US2831907A - Production of styrene and related compounds - Google Patents
Production of styrene and related compounds Download PDFInfo
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- US2831907A US2831907A US627170A US62717056A US2831907A US 2831907 A US2831907 A US 2831907A US 627170 A US627170 A US 627170A US 62717056 A US62717056 A US 62717056A US 2831907 A US2831907 A US 2831907A
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- steam
- temperature
- ethylbenzene
- mixture
- styrene
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- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 title description 42
- 150000001875 compounds Chemical class 0.000 title description 5
- 238000004519 manufacturing process Methods 0.000 title description 5
- 239000000203 mixture Substances 0.000 claims description 30
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 21
- 239000003054 catalyst Substances 0.000 claims description 15
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- 239000011874 heated mixture Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 238000004326 stimulated echo acquisition mode for imaging Methods 0.000 claims description 3
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 74
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 9
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 4
- KVNYFPKFSJIPBJ-UHFFFAOYSA-N 1,2-diethylbenzene Chemical compound CCC1=CC=CC=C1CC KVNYFPKFSJIPBJ-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000956 alloy Substances 0.000 description 3
- 229910045601 alloy Inorganic materials 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 description 2
- ZMXIYERNXPIYFR-UHFFFAOYSA-N 1-ethylnaphthalene Chemical compound C1=CC=C2C(CC)=CC=CC2=C1 ZMXIYERNXPIYFR-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- RJTJVVYSTUQWNI-UHFFFAOYSA-N beta-ethyl naphthalene Natural products C1=CC=CC2=CC(CC)=CC=C21 RJTJVVYSTUQWNI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910001950 potassium oxide Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- MNNZINNZIQVULG-UHFFFAOYSA-N 2-chloroethylbenzene Chemical compound ClCCC1=CC=CC=C1 MNNZINNZIQVULG-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- MJEMIOXXNCZZFK-UHFFFAOYSA-N ethylone Chemical compound CCNC(C)C(=O)C1=CC=C2OCOC2=C1 MJEMIOXXNCZZFK-UHFFFAOYSA-N 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 150000003440 styrenes Chemical class 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/321—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
- C07C5/3332—Catalytic processes with metal oxides or metal sulfides
Definitions
- This invention relates to an improved method of making styrene and related compounds by dehydrogenation of alkylatedaromatic hydrocarbons.
- styrene can be produced by rapidly passing a mixture of ethylbenzene and steam over a bed of a suitable catalyst at elevated temperature.
- the temperature at which the ethylbenzene is dehydrogenated e., the temperature at which the ethylbenzene is dehydrogenated; -(2) to simultaneously and separately heat the ethylbenzene to a temperature below the reaction temperature; (3) thereafter to admix the steam and ethylbenzene in the correct proportions to yield the correct reaction temperature; (4) and then to pass the mixture to a catalyst-containing reactor wherein the ethyl- One dissteam, upon being admixed with the ethylbenzene, causes portions of the latter to be brought up almost to the temperature of the steam before mixing, and since the steam is at or above the temperature at which the ethylbenzene begins to pyrolyze, some of the ethylbenzene is destroyed by thermal cracking to produce undesired materials such as benzene, toluene, carbon monoxide, carbon dioxide, tar, carbon, and the like, instead of styrene,
- a second important disadvantage is that high cost alloy equipment is required due to the fact that the steam is superheated to a relatively high temperature, e. g., usually in the range of 670 to 850 C. If the steam were kept at a lower temperature, it would be possible to utilize lower cost alloy equipment.
- Another object of this invention is to provide a method of dehydrogenating ethylbenzene or other alkylated aromatic hydrocarbons in admixture with steam, wherein the temperature of the steam prior to admixture with the ethylbenzene or its related compounds is maintained at a temperature below the reaction temperature, thereby permitting the method to be carried out in lower cost alloy equipment.
- Reactor Volume 15 105 89. 5 B9. 1 Lbs. Steam/lb. Ethylbenzenm 1.5-20 2. 5 2. 6 Reactor Inlet Temperature, 540-650 607 610 Reactor Inlet Pressure, p. s. i. g 1-15 6 7 Weight Percent Styrene in Product 2060 41. 3 39. 5 Weight Percent Styrene in Feed 012 5. 7 4.0 Yield, mols Stryene/mol Ethylbenzene destroyed -95 92.0 94. 1
- the process is normally continuous with the ethylbenzene and steam being constantly passed through the system.
