WO2012047274A2 - Production of a high octane alkylate from ethylene and isobutane - Google Patents

Production of a high octane alkylate from ethylene and isobutane Download PDF

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Publication number
WO2012047274A2
WO2012047274A2 PCT/US2011/001682 US2011001682W WO2012047274A2 WO 2012047274 A2 WO2012047274 A2 WO 2012047274A2 US 2011001682 W US2011001682 W US 2011001682W WO 2012047274 A2 WO2012047274 A2 WO 2012047274A2
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Prior art keywords
catalytic material
ethylene
isobutane
catalyst
catalytic
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PCT/US2011/001682
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French (fr)
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WO2012047274A3 (en
Inventor
Mitrajit Mukherjee
John F. Young
James P. Nehlsen
George D. Suciu
Kelly Ann Coley
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Exelus, Inc.
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Priority to PL11831033T priority Critical patent/PL2625251T3/en
Priority to EP11831033.3A priority patent/EP2625251B1/en
Priority to DK11831033.3T priority patent/DK2625251T3/en
Priority to CN201180048372.6A priority patent/CN103168088B/en
Priority to ES11831033T priority patent/ES2845613T3/en
Priority to CA2812666A priority patent/CA2812666C/en
Publication of WO2012047274A2 publication Critical patent/WO2012047274A2/en
Publication of WO2012047274A3 publication Critical patent/WO2012047274A3/en

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    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
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    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
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    • C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
    • C10G57/005—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with alkylation
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    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/085—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
    • B01J29/087—X-type faujasite
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    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J29/7815—Zeolite Beta
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    • C07C2529/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • C07C2529/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
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    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
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    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1081—Alkanes
    • C—CHEMISTRY; METALLURGY
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    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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    • C10G2300/1088—Olefins
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    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
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    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • This invention relates to the production of a high octane alkylate from a feed comprising ethylene and isobutane. More particularly, this invention relates to the production of a high octane alkylate from ethylene and isobutane by reacting ethylene and isobutane under catalytic conversion conditions in the presence of a first catalytic material which includes a dimerization catalyst, and a material which promotes regeneration of the dimerization catalyst, and a second catalytic material which includes an alkylation catalyst, wherein the first and second catalytic materials are separate and distinct from each other.
  • Fluid catalytic cracking is at the heart of every modern refinery, whereby heavy petroleum components are converted into high-value fuels.
  • the FCC operation as well as other common cracking processes, invariably makes a range of products, from light gases to heavy fuel oil. Included in this range are light paraffins and olefins in the range of C 2 (ethane, ethylene) to C (butane, isobutane, butenes, isobutylene).
  • a refiner will combine chemically the C 4 olefins (and possibly C 3 and C 5 olefins as well) with the isobutane in a process called alkylation.
  • the product from this process is called alkylate.
  • Alkylate is the cleanest gasoline blending stream produced in refineries and is an ideal clean fuel component because it has a high octane rating, low vapor pressure, and low toxicity. Alkylate has been blended into gasoline for decades to improve octane and thus the antiknock properties of gasoline. In addition, strict state and federal limitations on the formulation and physical properties of gasoline makes alkylate one of the most important and valuable blendstocks of the gasoline pool. Currently, large scale production of alkylate is produced by a process known as isoparaffin alkylation.
  • isoparaffin alkylation is a liquid acid catalyzed reaction that combines isobutane with alkenes such as propylene, butenes, and amylenes (C3-C5 olefins).
  • refiners employ either hydrofluoric acid (HF) or sulfuric acid (H 2 S0 4 ) as the liquid alkylation catalyst.
  • Ethylene (C 2 olefin) is another major component produced in the FCC unit.
  • the liquid acid catalysts used in all commercial alkylation units are quite effective in activating the C3-C5 olefins, they cannot activate ethylene. Instead ethylene forms stable ethyl ethers with the acids in these units, thereby providing an inert and useless mixture. (Nivarty, et al., Microporous and Mesoporous Materials, Vol. 35-36, pages 75-87 (2000)). Consequently, no commercial alkylation units are capable of alkylating ethylene.
  • Friedel-Crafts type catalysts such as BF 3 and chlorided alumina are needed to activate ethylene for alkylation (Goupil, et al., Catalysis Letters, Vol. 31 , pages 121 - 131 ( 1995); Hoffman, U.S. Patent No. 3,873,634).
  • the most active catalysts for isoparaffin alkylation with ethylene are mixtures of Lewis acids and protic mineral acids, such as HC1 and A 1 C 1 3 , because such blends have Lewis sites capable of activating ethylene and the requisite Br0nsted sites that promote the subsequent hybrid shift reactions (Olah, et al., Hydrocarbon Chemistry, 2 nd Edition, Wiley Interscience, page 632 (1995)).
  • zeolite Beta displayed stable ethylene conversion of only 40% for ten hours but gave complete conversion for butene (Nivarthy, et al.) under the same conditions.
  • the activation barrier for protonation of ethylene can be quite high (23-30 kcal/mol) (Namuangruk, et al., Chemphys. Chem., Vol. 6, pages 1333- 1339 (2005); Svelle, et al., J. Physical Chemistry. Vol. 108, pages 2953-2962 (2004)).
  • known solid acid catalysts also are unsuitable for alkylating directly with ethylene in a commercial process, as they would require impractical ly large quantities of catalyst.
  • Ethylene can be converted into butene by dimerization, whereby two ethylene molecules are combined into a single butene molecule. Dimerization of ethylene to butene is practiced commercially in the Axens Alphabutol process, for example. Such commercial processes require highly selective homogeneous catalysts, such as those disclosed in U.S. Patent No. 5, 162,595, and are limited to relatively pure streams of ethylene. Heterogeneous catalysts for ethylene oligomerization are not selective for butenes and provide for the production of less desired higher olefins.
  • the problem with this approach is that the dimerization sites within the alkylation catalyst become deactivated with use by a type of coke that cannot be removed except under very harsh regeneration conditions.
