CN1647855A - Catalyst containing MCM-22 zeolite - Google Patents
Catalyst containing MCM-22 zeolite Download PDFInfo
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- CN1647855A CN1647855A CN 200410000957 CN200410000957A CN1647855A CN 1647855 A CN1647855 A CN 1647855A CN 200410000957 CN200410000957 CN 200410000957 CN 200410000957 A CN200410000957 A CN 200410000957A CN 1647855 A CN1647855 A CN 1647855A
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- zeolite
- mcm
- catalyzer
- heavy
- catalyst
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- 229910021536 Zeolite Inorganic materials 0.000 title claims abstract description 44
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 239000010457 zeolite Substances 0.000 title claims abstract description 44
- 239000003054 catalyst Substances 0.000 title abstract description 31
- 239000000126 substance Substances 0.000 claims abstract description 14
- 229910052736 halogen Inorganic materials 0.000 claims abstract description 10
- 150000002367 halogens Chemical class 0.000 claims abstract description 10
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910052731 fluorine Inorganic materials 0.000 claims description 14
- 239000011737 fluorine Substances 0.000 claims description 14
- 239000000203 mixture Substances 0.000 claims description 12
- 239000000460 chlorine Substances 0.000 claims description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 6
- 229910052801 chlorine Inorganic materials 0.000 claims description 6
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims description 2
- 229910052794 bromium Inorganic materials 0.000 claims description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 claims 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 abstract description 33
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 abstract description 26
- 239000011159 matrix material Substances 0.000 abstract description 13
- 239000007791 liquid phase Substances 0.000 abstract description 12
- KVNYFPKFSJIPBJ-UHFFFAOYSA-N 1,2-diethylbenzene Chemical compound CCC1=CC=CC=C1CC KVNYFPKFSJIPBJ-UHFFFAOYSA-N 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- VIDOPANCAUPXNH-UHFFFAOYSA-N 1,2,3-triethylbenzene Chemical compound CCC1=CC=CC(CC)=C1CC VIDOPANCAUPXNH-UHFFFAOYSA-N 0.000 abstract description 3
- 230000002152 alkylating effect Effects 0.000 abstract 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 12
- 239000008367 deionised water Substances 0.000 description 12
- 229910021641 deionized water Inorganic materials 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 238000005804 alkylation reaction Methods 0.000 description 11
- 238000001035 drying Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 206010013786 Dry skin Diseases 0.000 description 8
- 229940079593 drug Drugs 0.000 description 8
- 238000000465 moulding Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 6
- 230000029936 alkylation Effects 0.000 description 6
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 150000002366 halogen compounds Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 3
- 150000003863 ammonium salts Chemical class 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229910017604 nitric acid Inorganic materials 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 238000004898 kneading Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 101000643890 Homo sapiens Ubiquitin carboxyl-terminal hydrolase 5 Proteins 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- MXRIRQGCELJRSN-UHFFFAOYSA-N O.O.O.[Al] Chemical compound O.O.O.[Al] MXRIRQGCELJRSN-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 1
- 102100021017 Ubiquitin carboxyl-terminal hydrolase 5 Human genes 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- -1 halogen group compound Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention is a kind of catalyst containing MCM-22 zeolite 30-90 wt%, halogen counting in simple substance 0.1-2 wt% and alumina matrix in the balanced amount. The catalyst is used in liquid phase benzene alkylating reaction, and compared with available technology, the catalyst has raised ethyl benzene selectivity, lowered diethyl benzene and triethyl benzene selectivity, and 7.3-10.0 % raised ethyl benzene STY.
Description
Technical field
The present invention relates to a kind of catalyzer of the MCM-22 of containing zeolite, further say to relate to a kind of catalyzer that contains the MCM-22 zeolite that is used for the benzene liquid phase alkylation reaction.
Background technology
Ethylbenzene is important Organic Chemicals, is mainly used in production vinylbenzene.Industrial mainly is to make by the benzene alkylation with ethylene reaction.In its preparation method, traditional AlCl
3The production technique of method ethylbenzene is because its catalyzer is to the deep-etching of equipment with to the severe contamination of environment, at present by the technology by catalyzer is replaced with the molecular sieve.And molecular sieve vapor-phase alkylation method is because the temperature of reaction height, and the xylene content height is replaced by the molecular sieve liquid phase method gradually.People claim that the molecular sieve liquid phase method is an environmentally friendly technology condition relaxes, selectivity is good, impurity is few because this technology has, pollution-free, do not have an advantage such as corrosion.Recently this technology has become the more satisfactory method of ethylbenzene production.