- the mixture passing out of the reactor is rapidly cooled to condense the styrene product and any unreacted ethylbenzene.
- the cooling may be brought about in a number of ways. Preferably this is accomplished by passing it through a heat exchanger adapted to transfer the heat removed from the reacted mixture to incoming ethylbenzene vapors and steam according to conventional heat exchange practice. Residual gases and water are first separated from the condensate and then the styrene is removed according to conventional practice. Preferably this is accomplished by fractionally distilling the mixture. The styrene and unreacted ethylbenzene are recovered as individual compounds and the unreacted ethylbenzene may be reintroduced into thesystem to produce additional styrene.
- a mixture comprising 1.0 lb. of ethylbenzene and 0.67 pound of steam was passed in a steady flow through an ethylbenzene vaporizer A and a first heat exchanger B in succession. Also passing through the same first heat exchanger so as to impart heat to the vaporized ethylbenzene-steam mixture was the reacted mixture from the catalyst containing reactor C. The ethylbenzene-steam mixture passed out of the heat exchanger B at a temperature of about 420 C. Simultaneously 2.1 lbs. of steam were passed in steady flow through a second heat exchanger D and heated therein by the reacted mixture passing out from the first heat exchanger.
- This steam was then mixed with the ethylbenzene-steam mixture from the first heat exchanger, and the combined mixture was passed through a furnace E which caused it to be heated to a temperature of about 614 C.
- the combined mixture at a temperature of 614 C. was then passed rapidly through the reactor shell C which contained a ferrous oxide-potassium oxide catalyst.
- the total actual residence "time for the combined mixture in the reactor was about 0.1 second.
- the reacted mixture had a temperature of about 546 C. as it left the reactor.
- the reacted mixture was cool-ed by passing it through the first and second heat exchangers in turn, thereby heating the incoming ethylbenzene and steam, as previously described.
- the temperature of the reacted mixture as it passed out of the first heat ex- It has been determined that the present method can be operated with as little as 1.5 pounds of steam and as high as 20 pounds of steam or even more per pound of ethylbenzene. However, for practical reasons such as economy of operation, the preferred range is from two to three pounds of steam per pound of ethylbenzene.
- the necessary heat of reaction is applied to the ethylbenzene steam mixture by passing the mixture through a furnace.
- the temperature re quired for converting the ethylbenzene to styrene is lower when a catalyst is used than when no catalyst is used.
- the ethylbenzene-steam mixture is subjected to little or no thermal cracking or pyrolysis prior to being intro Jerusalem into the reactor. Conversion of the ethylbenzene to styrene takes place when the mixture is passed over the catalyst.
- the method of dehydrogenating an alkylated aromatic hydrocarbon containing at least two carbon atoms in a side chain which comprises mixing said hydrocarbon with steam, said hydrocarbon and steam each being at a temperature lower than dehydrogenation temperature prior to mixing, heating the mixture to a temperature within the range required for dehydrogenation, and contacting said heated mixture while at dehydrogenation temperature with a dehydrogenation catalyst.
- the method which comprises dehydrogenating an alkylated aromatic hydrocarbon containing at least two A carbon atoms in a side chain, by mixing the same with steam having a temperature below dehydrogenation temperature, heating the mixture to a temperature within the range required for dehydrogenation, and contacting said heated mixture with a dehydrogenation catalyst.
- the method of producing styrene by dehydrogenation of ethylbenzene which comprises the steps of mixing ethylbenzene having a temperature below dehydrogenation temperature with steam which has been superheated insufiiciently to supply the heat required for dehydrogenation, heating the ethylbenzene steam mixture to a temperature at which rapid dehydrogenation will occur, and contacting said heated mixture while at a dehydrogenation temperature with a dehydrogenation catalyst.
