 hours, did not detect propylene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 95.0% (calculating with propyl group).[embodiment 13]
Catalyst 21 gram of getting embodiment 4 places fixed bed reactors, under 250 ℃, 4.0MPa condition, benzene and ethene is reacted by beds, and wherein the benzene inlet amount is 400 Grams Per Hours, is 0.5 hour with ethene calculated weight liquid air speed
-1This reaction was investigated through 1000 hours, did not detect ethene in the product, and activity of such catalysts, selectivity do not descend.Selectivity is 90.0% (calculating with ethyl).
Claims (8)
1, a kind of catalyst that is used to produce alkylbenzene, form by following component:
A) silica alumina ratio is 2～20 zeolite and is stated from the zeolite;
B) be 0.003～0.05% Metal Palladium by weight percentage.
2, according to the described catalyst that is used to produce alkylbenzene of claim 1, the silica alumina ratio that it is characterized in that zeolite is 2～8.
3,, it is characterized in that zeolite is Y zeolite, β zeolite, modenite or ZSM-5 zeolite according to the described catalyst that is used to produce alkylbenzene of claim 1.
4,, it is characterized in that zeolite is the Y zeolite according to the described catalyst that is used to produce alkylbenzene of claim 3.
5,, it is characterized in that alkylbenzene is ethylbenzene or isopropylbenzene according to claim 1,2, the 3 or 4 described catalyst that are used to produce alkylbenzene.
6, a kind of method that is used to produce alkylbenzene, with propylene or ethene and benzene is raw material, is 150～250 ℃ in reaction temperature, and reaction pressure is 0.7～4.0MPa, benzene/olefin molar ratio is that liquid phase is synthetic under 4～20 conditions, it is characterized in that catalyst system therefor is made up of following component:
A) silica alumina ratio is 2～20 zeolite and is stated from the zeolite;
B) be 0.003～0.05% Metal Palladium by weight percentage.
7,, it is characterized in that reaction temperature is 180～210 ℃ according to the described method that is used to produce alkylbenzene of claim 6.
8,, it is characterized in that reaction pressure is 2.0～3.5MPa according to the described method that is used to produce alkylbenzene of claim 6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99113813A CN1114493C (en) | 1999-06-24 | 1999-06-24 | Catalyst and process for prodn. of alkyl benzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99113813A CN1114493C (en) | 1999-06-24 | 1999-06-24 | Catalyst and process for prodn. of alkyl benzene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1287885A true CN1287885A (en) | 2001-03-21 |
| CN1114493C CN1114493C (en) | 2003-07-16 |
Family
ID=5276963
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99113813A Expired - Fee Related CN1114493C (en) | 1999-06-24 | 1999-06-24 | Catalyst and process for prodn. of alkyl benzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1114493C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111330631A (en) * | 2020-04-08 | 2020-06-26 | 中国石油大学(华东) | Preparation method of modified molecular sieve loaded Pd catalyst and application of modified molecular sieve loaded Pd catalyst in synthesis of dimethyl carbonate by gas phase method |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62246532A (en) * | 1986-04-16 | 1987-10-27 | Maruzen Petrochem Co Ltd | Alkylation of phenol |
| CN1053175C (en) * | 1996-01-25 | 2000-06-07 | 中国石油化工总公司 | Process for preparation of alkyl benzene |
-
1999
- 1999-06-24 CN CN99113813A patent/CN1114493C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111330631A (en) * | 2020-04-08 | 2020-06-26 | 中国石油大学(华东) | Preparation method of modified molecular sieve loaded Pd catalyst and application of modified molecular sieve loaded Pd catalyst in synthesis of dimethyl carbonate by gas phase method |
| CN111330631B (en) * | 2020-04-08 | 2022-09-16 | 中国石油大学(华东) | Preparation method of modified molecular sieve loaded Pd catalyst and application of modified molecular sieve loaded Pd catalyst in synthesis of dimethyl carbonate by gas phase method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1114493C (en) | 2003-07-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1283608C (en) | Method for preparing dimethyl ether by crude carbinol | |
| CN102746092B (en) | Method for separating and producing 1,3,5-trimethylbenzene through hydrocracking heavy aromatic hydrocarbons | |
| CN102039161B (en) | C8 arene isomerization catalyst and application thereof | |
| CN101417234A (en) | Preparation method of catalyst for shape-selective alkylation of naphthalene to produce 2,6-di(tert butyl)naphthalene | |
| CN101352690A (en) | Preparation method and use of molecular sieve catalyst for producing phenylethane from alkylation of benzene with dilute ethylene | |
| CN102909058B (en) | Catalyst containing modified EUO type molecular sieve, and preparation method and application thereof | |
| CN102746091B (en) | Method for producing BTX (benzene, toluene and xylol) aromatic hydrocarbons and trimethylbenzene from heavy aromatic hydrocarbons | |
| CN102441420B (en) | C8 aromatic hydrocarbon isomerization catalyst, preparation method and application thereof | |
| CN1098028A (en) | Beta-zeolite molecular sieve catalyst and preparation method thereof | |
| CN102039159B (en) | Xylene isomerization catalyst and application thereof | |
| CN1114493C (en) | Catalyst and process for prodn. of alkyl benzene | |
| CN100531907C (en) | Catalyst for alkyl transfer of polyalkylbenzene | |
| CN1028514C (en) | Process for isomerizing normal paraffin hydrocarbon in presence of at least one catalyst based on particular omega zeolite | |
| CN102909057B (en) | Catalyst comprising EUO type zeolite, preparation method and applications thereof | |
| CN1055876C (en) | Alkylated catalyst for preparation of alkylbenzene | |
| CN100553772C (en) | Be used to produce alkylbenzene Preparation of catalysts method | |
| CN101190869B (en) | Production increasing method for propylene | |
| CN1053175C (en) | Process for preparation of alkyl benzene | |
| CN1187299C (en) | Method for preparing ethylbenzene by liquid phase alkylation of ethylene | |
| CN100553773C (en) | The catalyst that is used for the diisopropylbenzene (DIPB) transalkylation | |
| CN103120949B (en) | Methylbenzene methylation catalyst for increasing production of o-xylene and p-xylene and preparation method thereof | |
| CN102309979B (en) | Catalyst for isomerizing ethyl benzene into dimethyl benzene and preparation method and application thereof | |
| CN109701598B (en) | Catalyst for preparing aromatic hydrocarbon from methanol and application thereof | |
| CN102441419B (en) | C8 aromatic hydrocarbon isomerization catalyst and preparation method and application thereof | |
| CN102746093B (en) | Heavy aromatics hydrocracking is utilized to increase production the method for BTX aromatic hydrocarbons and trimethylbenzene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20030716 Termination date: 20110624 |