In the molecular sieve liquid phase method, used alkylation catalyst mainly is zeolite catalysts such as USY, Beta, MCM-22.USP5 discloses the result of MCM-22, MCM-49, MCM-56 and the Beta zeolite catalyst comparison in liquid-phase alkylation ethylbenzene is produced in 453,554.MCM-22 zeolite catalyst selectivity is better than the Beta zeolite catalyst, but its activity will be lower than the latter.
On catalyzer scientific and technical conference in 1998 (the Science and Technology in Catalysis 1998) collection of thesis, J.C.CHENG etc. compare USY, Beta, the application of MCM-22 zeolite catalyst in benzene and ethene liquid phase alkylation reaction, in three kinds of catalyzer, MCM-22 zeolite catalyst selectivity is best, but its activity will be lower than the Beta zeolite catalyst.A.corma etc. also think in the article that 163-173 (2000) delivers that at Journal ofCatalysis192 the activity of MCM-22 zeolite catalyst is lower than the Beta zeolite catalyst.
At present, do not see as yet have on the document further raising contain the benzene liquid-phase alkylation activity of such catalysts of MCM-22 zeolite and optionally the report.
Summary of the invention
The purpose of this invention is to provide a kind of benzene liquid-phase alkylation catalyzer that contains the MCM-22 zeolite that contains new component, this catalyzer has higher activity and selectivity.
The catalyzer that contains the MCM-22 zeolite provided by the invention contains the MCM-22 zeolite of 30～90 heavy % and the alumina host of equal amount, it is characterized in that also containing the halogen in simple substance 0.1～2 heavy %, preferred 0.5～1.5 heavy %.
In the catalyzer provided by the invention, said halogen is selected from the mixture of one or both or three kinds in fluorine, chlorine and the bromine, wherein preferred fluorine and/or chlorine.Said MCM-22 zeolite, its SiO
2/ Al
2O
3Be preferably 15～50.Said matrix alumina be selected from amorphous alumina, various low temperature transition aluminas (ρ-, χ-, η-, γ-), various high temperature transition aluminas (κ-, δ-, θ-) or Alpha-alumina in one or more mixture, wherein preferred γ-Al
2O
3As matrix
Catalyzer provided by the invention is with MCM-22 zeolite and matrix Al
2O
3And halogen compounds, nitric acid, deionized water kneading and compacting, obtain through steps such as super-dry, roasts then.
(1) the MCM-22 zeolite is carried out ammonium and exchange the NaO that makes wherein
2Content exchanges (ammonium salt and MCM-22 zeolite weight ratio be 1.0～2.0) with ammonium salt aqueous solution less than 0.1 heavy %:MCM-22 zeolite under 80 ℃～90 ℃, wash then, filter, and 100～120 ℃ were descended the preferred NH of said ammonium salt dry 2～8 hours
4Cl, (NH
4)
2SO
4Or NH
4NO
3
(2) according to the product proportioning, with NaO
2Content is less than MCM-22 zeolite and the matrix Al of 0.1 heavy %
2O
3Mix, add halogen compounds, nitric acid and deionized water mix pinch, extrusion, and drying and roasting obtain the said catalyzer of the present invention.Adding nitric acid is the dissolving for the promotes oxidn aluminum matrix, strengthens the intensity of alumina host, and its add-on accounts for 0.5～2.5 heavy % of catalyzer butt, and the add-on of deionized water is pinched mixing, extrusion is as the criterion.
Said halogen compounds can be fluorochemical, muriate or bromide, wherein is preferred with the fluorochemical, for example BF
3, NH
4BF
3, HF, NH
4F etc.The method that nonmetal halogen group compound is introduced can adopt kneading method, also can adopt solution impregnation and steam treatment process.
The catalyzer that contains the MCM-22 zeolite provided by the invention is feature to introduce halogen as catalyst component, has improved the acidity of the acidity of catalyzer, particularly protonic acid.When this catalyzer is used for the benzene liquid phase alkylation reaction, compare with not halogen-containing MCM-22 zeolite catalyst, ethylbenzene selectivity has raise 2.8～3.2% relatively, the selectivity of diethylbenzene and triethyl-benzene has reduced by 41.0～47.0%, 70.8～79.2% respectively, and the ethylbenzene space-time yield has increased by 7.3～10.0%.Because ethylbenzene selectivity improves, many ethylbenzene selectivity obviously descend, and have improved the utilization ratio of ethene and benzene, have prolonged the running period of catalyzer.