  • the only method suitable for regenerating the dimerization sites on such a catalyst is first to oxidize the coke with an oxygen-containing stream such as air, and then hydrogenate any remaining coke using a hydrogen-containing stream. Both steps occur at elevated (250°C) temperatures.
  • Such regeneration schemes are not practical in industrial operation due to the hazards of introducing oxygen to a hydrocarbon process and the need to purge the system frequently as it is changed from hydrocarbon-based to oxygen-based.
  • the present invention is directed to producing a high octane alkylate from either concentrated or diluted streams of ethylene, in contrast to conventional processes that are capable of employing only concentrated ethylene streams.
  • a method of producing a high octane alkylate from ethylene and isobutane comprises reacting ethylene and isobutane under catalytic conversion conditions.
  • the ethylene and isobutane are contacted with a first catalytic material and a second catalytic material.
  • the first catalytic material comprises a dimerization catalyst and a material which promotes regeneration of the dimerization catalyst.
  • the second catalytic material comprises an alkylation catalyst.
  • the first catalytic material and the second catalytic material are separate and distinct from each other. Subsequent to the reacting of the ethylene and isobutane, a high octane alkylate is recovered.
  • first and second catalytic materials are two independent and physically separate materials.
  • first and second catalytic materials may be admixed physically with each other, e. g., wherein particles or pellets of the first catalytic material and particles or pellets of the second catalytic material are contained in the same catalyst bed, or the first and second catalytic materials may be contained in the same particle or pellet, the first and second catalytic materials retain their separate identities.
  • the first catalytic material comprises a dimerization catalyst and a material which promotes regeneration of the dimerization catalyst.
  • the dimerization catalyst catalyzes the dimerization of ethylene to butene, which then is reacted with isobutane to produce a high octane alkylate.
  • the dimerization catalyst comprises a metal and a support for the metal.
  • Metals which may be employed in the dimerization catalyst include, but are not limited to, nickel, palladium, chromium, vanadium, iron, cobalt, ruthenium, rhodium, copper, silver, rhenium, molybdenum, tungsten, and manganese.
  • Supports which may be employed include, but are not limited to, zeolites, alumina, silica, carbon, titania, zirconia, silica/alumina, and mesoporous silicas.
  • the dimerization catalyst is made by depositing or impregnating salts of the metal onto the support.
  • the metal is deposited or impregnated onto the support in an amount of about 0.1 wt.% to about 10 wt.%, 1 001682
  • the catalyst then is dried and calcined in air or nitrogen, thereby anchoring the metal to the support.
  • dimerization catalysts which may be employed include, but are not limited to, nickel supported on dealuminated zeolite Y; nickel supported on impregnated silica/alumina; nickel supported on the aluminum exchanged mesoporous zeolite A 1 MCM-41 ; nickel supported on zeolite ZSM-5; bis (imino) pyridyl iron (II) supported on silica; iron (II) tridentate di (imino) supported on silica gel; manganese, chromium, and/or vanadium with modified methylaluminoxane ligands; nickel, cobalt, palladium, platinum, or iron supported on silica activated with modified methylaluminoxane ligands; and chromium supported on silica gel with aluminum rea
  • the dimerization catalyst also includes a material which promotes regeneration of the dimerization catalyst.
  • the material which promotes regeneration of the dimerization catalyst is a hydrogenation catalyst.
  • Hydrogenation catalysts which may be employed include, but are not limited to, platinum, nickel, and palladium.
  • the hydrogenation catalyst is platinum.
  • the hydrogenation catalyst is palladium.
  • the hydrogenation catalyst is nickel.
  • the alkylation catalyst in general is a catalyst which exhibits at least some activity for the alkylation of isobutane with butenes (i.e., formed as a result of the dimerization of ethylene).
  • alkylation catalysts which may be employed include, but are not limited to, zeolites, sulfated zirconia, tungstated zirconia, chlorided alumina, aluminum chloride (AICI3), silicon-aluminum phosphates, titaniosilicates (including VTM zeolite), polyphosphoric acid (including solid phosphoric acid, or SPA, catalysts, which are made by reacting phosphoric acid with diatomaceous earth), polytungstic acid, and supported liquid acids such as triflic acid on silica, sulfuric acid on silica, hydrogen fluoride on carbon, antimony fluoride on silica, and aluminum chloride (AICI3) on alumina (A1 2 0 3 ).
  • the alkylation catalyst is a zeolite.
  • Zeolites which may be employed include, but are not limited to, zeolite Beta; BEA* zeolites; MC zeolites; faujasites including zeolite X, zeolite Y (including rare earth-exchanged zeolite X and zeolite Y), and USY zeolites; LTL zeolites; mordenite; MF1 zeolites, including ZSM-5; EMT zeolites; LTA zeolites; 1TW zeolites, ITQ zeolites, and SFO zeolites.
  • ethylene and isobutane are reacted under catalytic conversion conditions and are contacted with the first and second catalytic materials hereinbove described to produce a high octane alkylate.
  • the feed in addition to ethylene and isobutane, also may include paraffins (e.g., methane, ethane, propane, butane, etc.) and olefins (e.g., propylene, butenes, pentenes, etc.). The feed is reacted over the catalytic materials to produce alkylate.
  • the feed includes olefins other than ethylene, such olefins also may be reacted to produce alkylate.
  • isoparaffins other than isobutane e.g., isopentane
  • isoparaffins other than isobutane e.g., isopentane
  • the reaction may be conducted in the liquid phase, a mixed gas-liquid phase, or the gas phase.
  • the reaction is conducted in the liquid phase or in a mixed phase in which the ethylene-containing stream is combined with a liquid isobutane-containing stream to make a two-phase feed stream.
  • the composition of each phase is determined by the vapor-liquid equilibrium of the resulting mixture at the temperature and pressure used.
  • the ethylene and isobutane are reacted under conditions which produce a high octane alkylate.
  • the ethylene and isobutane are reacted at a temperature of from about 60° to about 150°C.
  • the ethylene and isobutane are reacted at a temperature of about 75°C.
  • the ethylene and isobutane are reacted at a pressure of up to about 500 psig. In yet another non-limiting embodiment, the ethylene and isobutane are reacted at a pressure of from about 300 psig to about 400 psig.