- the method of producing substantially water white and tar free styrene by dehydrogenation of ethylbenzene which comprises mixing ethylbenzene and steam at a temperature below 500 C., heating the resulting mixture to a temperature within the dehydrogenation range of from 500 to 700 C. and contacting said heated mixture while in said temperature range for a fraction of a second with a dehydrogenation catalyst.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
April 22, 1958 F. D. MAYFIELD ETAL 2,831,907v
PRODUCTION OF STYRENE AND RELATED COMPOUNDS I Filed Dec. 10, 1956 KE C 5 REACTION m qfb PRODUCT} STEAM A 2.| LBS.
STEAM- 0.s7 LBS.
ETHYLBENZENE |.o LBS.
INVENTORS' FRANKLIN D. MAYFIELD JAIX ES CLIFFORD SHAW ATTORNEYS benzene is dehydrogenated to form styrene.
advantage of this procedure is that the extremely hot.
United States Patent PRODUCTION OF STYRENE AND RELATED COMPOUNDS Franklin D. Mayfield, Baton Rouge, La., and James Clifford Shaw, Dallas, Tex.
Application December 10, 1956, Serial No. 627,170 11 Claims. (Cl. 260669) This invention relates to an improved method of making styrene and related compounds by dehydrogenation of alkylatedaromatic hydrocarbons.
It is well known that styrene can be produced by rapidly passing a mixture of ethylbenzene and steam over a bed of a suitable catalyst at elevated temperature. Heretofore, however, it has been practice (1) to superheat the steam to a temperature above the reaction temperature, i. e., the temperature at which the ethylbenzene is dehydrogenated; -(2) to simultaneously and separately heat the ethylbenzene to a temperature below the reaction temperature; (3) thereafter to admix the steam and ethylbenzene in the correct proportions to yield the correct reaction temperature; (4) and then to pass the mixture to a catalyst-containing reactor wherein the ethyl- One dissteam, upon being admixed with the ethylbenzene, causes portions of the latter to be brought up almost to the temperature of the steam before mixing, and since the steam is at or above the temperature at which the ethylbenzene begins to pyrolyze, some of the ethylbenzene is destroyed by thermal cracking to produce undesired materials such as benzene, toluene, carbon monoxide, carbon dioxide, tar, carbon, and the like, instead of styrene, thus lowering the yield of styrene. A second important disadvantage is that high cost alloy equipment is required due to the fact that the steam is superheated to a relatively high temperature, e. g., usually in the range of 670 to 850 C. If the steam were kept at a lower temperature, it would be possible to utilize lower cost alloy equipment.
Accordingly, it is an object of the present invention to provide a method whereby ethylbenzene or other alkylated aromatic hydrocarbons may be dehydrogenated to produce styrene or homologues or analogues thereof, without appreciable side reaction production of carbon, tar, benzene, etc.
Another object of this invention is to provide a method of dehydrogenating ethylbenzene or other alkylated aromatic hydrocarbons in admixture with steam, wherein the temperature of the steam prior to admixture with the ethylbenzene or its related compounds is maintained at a temperature below the reaction temperature, thereby permitting the method to be carried out in lower cost alloy equipment.
Other objects and many of the attendant advantages of this invention will be readily appreciated as the same becomes better understood by reference to the following detailed description together with the accompanying drawing which is a How sheet schematically illustrating how styrene is produced.
The essential steps of the present invention, as applied, for example, to the production of styrene from ethylbenzene, are:
(1) Mixing ethylbenzene vapor with steam in accordance with a predetermined ratio at any suitable temperature,
2,831,907 Patented Apr. 22, 1958 the ethylbenzene with steam. This steam-ethylbenzene mixture is superheated to a temperature which is often around 610 C., after which the mixture is then passed through a catalyst containing reactor where the contact then is as indicated in the test data given below:
Range Test Test Run A Run B Ethylbenzene Flow (Lbs/hr. per cu.
ft. of Reactor Volume) 7-50 35. 4 26.6 Steam Flow (Lbs/hr. per cu. ft. of
Reactor Volume) 15 105 89. 5 B9. 1 Lbs. Steam/lb. Ethylbenzenm 1.5-20 2. 5 2. 6 Reactor Inlet Temperature, 540-650 607 610 Reactor Inlet Pressure, p. s. i. g 1-15 6 7 Weight Percent Styrene in Product 2060 41. 3 39. 5 Weight Percent Styrene in Feed 012 5. 7 4.0 Yield, mols Stryene/mol Ethylbenzene destroyed -95 92.0 94. 1
The process is normally continuous with the ethylbenzene and steam being constantly passed through the system.
