EP0262049B1 - Verfahren zur Verbesserung von Dampfspaltungsprodukten - Google Patents
Verfahren zur Verbesserung von Dampfspaltungsprodukten Download PDFInfo
- Publication number
- EP0262049B1 EP0262049B1 EP19870402135 EP87402135A EP0262049B1 EP 0262049 B1 EP0262049 B1 EP 0262049B1 EP 19870402135 EP19870402135 EP 19870402135 EP 87402135 A EP87402135 A EP 87402135A EP 0262049 B1 EP0262049 B1 EP 0262049B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- steam
- zeolite
- cracking
- zsm
- catalyst
- 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.)
- Expired
Links
- 238000004230 steam cracking Methods 0.000 title claims description 38
- 238000000034 method Methods 0.000 title claims description 28
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 31
- 239000010457 zeolite Substances 0.000 claims description 31
- 229910021536 Zeolite Inorganic materials 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 28
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 claims description 22
- 239000000047 product Substances 0.000 claims description 20
- 229930195733 hydrocarbon Natural products 0.000 claims description 16
- 150000002430 hydrocarbons Chemical class 0.000 claims description 16
- 230000003197 catalytic effect Effects 0.000 claims description 12
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 10
- 239000010425 asbestos Substances 0.000 claims description 10
- 229910052593 corundum Inorganic materials 0.000 claims description 10
- 229910052895 riebeckite Inorganic materials 0.000 claims description 10
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 6
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 18
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 9
- 239000005977 Ethylene Substances 0.000 description 9
- 150000001336 alkenes Chemical class 0.000 description 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 230000004048 modification Effects 0.000 description 8
- 238000012986 modification Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 230000001965 increasing effect Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 239000008096 xylene Substances 0.000 description 5
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910044991 metal oxide Inorganic materials 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 150000003738 xylenes Chemical class 0.000 description 4
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 3
- 239000008246 gaseous mixture Substances 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 125000001931 aliphatic group Chemical group 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 239000001307 helium Substances 0.000 description 2
- 229910052734 helium Inorganic materials 0.000 description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- PRAKJMSDJKAYCZ-UHFFFAOYSA-N squalane Chemical compound CC(C)CCCC(C)CCCC(C)CCCCC(C)CCCC(C)CCCC(C)C PRAKJMSDJKAYCZ-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 238000011021 bench scale process Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229920006037 cross link polymer Polymers 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- HQQADJVZYDDRJT-UHFFFAOYSA-N ethene;prop-1-ene Chemical group C=C.CC=C HQQADJVZYDDRJT-UHFFFAOYSA-N 0.000 description 1
- -1 ethylene, propylene, butenes Chemical class 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000005350 fused silica glass Substances 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- JXTPJDDICSTXJX-UHFFFAOYSA-N n-Triacontane Natural products CCCCCCCCCCCCCCCCCCCCCCCCCCCCCC JXTPJDDICSTXJX-UHFFFAOYSA-N 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 229940032094 squalane Drugs 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
- C10G63/02—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only
- C10G63/04—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/06—Catalytic reforming characterised by the catalyst used
- C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
Definitions
- Steam-cracking is one of the most widely used basic petrochemical processes. It is used by industries to produce light olefins such as ethylene, propylene, butenes and butadiene and it is also relied upon for the production of aromatics such as benzene, toluene and xylenes.
- steam-cracking comprises a step in which the hydrocarbon mixture to be transformed is mixed with steam and submitted to elevated temperatures in a tubular reactor.
- the different resulting products, gaseous and liquid hydrocarbons are then collected and separated.
- product distribution depends on the nature of the initial hydrocarbon mixture as well as experimental conditions.
- C2-C4 light olefins as well as benzene, toluene, ethylbenzene and xylenes have the highest commercial values and since enormous quantities are processes throughout the world, even small yield improvements lead to substantial profit increases.
- ZSM-5 zeolite catalysts have drawn considerable attention because of their ability to increase selectivity in a variety of industrial processes such as xylene isomerization, toluene disproportionation, aromatic alkylation, methanol conversion and conversion of synthesis gas to ethane.