  • the ethylene and isobutane are reacted at a molar ratio of isobutane to ethylene of from about 5 to about 15. In another non-limiting embodiment, the ethylene and isobutane are reacted at a molar ratio of from about 8 to about 12.
  • the method of the present invention further comprises regenerating the first catalytic material.
  • the regeneration of the first catalytic material comprises contacting the first catalytic material with hydrogen.
  • the first catalytic material is contacted with hydrogen at a temperature of from about 250°C about 350°C.
  • the hydrogen reacts with ethylene oligomers (eg., hexene, octene) which may have formed on the first catalytic material in the presence of the hydrogenation catalyst contained in the first catalytic material, whereby the oligomers become saturated, thereby enabling the saturated oligomers to be desorbed thermally from the first catalytic material, thereby providing for the regeneration of the dimerization catalyst contained in the first catalytic material.
  • ethylene oligomers eg., hexene, octene
  • the first and second catalytic materials are separate and distinct from each other. By keeping the first and second catalytic materials separate and distinct from each other, the formation of hard coke on the alkylation catalyst included in the second catalytic material is prevented.
  • the strong acid sites which are present on the alkylation catalyst do not contribute to the formation of hard coke on both the dimerization catalyst and the alkylation catalyst.
  • the first and second materials are prevented from interacting with each other undesirably, thereby preventing the formation of coke which would make regeneration of the first and second catalytic materials more difficult.
  • the first and second catalytic materials may be combined in a single reactor or, may be contained in separate reactors.
  • a plurality i.e., three or more reactors, in which reactors containing the first and second catalytic materials are arranged in an alternating series.
  • particles or pellets of the first catalytic material and particles or pellets of the second catalytic material are combined in a single reactor.
  • the particles or pellets of the first and second catalytic materials are combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 : 10 to about 10: 1.
  • the particles or pellets of the first and second catalytic materials are combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 :5 to about 5: 1 .
  • the first catalytic material and the second catalytic material are mixed and combined physically into particles or pellets, whereby each of such particles or pellets includes the first catalytic material and the second catalytic material. In such particles, or pellets, the first catalytic material is not contained within the second catalytic material or absorbed on the surface of the second catalytic material and vice versa. In one non- limiting embodiment, when the first and second catalytic materials are mixed and combined physically into particles or pellets, the first and second catalytic materials are mixed and combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 : 10 to about 10: 1 . In another non-limiting embodiment, the first and second catalytic materials are mixed and combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 :5 to 5: 1 .
  • the physical mixing of the two catalytic materials provides for rapid consumption of butenes formed on the dimerization catalyst through the alkylation of isobutane with the butenes in the presence of the alkylation catalyst. This enhances the quality and yield of alkylate formed by minimizing the production of higher oligomers of ethylene (e.g., hexenes, octenes).
  • Such physical mixing of the first and second catalytic materials also limits the dimerization activity, which is highly exothermic, thereby reducing "hot spots" in the catalyst bed.
  • the relative amount of ethylene dimerization activity and alkylation activity can be controlled by adjusting the amounts of each of the first and second catalytic materials.
  • the present invention enables one to react as much ethylene as possible, produces a high octane alkylate that is almost identical to that produced when using butenes as the initial olefin, and employs a regenerable catalyst that requires only a single regeneration step.
  • Figure 1 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated zeolite Beta catalyst or a zeolite Beta catalyst impregnated with palladium;
  • TOS time on stream
  • Figure 2 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated lanthanum-exchanged zeolite X catalyst or a lanthanum-exchanged zeolite X catalyst impregnated with palladium;
  • TOS time on stream
  • Figure 3 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated zeolite Beta catalyst or a zeolite Beta catalyst impregnated with nickel;
  • TOS time on stream
  • Figure 4 is a graph of time on stream (TOS) versus percent ethylene conversion, for the first and second reaction runs wherein ethylene is reacted with isobutane in the presence of a zeolite Beta catalyst impregnated with nickel; and
  • Figure 5 is a graph of time on stream (TOS) versus percent olefin conversion, wherein ethylene is reacted with isobutane in the presence of separate dimerization and alkylation catalysts.
  • An alkylation catalyst was prepared by converting zeolite Beta into its acidic form through exchange with a 0.5 M ammonium nitrate solution, followed by drying and calcination, using techniques well established in the art.
  • a dimerization catalyst in the form of tetraamine palladium (II) nitrate was added to achieve a loading of 0.1 wt% Pd in the finished catalyst.
  • the Pd salt was added via conventional wet impregnation procedures that included dissolving the desired amount of salt in distilled water, adding the solution to the dry catalyst, allowing the solution to remain in the catalyst for a period of 4 hours, removing the solvent (water) through evaporation, and then calcining in air to decompose the salt.
  • Each catalyst was activated in the reactor prior to catalyst testing by passing hydrogen over the catalyst bed at 350°C.
  • Two gram samples of each of the Pd-impregnated and untreated alkylation catalyst were tested for ethylene alkylation activity under identical conditions.
  • a feed of ethylene in isobutane at a 12 to 1 isobutane to ethylene molar ratio was contacted with a fixed bed of the catalyst in a once-through, continuous flow reactor system.
  • the feed flow rate was at 1 .2 hr " 1 weight hourly space velocity.
  • the reaction temperature was 80°C and the pressure was 400 psig.
  • Example 2 The procedure of Example 1 was repeated except that a La-exchanged zeolite X was used as the parent alkylation catalyst. The catalyst was tested under conditions identical to those in Example 1. The results of this test are shown in Figure 2. Again, the Pd-containing catalyst exhibits significantly higher activity for ethylene alkylation than the parent material. The fraction of the alkylate present as the desirable octane (C 8 ) isomers increased from 70% with the untreated catalyst to 90% with the Pd-treated catalyst. The alkylate produced by the Pd-treated catalyst had a research octane number (RON) of 97.5.