The mixture passing out of the reactor is rapidly cooled to condense the styrene product and any unreacted ethylbenzene. The cooling may be brought about in a number of ways. Preferably this is accomplished by passing it through a heat exchanger adapted to transfer the heat removed from the reacted mixture to incoming ethylbenzene vapors and steam according to conventional heat exchange practice. Residual gases and water are first separated from the condensate and then the styrene is removed according to conventional practice. Preferably this is accomplished by fractionally distilling the mixture. The styrene and unreacted ethylbenzene are recovered as individual compounds and the unreacted ethylbenzene may be reintroduced into thesystem to produce additional styrene.
The following example is illustrative only of the present invention and, therefore, is not to be construed as limiting the invention.
Referring to the accompanying flow sheet, a mixture comprising 1.0 lb. of ethylbenzene and 0.67 pound of steam was passed in a steady flow through an ethylbenzene vaporizer A and a first heat exchanger B in succession. Also passing through the same first heat exchanger so as to impart heat to the vaporized ethylbenzene-steam mixture was the reacted mixture from the catalyst containing reactor C. The ethylbenzene-steam mixture passed out of the heat exchanger B at a temperature of about 420 C. Simultaneously 2.1 lbs. of steam were passed in steady flow through a second heat exchanger D and heated therein by the reacted mixture passing out from the first heat exchanger. The steam passed out of the second heat exchanger D at a temperature of about 335 C. This steam was then mixed with the ethylbenzene-steam mixture from the first heat exchanger, and the combined mixture was passed through a furnace E which caused it to be heated to a temperature of about 614 C. The combined mixture at a temperature of 614 C. was then passed rapidly through the reactor shell C which contained a ferrous oxide-potassium oxide catalyst. The total actual residence "time for the combined mixture in the reactor was about 0.1 second.
aesneor 3 The reacted mixture had a temperature of about 546 C. as it left the reactor. The reacted mixture was cool-ed by passing it through the first and second heat exchangers in turn, thereby heating the incoming ethylbenzene and steam, as previously described. The temperature of the reacted mixture as it passed out of the first heat ex- It has been determined that the present method can be operated with as little as 1.5 pounds of steam and as high as 20 pounds of steam or even more per pound of ethylbenzene. However, for practical reasons such as economy of operation, the preferred range is from two to three pounds of steam per pound of ethylbenzene.
As is to be expected, by similar procedure it is pos sible to dehydrogenate other alkylated aromatic hydrocarbons containing at least two carbon atoms in a side chain. Thus, for example, diethyl-benzen'e, isopropylbenzene, ethyl toluene, ethyl naphthalene, and ethylchlorobenzene, may be dehydrogenated to produce homologues or analogues of styrene. The procedure of the present invention may be executed at atmospheric pressures or at higher pressures, e. g. 40 pounds per square inch. In place of the ferrous oxide-potassium oxide, other well known catalysts may be utilized, e. g. catalysts of the type described in the patent to Hermann Mark et al., No. 2,110,833, issued March 8, 1938.
As stated hereinabove the necessary heat of reaction is applied to the ethylbenzene steam mixture by passing the mixture through a furnace. The temperature re quired for converting the ethylbenzene to styrene is lower when a catalyst is used than when no catalyst is used. At the temperature utilized in the present method, the ethylbenzene-steam mixture is subjected to little or no thermal cracking or pyrolysis prior to being intro duced into the reactor. Conversion of the ethylbenzene to styrene takes place when the mixture is passed over the catalyst. At the same time, since the ethylbenzene is already admixed with the steam, when it is heated to the required reaction temperature, it is subject to little or no local heating as is the case when the ethylbenzene is mixed with steam above the required reaction temperature. For this reason there is a higher yield of the desired product, styrene, and the quantity of undesired materials, such as tar, produced by thermal cracking is reduced to a quantity that prevents rapid fouling of the system.