- US 4 472 535 discloses a method of converting a synthesis gas mixture comprising hydrogen and carbon monoxide to a hydrocarbon product, with improved selectivity for the production of ethane, which comprises contacting the synthesis gas under conversion conditions with a conversion catalyst comprising a crystalline zeolite component having acidic functionality and a metal component impregnated into the zeolite from a liquid ammonia solution wherein said metal component comprises a metal or metals which are an effective catalyst for the conversion of synthesis gas to methanol.
- modifications of the catalyst can also lead to highly efficient production of light olefins resulting from methanol conversion.
- modified zeolite catalysts have the possibilities to present very interesting properties for enhancing yields in petrochemical reactions.
- the present invention relates to a process for up-grading products resulting from the steam-cracking of hydrocarbons which comprises bringing the steam-cracking reaction products in contact with a multifunctional Zn-ZSM-5 zeolite/Cr2O3/Al2O3 catalyst comprising of a mixture of from 2.5 to 7.5% wt of Cr2O3, 5 to 17.5% wt of Al2O3 and 75 to 85% wt of a Zn-ZSM-5 zeolite or a Zn-ZSM-5 zeolite/asbestos.
- a multifunctional Zn-ZSM-5 zeolite/Cr2O3/Al2O3 catalyst comprising of a mixture of from 2.5 to 7.5% wt of Cr2O3, 5 to 17.5% wt of Al2O3 and 75 to 85% wt of a Zn-ZSM-5 zeolite or a Zn-ZSM-5 zeolite/asbestos.
- the main feature of the present invention resides in the presence of a catalytic reactor at the outlet of the steam-cracking reactor.
- This catalytic reactor contains a multifunctional catalyst which comprises a zeolite of the ZSM-5 type coupled with metallic oxides.
- These oxides can either be coupled to the zeolite by being directly deposited on the zeolite or mechanically mixed with the zeolite.
- the metallic oxides can be selected from oxides such as Cr2O3, Al2O3, or from any metallic oxide having a hydrogenating/dehydrogenating function.
- catalytic reactor used in the present invention was a fixed-bed reactor, it will be understood that any suitable design commonly used for catalytic reactions could have been chosen.
- the starting hydro-carbon material 2 is first mixed with a stripping gas 4. It is to be noted, however, that the use of a stripping gas is optional. In the context of the actual experiments, a stripping gas was used only for convenience.
- the resulting mixture is then forwarded to a vaporizer-mixer 6, in which steam is injected by means of an infusion pump 8.
- the gaseous mixture thus obtained enters a steam-cracking tubular reactor 10 heated at a temperature ranging between 760° and 860°C.
- products coming out of the steam-cracking tubular reactor 10 are sent into a catalytic reactor 12 heated at a temperature ranging between 450° and 550°C.
- the resulting products are then cooled by a series of condensers 14 (water-cooling condensers and ice bath).
- the liquid and gaseous phases are separated.
- the liquids are first collected in a liquid-collector cylinder 16 while the gases flow through the liquid-collector cylinder to be collected for on line analysis in a dynamic sampler cylinder 18 located at a higher position than the liquid collector cylinder.
- Propane is the starting hydrocarbon material on which the steam-cracking process was performed. It was introduced into the system at a flow rate of 45 ml/min. or 4.95 g/hour. It was first mixed with helium acting as a stripping gas. After having been flown through the vaporizer-mixer, in which steam was injected at a rate of 1.7 g/hour, the gaseous mixture was then sent into the steam-cracking reactor whose internal temperature had been set to 780°C at atmospheric pressure. The residence time of the starting material in the steam-cracking reactor was approximately 1 second.
- the resulting product was then separated into its liquid and the gaseous phases.
- the liquid fraction was analyzed by GC using a capillary column (length: 50 m, PONA® type, fused silica coated with a cross-linked polymer).
- the gases were analyzed on line by gas chromatography.