  • RON research octane number
  • Example 3 The procedure of Example 1 was repeated except that the alkylation catalyst was exchanged with an aqueous solution of 0.2 M nickel nitrate in lieu of the Pd salt impregnation.
  • the exchanged catalyst was washed with distilled water and dried, and subsequently calcined.
  • the catalyst had a Ni loading of 5 wt%.
  • the Ni-exchanged catalyst was activated and tested in the same manner as Example 1. The results of this test are given in Figure 3.
  • the nickel-containing catalyst exhibits the same increase in activity as the catalysts containing Pd, which shows clearly that any metal that catalyzes ethylene dimerization may be employed in the present invention.
  • the benefit of having nickel or other base metals is their substantially lower cost compared to a precious metal such as palladium.
  • the catalysts shown in the prior examples are active, they are not able to be regenerated without the undesirable use of an oxidation step.
  • a common regeneration material, Pt is added to a fresh sample of the Ni-zeolite Beta catalyst from Example 3.
  • the catalyst is used in the reaction of ethylene and isobutane at a temperature of 75°C, a pressure of 400 psig, an olefin space velocity of 0.20 hr " 1 , and a feed isobutane/ethylene ratio of 12 mol/mol.
  • the run is stopped and the catalyst is regenerated by heating to 400°C under flowing hydrogen for 3 hours. The run is then repeated. As shown in Figure 4, full activity is not restored to the catalyst.
  • a dimerization catalyst is made by impregnating 1 wt.% Ni onto a support of silica- alumina. 0.1 wt.% Pt is also added as a hydrogenation catalyst.
  • a separate alkylation catalyst is prepared by adding 0.1 wt.% Pt to zeolite Beta. The two catalysts are mixed physically in a reactor. The mixed catalysts are used for the alkylation of isobutane with ethylene under the same conditions as in Example 4. As in Example 4, the run is stopped after 8 hours, and the catalyst is regenerated by heating to 400°C under flowing hydrogen for 3 hours. The run was then repeated twice more. The results, shown in Figure 5, demonstrate that full catalyst activity is restored after each cycle.

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Abstract

A method of producing a high octane alkylate from ethylene and isobutane by reacting ethylene and isobutane under catalytic conversion conditions. The ethylene and isobutane are contacted with a first catalytic material comprising a dimerization catalyst (i.e, for dimerizing ethylene) and a second catalytic material comprising an alkylation catalyst. The first and second catalytic materials are separate and distinct from each other. A high octane alkylate is recovered as a result of reacting the ethylene and isobutane in the presence of the first and second catalytic materials.

Description

PRODUCTION OF A HIGH OCTANE ALKYLATE
FROM ETHYLENE AND ISOBUTANE
This application claims priority based on Provisional Application Serial No. 61 /404,597, filed October 6, 2010, the contents of which are incorporated by reference in their entirety.
This invention relates to the production of a high octane alkylate from a feed comprising ethylene and isobutane. More particularly, this invention relates to the production of a high octane alkylate from ethylene and isobutane by reacting ethylene and isobutane under catalytic conversion conditions in the presence of a first catalytic material which includes a dimerization catalyst, and a material which promotes regeneration of the dimerization catalyst, and a second catalytic material which includes an alkylation catalyst, wherein the first and second catalytic materials are separate and distinct from each other.
Fluid catalytic cracking, or FCC, is at the heart of every modern refinery, whereby heavy petroleum components are converted into high-value fuels. The FCC operation, as well as other common cracking processes, invariably makes a range of products, from light gases to heavy fuel oil. Included in this range are light paraffins and olefins in the range of C2 (ethane, ethylene) to C (butane, isobutane, butenes, isobutylene). Typically, a refiner will combine chemically the C4 olefins (and possibly C3 and C5 olefins as well) with the isobutane in a process called alkylation. The product from this process is called alkylate.
Alkylate is the cleanest gasoline blending stream produced in refineries and is an ideal clean fuel component because it has a high octane rating, low vapor pressure, and low toxicity. Alkylate has been blended into gasoline for decades to improve octane and thus the antiknock properties of gasoline. In addition, strict state and federal limitations on the formulation and physical properties of gasoline makes alkylate one of the most important and valuable blendstocks of the gasoline pool. Currently, large scale production of alkylate is produced by a process known as isoparaffin alkylation. Commercially, isoparaffin alkylation is a liquid acid catalyzed reaction that combines isobutane with alkenes such as propylene, butenes, and amylenes (C3-C5 olefins). For this process, refiners employ either hydrofluoric acid (HF) or sulfuric acid (H2S04) as the liquid alkylation catalyst.
Ethylene (C2 olefin) is another major component produced in the FCC unit. Although the liquid acid catalysts used in all commercial alkylation units are quite effective in activating the C3-C5 olefins, they cannot activate ethylene. Instead ethylene forms stable ethyl ethers with the acids in these units, thereby providing an inert and useless mixture. (Nivarty, et al., Microporous and Mesoporous Materials, Vol. 35-36, pages 75-87 (2000)). Consequently, no commercial alkylation units are capable of alkylating ethylene.
In alkylation, protonation of the olefin is a vital initiation step (Corma, et al., Trends Catal. Rev.-Sci. Eng., Vol. 35, pg. 483 (1993), and thus activation of the olefin greatly depends on the stability of the carbocation generated. Inherently, ethylene is less reactive compared to butene; protonation of either carbon atom in ethylene results in the formation of an unstable primary carbocation, whereas protonation of butene forms a more-stable secondary carbocation.
Butene can be protonated easily during conventional alkylation by Br0nsted acids, such as the conventional liquid acid catalysts. In contrast, Friedel-Crafts type catalysts such as BF3 and chlorided alumina are needed to activate ethylene for alkylation (Goupil, et al., Catalysis Letters, Vol. 31 , pages 121 - 131 ( 1995); Hoffman, U.S. Patent No. 3,873,634). The most active catalysts for isoparaffin alkylation with ethylene are mixtures of Lewis acids and protic mineral acids, such as HC1 and A 1 C 13, because such blends have Lewis sites capable of activating ethylene and the requisite Br0nsted sites that promote the subsequent hybrid shift reactions (Olah, et al., Hydrocarbon Chemistry, 2nd Edition, Wiley Interscience, page 632 (1995)). A related catalyst, an ionic liquid with an aluminum chloride anion, was used in US Patent No. 7,432,408 to alkylate isopentane with ethylene.