Embodiment
The following examples will the invention will be further described, but not thereby limiting the invention.
Embodiment 1
With 80g NH
4NO
3(chemical pure, Beijing Meng Li fine chemicals company limited) is dissolved in the 3200ml deionized water, and the back that stirs adds MCM-22 zeolite (production of Chang Ling catalyst plant, the SiO of 80g
2/ Al
2O
3=25, Na
2The heavy % of O 0.5),, uses the deionized water wash of 6400ml then, 120 ℃ of dryings 2 hours 90 ℃ of exchanges 2 hours down.
Get 43g MCM-22 zeolite and 22g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 0.49gNH
4F (chemical pure, Beijing company of China Drug Co. sells), the HNO of 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature, obtain the heavy % of MCM-22 zeolite content 70 (is the theoretical value that benchmark calculates with the catalyzer butt, below identical), fluorine content is the catalyst A of 0.5 heavy %.
Embodiment 2
Get 43g MCM-22 zeolite and 22g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 0.97gNH
4F (chemical pure, Beijing company of China Drug Co. sells), the HNO of 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature, obtaining MCM-22 zeolite content 70 heavy %, fluorine content is the catalyst B of 1.0 heavy %.
Embodiment 3
Get 43g MCM-22 zeolite and 22g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 0.97gNH
4F (chemical pure, Beijing company of China Drug Co. sells), and deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature obtains MCM-22 zeolite content 70 heavy %, fluorine content is the catalyzer C of 1.0 heavy %.
Embodiment 4
Get 43g MCM-22 zeolite and 22g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 1.41gNH
4Cl (chemical pure, Beijing company of China Drug Co. sells), the HNO of 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature, obtaining MCM-22 zeolite content 70 heavy %, cl content is the catalyzer D of 1.0 heavy %.
Embodiment 5
Get 43gMCM-22 zeolite and 22g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %, H
2The heavy % of O30, specific surface area 335m
2g
-1, pore volume 0.8ml.g
-1) mix, add 1.41gNH
4Cl (chemical pure, Beijing company of China Drug Co. sells), 0.49gNH
4F, the HNO of (chemical pure, Beijing company of China Drug Co. sells) and 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature obtains the catalyzer E of MCM-22 zeolite content 70 heavy %, chloride and fluorine total content 1.5 heavy %.
Embodiment 6
Get 49gMCM-22 zeolite and 14g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 0.97gNH
4F (chemical pure, Beijing company of China Drug Co. sells), the HNO of 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature, obtaining MCM-22 zeolite content about 80 heavy %, fluorine content is the catalyzer of 1.0 heavy %.
Embodiment 7
Get 25g MCM-22 zeolite and 44g matrix Al
2O
3(Wenzhou catalyst plant is produced, Al
2O
370 heavy %) mix, add 1.46gNH
4F (chemical pure, Beijing company of China Drug Co. sells), the HNO of 1 heavy %
3And deionized water mixed back extruded moulding of pinching on banded extruder, make the catalyzer bar of diameter 1.5mm, then 120 ℃ of dryings 5 hours, 550 ℃ of roasts 3 hours in the Ma Fufu stove again, cool to room temperature, obtaining MCM-22 zeolite content about 40 heavy %, fluorine content is the catalyzer of 1.5 heavy %.
Comparative Examples
Do not add during except moulding the halogen compounds, other preparation process and feeding quantity have obtained the comparative catalyst with embodiment 1, numbering W.
Embodiment 8
Catalyst A provided by the invention, B, C, D, E and the comparative catalyst W contrast effect in benzene and ethene liquid phase alkylation reaction is described.
The CDS-900 of U.S.'s import pressurization little anti--chromatogram arrangement on, be raw material with benzene and ethene, catalyst A, B, C are carried out liquid phase alkylation reaction activity and selective evaluation.Reactor is the stainless steel tube of internal diameter 12.5mm.The loadings of catalyzer is 8mL, and granularity is 16～20 orders, and with the dilution of 16～20 order quartz sands, thinning ratio is 3.Temperature of reaction: 190 ℃, reaction pressure: 3.5MPa, benzene/ethylene molecule be than 12, reaction result table 1.