- a column having a length of 3.5 m packed with Chromosorb® P coated with 20% by weight of Squalane® was used for the analysis.
- the GC used was a dual FID Hewlett-Packard Model 5790 equipped with a 3392A Model integrator. Results are shown in Table 1.
- Example 1 The same procedure as in Example 1 was repeated the only modification being the internal temperature of the steam-cracking reactor which was set at 800°C. Results are shown in Table 1.
- Example 5 The same procedure as in Example 1 was repeated the only modification being the internal temperature of the steam-cracking reactor which was set at 835°C. Results are shown in Table 5.
- propane was chosen as the starting hydrocarbon material. It was mixed with helium and flown through the vaporizer-mixer. The gaseous mixture was then forwarded through the steam-cracking reactor whose internal temperature had been set to 780°C. The resulting products were then sent to the catalytic reactor which had been previously embedded with 4 g of a Zn-Mn-ZSM-5 zeolite which was prepared according to the procedure described in Can. Pat. Appl. S.N. 471,463 (US-A-4 615 995). The temperature of the catalytic reactor had been previously set at 500°C, with a pressure of 1 atmosphere and a W.H.S.V. (weight hourly space velocity) of 1 h ⁇ 1. The final products were analyzed using the techniques discussed in Example 1. Results are shown in Table 2.
- Example 2 The same procedure as in Example 4 was repeated, the only modification being the internal temperature of the steam-cracking reactor which was set at 800°C. Results are shown in Table 2.
- Example 4 The same procedure as in Example 4 was repeated, except for the following modifications: the catalytic reactor was embedded with 4 g of a Zn-Mn-ZSM-5 zeolite/asbestos catalyst prepared according to the procedure described in Can. Pat. Appl. S.N. 471,463 (US-A- 4 615 995). Results are shown in Table 3.
- Example 6 The same procedure as in Example 6 was repeated, the only modification being the internal temperature of the steam-cracking reactor which was set at 800°C. Results are shown in Table 3.
- Example 4 The same procedure as in Example 4 was repeated, except for the following modification: the catalytic reactor was embedded with a Zn-ZSM-5 zeolite/ asbestos/Cr2O3/Al2O3 catalyst.
- the Zn-ZSM-5 zeolite/ asbestos catalyst was prepared according to the method described in Can. Pat. Appl. S.N. 471,463. Then, 4.5 g of the Zn-ZSM-5 zeolite/asbestos catalyst obtained were wet with a solution prepared from 0.3 g of Cr2O3 and 0.4 g of sodium aluminate dissolved in 5 ml of distilled water. The resulting multifunctional catalyst was dried at 120°C for 12 hours and actuated at 500°C for another 12 hour period. Finally, the catalyst was reduced in hydrogen at 350°C for at least 1 hour. Results are shown in Table 4.
- Example 8 The same procedure as in Example 8 was repeated, the only modification being the internal temperature of the steam-cracking reactor which was set at 800°C. Results were shown in Table 4.
- Example 3 a run without catalyst was performed at 835°C. This temperature was fairly close to temperatures used in industrial steam-cracking facilities using propane as a starting hydrocarbon material.
- the product distribution of such a run is compared to the run performed in presence of the Zn-ZSM-5 zeolite/asbestos/Cr2O3/Al2O3 catalyst and with the steam-cracking reactor temperature set at 800°C, as described in Example 9, it can be seen, as it is shown in Table 5, that in the presence of the multifunctional catalyst and with a much lower steam-cracking temperature, higher yields in ethylene and propylene were obtained.
- the propylene yield was nearly doubled (due mainly to a lower steam-cracking temperature) and the ethylene yield was increased by 5 wt percentage points while methane formation was significantly lower.
- the liquid yield was much lower for the run performed at a lower steam-cracking temperature in the presence of the multifunctional catalyst.
- the BTX aromatics benzene, toluene, ethylbenzene and xylenes
- the total "ethylene + propylene" yield can be increased by 10 wt percentage points and the ethylene/propylene wt ratio can be decreased to a very large extent (see Table 5).