These catalysts, however, are sensitive to trace water, deactivate readily, and corrode equipment. Therefore, they are not suitable for a cost-effective refinery process and have not been employed commercially for this use.
Zeolites possess both Br0nsted and Lewis acid sites; however, these catalysts do not exhibit high activity for ethylene alkylation. For example, it was reported that zeolite Beta displayed stable ethylene conversion of only 40% for ten hours but gave complete conversion for butene (Nivarthy, et al.) under the same conditions. It also has been calculated in other zeolitic systems that the activation barrier for protonation of ethylene can be quite high (23-30 kcal/mol) (Namuangruk, et al., Chemphys. Chem., Vol. 6, pages 1333- 1339 (2005); Svelle, et al., J. Physical Chemistry. Vol. 108, pages 2953-2962 (2004)). As a result of this low activity, known solid acid catalysts also are unsuitable for alkylating directly with ethylene in a commercial process, as they would require impractical ly large quantities of catalyst.
Ethylene can be converted into butene by dimerization, whereby two ethylene molecules are combined into a single butene molecule. Dimerization of ethylene to butene is practiced commercially in the Axens Alphabutol process, for example. Such commercial processes require highly selective homogeneous catalysts, such as those disclosed in U.S. Patent No. 5, 162,595, and are limited to relatively pure streams of ethylene. Heterogeneous catalysts for ethylene oligomerization are not selective for butenes and provide for the production of less desired higher olefins.
One known alternative used to circumvent the problem of low ethylene reactivity 1682
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is to incorporate an ethylene dimerization function into an alkylation catalyst. With this catalyst, the ethylene first is dimerized into butenes, which then undergo conventional alkylation with isobutane. Butenes are much more reactive for alkylation than ethylene, resulting in a higher overall reaction rate. This, however, still requires a suitable alkylation catalyst, and the addition of a dimerization function to the alkylation catalyst prevents the combined catalyst from being regenerated due to the formation of difficult-to-remove ethylene oligomers and coke.
The problem with this approach is that the dimerization sites within the alkylation catalyst become deactivated with use by a type of coke that cannot be removed except under very harsh regeneration conditions. The only method suitable for regenerating the dimerization sites on such a catalyst is first to oxidize the coke with an oxygen-containing stream such as air, and then hydrogenate any remaining coke using a hydrogen-containing stream. Both steps occur at elevated (250°C) temperatures. Such regeneration schemes are not practical in industrial operation due to the hazards of introducing oxygen to a hydrocarbon process and the need to purge the system frequently as it is changed from hydrocarbon-based to oxygen-based.
The present invention is directed to producing a high octane alkylate from either concentrated or diluted streams of ethylene, in contrast to conventional processes that are capable of employing only concentrated ethylene streams.
In accordance with an aspect of the present invention, there is provided a method of producing a high octane alkylate from ethylene and isobutane. The method comprises reacting ethylene and isobutane under catalytic conversion conditions. The ethylene and isobutane are contacted with a first catalytic material and a second catalytic material. The first catalytic material comprises a dimerization catalyst and a material which promotes regeneration of the dimerization catalyst. The second catalytic material comprises an alkylation catalyst. The first catalytic material and the second catalytic material are separate and distinct from each other. Subsequent to the reacting of the ethylene and isobutane, a high octane alkylate is recovered.
The term, "separate and distinct from each other," with respect to the first and second catalytic materials, as used herein, means that the first and second catalytic materials are two independent and physically separate materials. Although, in non-limiting embodiments of the present invention, the first and second catalytic materials may be admixed physically with each other, e. g., wherein particles or pellets of the first catalytic material and particles or pellets of the second catalytic material are contained in the same catalyst bed, or the first and second catalytic materials may be contained in the same particle or pellet, the first and second catalytic materials retain their separate identities.
The first catalytic material, as noted hereinabove, comprises a dimerization catalyst and a material which promotes regeneration of the dimerization catalyst. The dimerization catalyst catalyzes the dimerization of ethylene to butene, which then is reacted with isobutane to produce a high octane alkylate. In a non-limiting embodiment, the dimerization catalyst comprises a metal and a support for the metal. Metals which may be employed in the dimerization catalyst include, but are not limited to, nickel, palladium, chromium, vanadium, iron, cobalt, ruthenium, rhodium, copper, silver, rhenium, molybdenum, tungsten, and manganese. Supports which may be employed include, but are not limited to, zeolites, alumina, silica, carbon, titania, zirconia, silica/alumina, and mesoporous silicas.
In a non-limiting embodiment, the dimerization catalyst is made by depositing or impregnating salts of the metal onto the support. In a non-limiting embodiment, the metal is deposited or impregnated onto the support in an amount of about 0.1 wt.% to about 10 wt.%, 1 001682
based on the weight of the support. The catalyst then is dried and calcined in air or nitrogen, thereby anchoring the metal to the support.
Although the scope of the present invention is not to be limited to any theoretical reasoning, it is believed that the activity of the dimerization catalyst is created by the interaction of the metal and the support. In a non-limiting embodiment, dimerization catalysts which may be employed include, but are not limited to, nickel supported on dealuminated zeolite Y; nickel supported on impregnated silica/alumina; nickel supported on the aluminum exchanged mesoporous zeolite A 1 MCM-41 ; nickel supported on zeolite ZSM-5; bis (imino) pyridyl iron (II) supported on silica; iron (II) tridentate di (imino) supported on silica gel; manganese, chromium, and/or vanadium with modified methylaluminoxane ligands; nickel, cobalt, palladium, platinum, or iron supported on silica activated with modified methylaluminoxane ligands; and chromium supported on silica gel with aluminum reagents.