Obviously many modifications and variations of the present invention are possible in the light of the above teachings. Therefore, it is to be understood that the invention is not limited in its application to the details specifically described or illustrated, and that within the scope of the appended claims it may be practiced otherwise than as specifically described or illustrated.
We claim:
1. The method of dehydrogenating an alkylated aromatic hydrocarbon containing at least two carbon atoms in a side chain which comprises mixing said hydrocarbon with steam, said hydrocarbon and steam each being at a temperature lower than dehydrogenation temperature prior to mixing, heating the mixture to a temperature within the range required for dehydrogenation, and contacting said heated mixture while at dehydrogenation temperature with a dehydrogenation catalyst.
2. The method of claim 1 wherein the alkylated aromatic hydrocarbon and steam are mixed at a temperature below 500 C. and said mixture is subsequently heated to a dehydrogenation temperature in the range of from 500 to 700 C.
3. The method of claim 1, wherein said hydrocarbon is ethylbenzene.
4. The method of claim 1 wherein the alkylated aromatic hydrocarbon is isopropyl-benzene.
5. The method of claim 1 wherein the alkylated aromatic hydrocarbon is Y diethyl-benzene.
6. The method of claim 1 wherein the alkylated aromatic hydrocarbon is ethyl toluene.
7. The method of claim 1 wherein the alkylated aromatic hydrocarbon is ethyl naphthalene.
8. The method which comprises dehydrogenating an alkylated aromatic hydrocarbon containing at least two A carbon atoms in a side chain, by mixing the same with steam having a temperature below dehydrogenation temperature, heating the mixture to a temperature within the range required for dehydrogenation, and contacting said heated mixture with a dehydrogenation catalyst.
9. The method of producing styrene by dehydrogenation of ethylbenzene which comprises the steps of mixing ethylbenzene having a temperature below dehydrogenation temperature with steam which has been superheated insufiiciently to supply the heat required for dehydrogenation, heating the ethylbenzene steam mixture to a temperature at which rapid dehydrogenation will occur, and contacting said heated mixture while at a dehydrogenation temperature with a dehydrogenation catalyst.
10. The method of claim 9, wherein said mixture is heated to a temperature of approximately'610" C.
11. The method of producing substantially water white and tar free styrene by dehydrogenation of ethylbenzene which comprises mixing ethylbenzene and steam at a temperature below 500 C., heating the resulting mixture to a temperature within the dehydrogenation range of from 500 to 700 C. and contacting said heated mixture while in said temperature range for a fraction of a second with a dehydrogenation catalyst.
References Cited in the file of this patent UNITED STATES PATENTS 2,683,180 Amos et al July 6, 1954 2,813,089 Twaddle et al. Nov. 12, 1957 2,813,137 Twaddle et a1. NOV. 12, 1957 FOREIGN PATENTS 635,827 Great Britain Apr. 19, 1950
Claims (1)
1. THE METHOD OF DEHYDROGENATING AN ALKYLATED AROMATIC HYDROCARBON CONTAINING AT LEAST TWO CARBON ATOMS IN A SIDE CHAIN WHICH COMPRISES MIXING SAID HYDROCARBON WITH STEAM, SAID HYDROCARBON AND STEAM EACH BEING AT A TEMPERATURE LOWER THAN DEHYDROGENATION TEMPERATURE PRIOR TO MIXING HEATING THE MIXTURE TO A TEMPERATURE WITHIN THE RANGE REQUIRED FOR DEHYDROGENATION, AND CONTACTING SAID HEATED MIXTURE WHILE AT DEHYDROGENATION TEMPERATURE WITH A DEHYDROGENATION CATALYST.