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Claims (5)
- Verfahren zur Vesserung von Produkten, die aus dem Wasserdampfkracken von Kohlenwasserstoffen stammen, indem man die Wasserdampfkrackreaktionsprodukte in Berührung mit einem Katalysator bringt, der ein Gemisch von 2,5 bis 7,5 Gew.-% Cr₂O₃, 5 bis 17 Gew.-% Al₂O₃ und 75 bis 85 Gew.-% Zn-ZSM-5-Zeolith oder Zn-ZSM-5-Zeolith/Asbest umfaßt, und die erwünschten Produkte gewinnt.
- Verfahren nach Anspruch 1, bei dem Cr₂O₃ und Al₂O₃ direkt auf dem Zn-ZSM-5-Zeolith oder Zn-ZSM-5-Zeolith/Asbest abgelagert werden.
- Verfahren nach Anspruch 1, bei dem Cr₂O₃ und Al₂O₃ mechanisch mit dem Zn-ZSM-5-Zeolith oder dem Zn-ZSM-5-Zeolith/Asbest vermischt werden.
- Verfahren nach Anspruch 1, bei dem der Katalysator in einen Röhrenreaktor gepackt wird.
- Verfahren nach Anspruch 4, bei dem die Temperatur des katalytischen Röhrenreaktors zwischen 400 und 600°C gehalten wird.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA000519081A CA1270240A (en) | 1986-09-25 | 1986-09-25 | Process for up-grading steam-cracking products |
CA519081 | 1986-09-25 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0262049A2 EP0262049A2 (de) | 1988-03-30 |
EP0262049A3 EP0262049A3 (en) | 1989-03-22 |
EP0262049B1 true EP0262049B1 (de) | 1992-03-11 |
Family
ID=4134019
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19870402135 Expired EP0262049B1 (de) | 1986-09-25 | 1987-09-24 | Verfahren zur Verbesserung von Dampfspaltungsprodukten |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0262049B1 (de) |
JP (1) | JPS6397233A (de) |
CA (1) | CA1270240A (de) |
DE (1) | DE3777305D1 (de) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3867245D1 (de) * | 1987-01-23 | 1992-02-13 | Mobil Oil Corp | Verbesserung von diolefine enthaltenden kohlenwasserstoffen. |
ATE118525T1 (de) * | 1989-09-26 | 1995-03-15 | Shell Int Research | Verfahren zur verbesserung eines schwefel enthaltenden einsatzmaterials. |
GB9218346D0 (en) * | 1992-08-28 | 1992-10-14 | Bp Chem Int Ltd | Process |
US6033555A (en) * | 1997-06-10 | 2000-03-07 | Exxon Chemical Patents Inc. | Sequential catalytic and thermal cracking for enhanced ethylene yield |
EP1307525B1 (de) * | 2000-07-31 | 2007-10-24 | Concordia University | Katalysator für das kräcken von kohlenwasserstoffeinsätzen zur erzeugung von leichtolefinen und herstellung der katalysatoren |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4097367A (en) * | 1977-07-25 | 1978-06-27 | Mobil Oil Corporation | Conversion of olefinic naphtha |
US4188336A (en) * | 1977-08-18 | 1980-02-12 | Mobil Oil Corporation | Conversion of synthesis gas to aromatic hydrocarbons |
US4472535A (en) * | 1982-11-22 | 1984-09-18 | Mobil Oil Corporation | Conversion of synthesis gas to ethane |
DE3473611D1 (en) * | 1983-07-14 | 1988-09-29 | Shell Int Research | Process for upgrading a gasoline |
US4615995A (en) * | 1985-01-03 | 1986-10-07 | The Asbestos Institute | Zeolite catalysts |
-
1986
- 1986-09-25 CA CA000519081A patent/CA1270240A/en not_active Expired - Fee Related
-
1987
- 1987-09-24 DE DE8787402135T patent/DE3777305D1/de not_active Expired - Fee Related
- 1987-09-24 JP JP23990287A patent/JPS6397233A/ja active Pending
- 1987-09-24 EP EP19870402135 patent/EP0262049B1/de not_active Expired
Also Published As
Publication number | Publication date |
---|---|
EP0262049A2 (de) | 1988-03-30 |
DE3777305D1 (de) | 1992-04-16 |
JPS6397233A (ja) | 1988-04-27 |
CA1270240A (en) | 1990-06-12 |