The dimerization catalyst also includes a material which promotes regeneration of the dimerization catalyst. In a non-limiting embodiment, the material which promotes regeneration of the dimerization catalyst is a hydrogenation catalyst. Hydrogenation catalysts which may be employed include, but are not limited to, platinum, nickel, and palladium. In a non-limiting embodiment, the hydrogenation catalyst is platinum. In another non-limiting embodiment, the hydrogenation catalyst is palladium. In another non-limiting embodiment, the hydrogenation catalyst is nickel.
The alkylation catalyst in general is a catalyst which exhibits at least some activity for the alkylation of isobutane with butenes (i.e., formed as a result of the dimerization of ethylene). In a non-limiting embodiment, alkylation catalysts which may be employed include, but are not limited to, zeolites, sulfated zirconia, tungstated zirconia, chlorided alumina, aluminum chloride (AICI3), silicon-aluminum phosphates, titaniosilicates (including VTM zeolite), polyphosphoric acid (including solid phosphoric acid, or SPA, catalysts, which are made by reacting phosphoric acid with diatomaceous earth), polytungstic acid, and supported liquid acids such as triflic acid on silica, sulfuric acid on silica, hydrogen fluoride on carbon, antimony fluoride on silica, and aluminum chloride (AICI3) on alumina (A1203).
In a non-limiting embodiment, the alkylation catalyst is a zeolite. Zeolites which may be employed include, but are not limited to, zeolite Beta; BEA* zeolites; MC zeolites; faujasites including zeolite X, zeolite Y (including rare earth-exchanged zeolite X and zeolite Y), and USY zeolites; LTL zeolites; mordenite; MF1 zeolites, including ZSM-5; EMT zeolites; LTA zeolites; 1TW zeolites, ITQ zeolites, and SFO zeolites.
As noted hereinabove, ethylene and isobutane are reacted under catalytic conversion conditions and are contacted with the first and second catalytic materials hereinbove described to produce a high octane alkylate. In a non-limiting embodiment, the feed, in addition to ethylene and isobutane, also may include paraffins (e.g., methane, ethane, propane, butane, etc.) and olefins (e.g., propylene, butenes, pentenes, etc.). The feed is reacted over the catalytic materials to produce alkylate. If the feed includes olefins other than ethylene, such olefins also may be reacted to produce alkylate. In addition, isoparaffins other than isobutane (e.g., isopentane), if present, also may be reacted to form alkylate.
The reaction may be conducted in the liquid phase, a mixed gas-liquid phase, or the gas phase. In a non-limiting embodiment, the reaction is conducted in the liquid phase or in a mixed phase in which the ethylene-containing stream is combined with a liquid isobutane-containing stream to make a two-phase feed stream. The composition of each phase is determined by the vapor-liquid equilibrium of the resulting mixture at the temperature and pressure used. The ethylene and isobutane are reacted under conditions which produce a high octane alkylate. In a non-limiting embodiment, the ethylene and isobutane are reacted at a temperature of from about 60° to about 150°C. In another non-limiting embodiment, the ethylene and isobutane are reacted at a temperature of about 75°C.
In another non-limiting embodiment, the ethylene and isobutane are reacted at a pressure of up to about 500 psig. In yet another non-limiting embodiment, the ethylene and isobutane are reacted at a pressure of from about 300 psig to about 400 psig.
In a further non-limiting embodiment, the ethylene and isobutane are reacted at a molar ratio of isobutane to ethylene of from about 5 to about 15. In another non-limiting embodiment, the ethylene and isobutane are reacted at a molar ratio of from about 8 to about 12.
In a non-limiting embodiment, the method of the present invention further comprises regenerating the first catalytic material. In a further non-limiting embodiment, the regeneration of the first catalytic material comprises contacting the first catalytic material with hydrogen. In yet another non-limiting embodiment, the first catalytic material is contacted with hydrogen at a temperature of from about 250°C about 350°C.
Although the scope of this embodiment of the present invention is not to be limited to any theoretical reasoning, it is believed that the hydrogen reacts with ethylene oligomers (eg., hexene, octene) which may have formed on the first catalytic material in the presence of the hydrogenation catalyst contained in the first catalytic material, whereby the oligomers become saturated, thereby enabling the saturated oligomers to be desorbed thermally from the first catalytic material, thereby providing for the regeneration of the dimerization catalyst contained in the first catalytic material.
As noted hereinabove, the first and second catalytic materials are separate and distinct from each other. By keeping the first and second catalytic materials separate and distinct from each other, the formation of hard coke on the alkylation catalyst included in the second catalytic material is prevented.
More particularly, the strong acid sites which are present on the alkylation catalyst do not contribute to the formation of hard coke on both the dimerization catalyst and the alkylation catalyst. By keeping the first and second materials separate and distinct from each other, the first and second catalytic materials are prevented from interacting with each other undesirably, thereby preventing the formation of coke which would make regeneration of the first and second catalytic materials more difficult.
The first and second catalytic materials may be combined in a single reactor or, may be contained in separate reactors. In yet another alternative non-binding embodiment, there is provided a plurality (i.e., three or more) reactors, in which reactors containing the first and second catalytic materials are arranged in an alternating series.
In a non-limiting embodiment, particles or pellets of the first catalytic material and particles or pellets of the second catalytic material are combined in a single reactor. In one non- limiting embodiment, when particles or pellets of the first catalytic material are combined with particles or pellets of the second catalytic material in a single reactor, the particles or pellets of the first and second catalytic materials are combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 : 10 to about 10: 1. In another non- limiting embodiment, the particles or pellets of the first and second catalytic materials are combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 :5 to about 5: 1 .
In another non-limiting embodiment, the first catalytic material and the second catalytic material are mixed and combined physically into particles or pellets, whereby each of such particles or pellets includes the first catalytic material and the second catalytic material. In such particles, or pellets, the first catalytic material is not contained within the second catalytic material or absorbed on the surface of the second catalytic material and vice versa. In one non- limiting embodiment, when the first and second catalytic materials are mixed and combined physically into particles or pellets, the first and second catalytic materials are mixed and combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 : 10 to about 10: 1 . In another non-limiting embodiment, the first and second catalytic materials are mixed and combined at a weight ratio of the first catalytic material to the second catalytic material of from about 1 :5 to 5: 1 .