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US627170A US2831907A (en) | 1956-12-10 | 1956-12-10 | Production of styrene and related compounds |
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US627170A US2831907A (en) | 1956-12-10 | 1956-12-10 | Production of styrene and related compounds |
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Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3326996A (en) * | 1964-05-06 | 1967-06-20 | Union Carbide Corp | Dehydrogenation of ethylbenzene to styrene |
US3402212A (en) * | 1966-07-18 | 1968-09-17 | Universal Oil Prod Co | Dehydrogenation of ethylbenzene to styrene |
US3409689A (en) * | 1966-05-23 | 1968-11-05 | Universal Oil Prod Co | Dehydrogenation process |
US3437703A (en) * | 1966-05-05 | 1969-04-08 | Foster Grant Co Inc | Catalytic dehydrogenation process and compositions |
US3499051A (en) * | 1967-08-03 | 1970-03-03 | Idemitsu Petrochemical Co | Method for the catalytic dehydrogenation of alkylated aromatic hydrocarbons |
US3542889A (en) * | 1968-05-09 | 1970-11-24 | Universal Oil Prod Co | Method for converting ethylbenzene to styrene |
JPS501007B1 (en) * | 1969-04-03 | 1975-01-14 | ||
US4174353A (en) * | 1978-06-27 | 1979-11-13 | Union Carbide Corporation | Olefin separation process |
US4461751A (en) * | 1979-05-22 | 1984-07-24 | Lummus Crest Inc. | Processes for carrying out catalytic endothermic high-pressure gas reactions |
US4479025A (en) * | 1982-11-22 | 1984-10-23 | Uop Inc. | Alkylaromatic hydrocarbon dehydrogenation process |
US4695664A (en) * | 1986-04-17 | 1987-09-22 | The Badger Company, Inc. | Method of recovering heat from low temperature effluent |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB635827A (en) * | 1946-04-12 | 1950-04-19 | Koppers Co Inc | Dehydrogenation of alkyl aromatic compounds |
US2683180A (en) * | 1952-02-28 | 1954-07-06 | Dow Chemical Co | Method for production of ar-methylstyrene |
US2813089A (en) * | 1955-07-21 | 1957-11-12 | Standard Oil Co | Direct production of polystyrene from petroleum by-product ethylbenzene |
US2813137A (en) * | 1955-07-21 | 1957-11-12 | Standard Oil Co | Selective dehydrogenation of ethylbenzene from xylene solution for direct productionof polystyrene |
-
1956
- 1956-12-10 US US627170A patent/US2831907A/en not_active Expired - Lifetime
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB635827A (en) * | 1946-04-12 | 1950-04-19 | Koppers Co Inc | Dehydrogenation of alkyl aromatic compounds |
US2683180A (en) * | 1952-02-28 | 1954-07-06 | Dow Chemical Co | Method for production of ar-methylstyrene |
US2813089A (en) * | 1955-07-21 | 1957-11-12 | Standard Oil Co | Direct production of polystyrene from petroleum by-product ethylbenzene |
US2813137A (en) * | 1955-07-21 | 1957-11-12 | Standard Oil Co | Selective dehydrogenation of ethylbenzene from xylene solution for direct productionof polystyrene |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3326996A (en) * | 1964-05-06 | 1967-06-20 | Union Carbide Corp | Dehydrogenation of ethylbenzene to styrene |
US3437703A (en) * | 1966-05-05 | 1969-04-08 | Foster Grant Co Inc | Catalytic dehydrogenation process and compositions |
US3409689A (en) * | 1966-05-23 | 1968-11-05 | Universal Oil Prod Co | Dehydrogenation process |
US3402212A (en) * | 1966-07-18 | 1968-09-17 | Universal Oil Prod Co | Dehydrogenation of ethylbenzene to styrene |
US3499051A (en) * | 1967-08-03 | 1970-03-03 | Idemitsu Petrochemical Co | Method for the catalytic dehydrogenation of alkylated aromatic hydrocarbons |
US3542889A (en) * | 1968-05-09 | 1970-11-24 | Universal Oil Prod Co | Method for converting ethylbenzene to styrene |
JPS501007B1 (en) * | 1969-04-03 | 1975-01-14 | ||
US4174353A (en) * | 1978-06-27 | 1979-11-13 | Union Carbide Corporation | Olefin separation process |
US4461751A (en) * | 1979-05-22 | 1984-07-24 | Lummus Crest Inc. | Processes for carrying out catalytic endothermic high-pressure gas reactions |
US4479025A (en) * | 1982-11-22 | 1984-10-23 | Uop Inc. | Alkylaromatic hydrocarbon dehydrogenation process |
US4695664A (en) * | 1986-04-17 | 1987-09-22 | The Badger Company, Inc. | Method of recovering heat from low temperature effluent |
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