EP0262049A3 (en) | 1989-03-22 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CA1156265A (en) | Process for carrying out catalytic conversions | |
US4062905A (en) | Manufacture of light olefins | |
Schulz et al. | Conversion of ethanol over zeolite H‐ZSM‐5 | |
JP4432019B2 (ja) | 炭化水素原料から芳香族炭化水素化合物及び液化石油ガスを製造する方法 | |
KR100881042B1 (ko) | 에틸렌 및 프로필렌 제조 방법 | |
US6916448B2 (en) | Process for selective production of propylene from hydrocarbon fractions with four carbon atoms | |
US4732881A (en) | Catalysts for up-grading steam-cracking products | |
US4899015A (en) | Process for olefins to gasoline conversion | |
JP2010241826A (ja) | オレフィンの製造 | |
JPH11246870A (ja) | オレフイン類の製造 | |
EP0332243B1 (de) | Verfahren zur Herstellung von normalerweise flüssigen Kohlenwasserstoffen aus einer Kohlenwasserstoffcharge, die geradkettige und verzweigte Olefine enthält | |
GB2164054A (en) | Liquid hydrocarbon synthesis using supported ruthenium catalysts | |
US4906800A (en) | Procedure for imparting selectivity to hydrogenation catalysts and method for using the same | |
US4140621A (en) | Maintaining or increasing the isobutane content of a cut subjected to selective hydrogenolysis | |
US20070246400A1 (en) | Zeolite Catalysts | |
JPH0639416B2 (ja) | 2−メチル−1−ブテンと少なくとも1つのn−ペンテンとを含むC▲下5▼オレフイン留分からの2−メチル−2−ブテンの製造方法 | |
JPS58203920A (ja) | 2価銅含有zsm‐5型触媒を使用する炭化水素の転化方法 | |
Varma et al. | Performance of dual-reactor system for conversion of syngas to aromatic-containing hydrocarbons | |
EP0262049B1 (de) | Verfahren zur Verbesserung von Dampfspaltungsprodukten | |
NZ202810A (en) | Converting fossil fuel successively to synthesis gas,oxygenates and hydrocarbons,then upgrading | |
CA1250318A (en) | Natural gas conversion | |
CA1175446A (en) | Conversions of alcohols and ethers and feedstreams containing the same to benzene, toluene and xylene | |
US4774376A (en) | Production of liquid products from aliphatic hydrocarbons | |
GB2061999A (en) | Catalyst for the production of hydrocarbons | |
Egiebor et al. | The polyfunctionality of iron catalysts during carbon monoxide hydrogenation: II. The formation of secondary products by α-olefin isomerization |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
AK | Designated contracting states |
Kind code of ref document: A2 Designated state(s): DE FR GB IT NL |
|
PUAL | Search report despatched |
Free format text: ORIGINAL CODE: 0009013 |
|
AK | Designated contracting states |
Kind code of ref document: A3 Designated state(s): DE FR GB IT NL |
|
17P | Request for examination filed |
Effective date: 19890918 |
|
17Q | First examination report despatched |
Effective date: 19900905 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): DE FR GB IT NL |
|
REF | Corresponds to: |
Ref document number: 3777305 Country of ref document: DE Date of ref document: 19920416 |
|
ITF | It: translation for a ep patent filed | ||
ET | Fr: translation filed | ||
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Effective date: 19920924 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed | ||
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Effective date: 19930401 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee | ||
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 19920924 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Effective date: 19930528 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Effective date: 19930602 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED. Effective date: 20050924 |