Although the scope of the above embodiments is not intended to be limited to any theoretical reasoning, the physical mixing of the two catalytic materials provides for rapid consumption of butenes formed on the dimerization catalyst through the alkylation of isobutane with the butenes in the presence of the alkylation catalyst. This enhances the quality and yield of alkylate formed by minimizing the production of higher oligomers of ethylene (e.g., hexenes, octenes). Such physical mixing of the first and second catalytic materials also limits the dimerization activity, which is highly exothermic, thereby reducing "hot spots" in the catalyst bed. In addition, the relative amount of ethylene dimerization activity and alkylation activity can be controlled by adjusting the amounts of each of the first and second catalytic materials.
Thus, the present invention enables one to react as much ethylene as possible, produces a high octane alkylate that is almost identical to that produced when using butenes as the initial olefin, and employs a regenerable catalyst that requires only a single regeneration step.
The invention now will be described with respect to the drawings, wherein: Figure 1 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated zeolite Beta catalyst or a zeolite Beta catalyst impregnated with palladium;
Figure 2 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated lanthanum-exchanged zeolite X catalyst or a lanthanum-exchanged zeolite X catalyst impregnated with palladium;
Figure 3 is a graph of time on stream (TOS) versus percent ethylene conversion, wherein ethylene is reacted with isobutane in the presence of an untreated zeolite Beta catalyst or a zeolite Beta catalyst impregnated with nickel;
Figure 4 is a graph of time on stream (TOS) versus percent ethylene conversion, for the first and second reaction runs wherein ethylene is reacted with isobutane in the presence of a zeolite Beta catalyst impregnated with nickel; and
Figure 5 is a graph of time on stream (TOS) versus percent olefin conversion, wherein ethylene is reacted with isobutane in the presence of separate dimerization and alkylation catalysts.
2
EXAMPLES
The invention now will be described with respect to the following examples. It is to be understood, however, that the scope of the present invention is not intended to be limited thereby.
Example 1
This example demonstrates that adding a dimerization catalyst to a known alkylation catalyst results in a significant improvement in performance when using ethylene as the olefin.
An alkylation catalyst was prepared by converting zeolite Beta into its acidic form through exchange with a 0.5 M ammonium nitrate solution, followed by drying and calcination, using techniques well established in the art. To one portion of this material a dimerization catalyst in the form of tetraamine palladium (II) nitrate was added to achieve a loading of 0.1 wt% Pd in the finished catalyst. The Pd salt was added via conventional wet impregnation procedures that included dissolving the desired amount of salt in distilled water, adding the solution to the dry catalyst, allowing the solution to remain in the catalyst for a period of 4 hours, removing the solvent (water) through evaporation, and then calcining in air to decompose the salt. Each catalyst was activated in the reactor prior to catalyst testing by passing hydrogen over the catalyst bed at 350°C.
Two gram samples of each of the Pd-impregnated and untreated alkylation catalyst were tested for ethylene alkylation activity under identical conditions. A feed of ethylene in isobutane at a 12 to 1 isobutane to ethylene molar ratio was contacted with a fixed bed of the catalyst in a once-through, continuous flow reactor system. The feed flow rate was at 1 .2 hr" 1 weight hourly space velocity. The reaction temperature was 80°C and the pressure was 400 psig.
The results of this test are shown in Figure 1 . While the untreated catalyst lost activity for ethylene alkylation rapidly, the catalyst including the Pd dimerization catalyst exhibited full ethylene conversion for the duration of the test. Furthermore, the fraction of the alkylate present as desirable octane (Cg) isomers increased from 26% with the untreated catalyst to 60% with the Pd-treated catalyst. The alkylate produced by the Pd-treated catalyst had a research octane number (RON) of 90.
Example 2
The procedure of Example 1 was repeated except that a La-exchanged zeolite X was used as the parent alkylation catalyst. The catalyst was tested under conditions identical to those in Example 1. The results of this test are shown in Figure 2. Again, the Pd-containing catalyst exhibits significantly higher activity for ethylene alkylation than the parent material. The fraction of the alkylate present as the desirable octane (C8) isomers increased from 70% with the untreated catalyst to 90% with the Pd-treated catalyst. The alkylate produced by the Pd-treated catalyst had a research octane number (RON) of 97.5.
Example 3
The procedure of Example 1 was repeated except that the alkylation catalyst was exchanged with an aqueous solution of 0.2 M nickel nitrate in lieu of the Pd salt impregnation. The exchanged catalyst was washed with distilled water and dried, and subsequently calcined. The catalyst had a Ni loading of 5 wt%. The Ni-exchanged catalyst was activated and tested in the same manner as Example 1. The results of this test are given in Figure 3.
As shown in Figure 3, the nickel-containing catalyst exhibits the same increase in activity as the catalysts containing Pd, which shows clearly that any metal that catalyzes ethylene dimerization may be employed in the present invention. The benefit of having nickel or other base metals is their substantially lower cost compared to a precious metal such as palladium. Example 4
Although the catalysts shown in the prior examples are active, they are not able to be regenerated without the undesirable use of an oxidation step. In this example, a common regeneration material, Pt, is added to a fresh sample of the Ni-zeolite Beta catalyst from Example 3. The catalyst is used in the reaction of ethylene and isobutane at a temperature of 75°C, a pressure of 400 psig, an olefin space velocity of 0.20 hr" 1 , and a feed isobutane/ethylene ratio of 12 mol/mol. After 8 hours, the run is stopped and the catalyst is regenerated by heating to 400°C under flowing hydrogen for 3 hours. The run is then repeated. As shown in Figure 4, full activity is not restored to the catalyst.