Table 1
| Catalyzer | ????A | ????B | ????C | ????D | ????E | ????W |
| STY, ethylbenzene g/kgcat.h -1 | ????880 | ????902 | ????890 | ????890 | ????885 | ????820 |
| The STY relative growth rate, % | ????107.32 | ????110.00 | ????108.54 | ????108.54 | ????107.93 | ????100 |
| Ethylbenzene selectivity, % | ????96.39 | ????96.77 | ????96.5 | ????96.48 | ????96.42 | ????93.76 |
| The diethylbenzene selectivity, % | ????3.54 | ????3.18 | ????3.31 | ????3.40 | ????3.48 | ????6.00 |
| The triethyl-benzene selectivity, % | ????0.07 | ????0.05 | ????0.06 | ????0.06 | ????0.06 | ????0.24 |
| The ethylbenzene selectivity relative growth rate, % | ????102.81 | ????103.21 | ????102.92 | ????102.90 | ????102.8 | ????100 |
| The relative decrement of diethylbenzene selectivity, % | ????41.00 | ????47.00 | ????44.8 | ????43.3 | ????42.0 | ????100 |
| The ethylization selectivity, % | ????99.84 | ????99.84 | ????99.83 | ????99.83 | ????99.83 | ????99.79 |
| Content of halogen in the catalyzer, % | Fluorine 0.5 | Fluorine 1.0 | Fluorine 1.0 | Chlorine 1.0 | Chlorine and fluorine totally 1.5 | ????0 |
Claims (5)
1, a kind of catalyzer that contains the MCM-22 zeolite contains the MCM-22 zeolite of 30～90 heavy % and the alumina host of equal amount, it is characterized in that this catalyzer contains the halogen in simple substance 0.1～2.0 heavy %.
2,, contain the halogen of counting 0.5～1.5 heavy % with simple substance according to the catalyzer of claim 1.
3, according to the catalyzer of claim 1 or 2, said halogen is selected from a kind of, two or three the mixture in fluorine, chlorine and the bromine.
4, according to the catalyzer of claim 3, said halogen is fluorine and/or chlorine.
5, according to the catalyzer of claim 1, the SiO of said MCM-22 zeolite
2/ Al
2O
3Be 15～50.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100009572A CN1296133C (en) | 2004-01-19 | 2004-01-19 | Catalyst containing MCM-22 zeolite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100009572A CN1296133C (en) | 2004-01-19 | 2004-01-19 | Catalyst containing MCM-22 zeolite |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1647855A true CN1647855A (en) | 2005-08-03 |
| CN1296133C CN1296133C (en) | 2007-01-24 |
Family
ID=34866952
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100009572A Expired - Lifetime CN1296133C (en) | 2004-01-19 | 2004-01-19 | Catalyst containing MCM-22 zeolite |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1296133C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115857181A (en) * | 2022-10-20 | 2023-03-28 | 中国航天三江集团有限公司 | High-power solid beam and annular beam conversion device |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5334795A (en) * | 1990-06-28 | 1994-08-02 | Mobil Oil Corp. | Production of ethylbenzene |
| CN1041387C (en) * | 1993-06-15 | 1998-12-30 | 中国石油化工总公司 | Beta-zeolite-gamma-alumina catalyst and its preparation |
| US5600048A (en) * | 1994-12-27 | 1997-02-04 | Mobil Oil Corporation | Continuous process for preparing ethylbenzene using liquid phase alkylation and vapor phase transalkylation |
| CN1224673C (en) * | 2000-08-23 | 2005-10-26 | 中国科学院大连化学物理研究所 | Catalyst for modifying gasoline |
| CN1123387C (en) * | 2001-02-28 | 2003-10-08 | 中国科学院大连化学物理研究所 | Zeolite catalyst for preparing alkylbenzene from olefin and benzene and preparing process thereof |
| CN1589967A (en) * | 2003-09-05 | 2005-03-09 | 中国科学院大连化学物理研究所 | Catalyst for production of ethyl benzene using ethylene and benzene and its preparation method and application |
| CN1597110A (en) * | 2003-09-16 | 2005-03-23 | 中国科学院大连化学物理研究所 | Catalyst for producing ethyl benzene from multi ethyl benzene and benzene |
-
2004
- 2004-01-19 CN CNB2004100009572A patent/CN1296133C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115857181A (en) * | 2022-10-20 | 2023-03-28 | 中国航天三江集团有限公司 | High-power solid beam and annular beam conversion device |
| CN115857181B (en) * | 2022-10-20 | 2023-11-17 | 中国航天三江集团有限公司 | High-power solid beam and annular beam conversion device |
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| Publication number | Publication date |
|---|---|
| CN1296133C (en) | 2007-01-24 |
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