Example 5
A dimerization catalyst is made by impregnating 1 wt.% Ni onto a support of silica- alumina. 0.1 wt.% Pt is also added as a hydrogenation catalyst. A separate alkylation catalyst is prepared by adding 0.1 wt.% Pt to zeolite Beta. The two catalysts are mixed physically in a reactor. The mixed catalysts are used for the alkylation of isobutane with ethylene under the same conditions as in Example 4. As in Example 4, the run is stopped after 8 hours, and the catalyst is regenerated by heating to 400°C under flowing hydrogen for 3 hours. The run was then repeated twice more. The results, shown in Figure 5, demonstrate that full catalyst activity is restored after each cycle.
The disclosures of all patents and publications (including published patent applications) hereby are incorporated by reference to the same extent as if each patent and publication were incorporated individually by reference.
It is to be understood, however, that the scope of the present invention is not to be limited to the specific embodiments described above. The invention may be practiced other than as particularly described and still be within the scope of the accompanying claims.

Claims

WHAT IS CLAIMED:
1. A method of producing a high octane alkylate from ethylene and isobutane comprising:
(a) reacting ethylene and isobutane under catalytic conversion conditions, and wherein said ethylene and isobutane are contacted with a (i) first catalytic material comprising a dimerization catalyst and a material which promotes regeneration of said dimerization catalyst and (ii) a second catalytic material comprising an alkylation catalyst, wherein said first catalytic material and said second catalytic material are separate and distinct from each other; and
(b) recovering a high octane alkylate from step (a).
2. The method of Claim 1 wherein said material which promotes regeneration of said dimerization catalyst is a hydrogenation catalyst.
3. The method of Claim 1 wherein said dimerization catalyst comprises a metal and a support for said metal.
4. The method of Claim 3 wherein said metal is selected from the group consisting of nickel, palladium, platinum, chromium, vanadium, iron, cobalt, ruthenium, rhodium, copper, silver, rhenium, molybdenum, tungsten, and manganese.
5. The method of Claim 3 wherein said support for said metal is selected from the group consisting of zeolites, silica, alumina, carbon, titania, zirconia, silica/alumina, and mesoporous silicas.
6. The method of Claim 2 wherein said hydrogenation catalyst is selected from the group consisting of platinum, nickel, and palladium.
7. The method of Claim 6 wherein said hydrogenation catalyst is platinum.
8. The method of Claim 6 wherein said hydrogenation catalyst is palladium.
9. The method of Claim 6 wherein said hydrogenation catalyst is nickel.
10. The method of Claim 1 wherein said alkylation catalyst is selected from the group consisting of zeolites, sulfated zirconia, tungstated zirconia, chlorided alumina, aluminum chloride, silicon-aluminum phosphates, titaniosilicates, polyphosphoric acid, polytungstic acid, triflic acid on silica, sulfuric acid on silica, hydrogen fluoride on carbon, antimony fluoride on silica, and aluminum chloride on alumina.
1 1. The method of Claim 10 wherein said alkylation catalyst is a zeolite.
12. The method of Claim 1 wherein said ethylene and said isobutane are reacted at a temperature of from about 60°C to about 150°C.
13. The method of Claim 12 wherein said ethylene and said isobutane are reacted at a temperature of about 75°C.
14. The method of Claim 1 wherein said ethylene and said isobutane are reacted at a pressure of up to about 500 psig.
15. The method of Claim 14 wherein said ethylene and said isobutane are reacted at a pressure of from about 300 psig to about 400 psig.
16. The method of Claim 1 wherein said ethylene and said isobutane are reacted at a molar ratio of isobutane to ethylene of from about 5 to about 15.
17. The method of Claim 16 wherein said ethylene and said isobutane are reacted at a molar ratio of isobutane to ethylene of from about 8 to about 12.
18. The method of Claim 2, and further comprising:
(c) regenerating said first catalytic material.
19. The method of Claim 18 wherein said regenerating of said first catalytic material comprises contacting said first catalytic material with hydrogen.
20. The method of Claim 19 wherein said first catalytic material is contacted with hydrogen at a temperature of from about 250°C to about 350°C.
21. The method of Claim 1 wherein said first catalytic material and said second catalytic material are combined in a single reactor.
22. The method of Claim 21 wherein particles or pellets of said first catalytic material and particles or pellets of said second catalytic material are combined at a weight ratio of said first catalytic material to said second catalytic material of from about 1 : 10 to about 10: 1.
23. The method of Claim 22 wherein particles or pellets of said first catalytic material and particles or pellets of said second catalytic material are combined at a weight ratio of said first catalytic material to said second catalytic material of from about 1 :5 to about 5: 1.
24. The method of Claim 21 wherein said first catalytic material and said second catalytic material have been combined physically into particles or pellets, whereby each of said particles or pellets contains said first catalytic material and said second catalytic material.
25. The method of Claim 24 wherein said first catalytic material and said second catalytic material are combined physically into particles or pellets at a weight ratio of said first catalytic material to said second catalytic material of from about 1 : 10 to about 10: 1.
26. The method of Claim 25 wherein said first catalytic material and said second catalytic material are combined into particles or pellets at a weight ratio of said first catalytic material to said second catalytic material of from about 1 :5 to about 5: 1.
PCT/US2011/001682 2010-10-06 2011-09-29 Production of a high octane alkylate from ethylene and isobutane WO2012047274A2 (en)

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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10183900B2 (en) 2012-12-07 2019-01-22 Siluria Technologies, Inc. Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products
US10301234B2 (en) 2014-01-08 2019-05-28 Siluria Technologies, Inc. Ethylene-to-liquids systems and methods
US10787400B2 (en) 2015-03-17 2020-09-29 Lummus Technology Llc Efficient oxidative coupling of methane processes and systems
US10793490B2 (en) 2015-03-17 2020-10-06 Lummus Technology Llc Oxidative coupling of methane methods and systems
US10829424B2 (en) 2014-01-09 2020-11-10 Lummus Technology Llc Oxidative coupling of methane implementations for olefin production
US10836689B2 (en) 2017-07-07 2020-11-17 Lummus Technology Llc Systems and methods for the oxidative coupling of methane
US10865165B2 (en) 2015-06-16 2020-12-15 Lummus Technology Llc Ethylene-to-liquids systems and methods
US10870611B2 (en) 2016-04-13 2020-12-22 Lummus Technology Llc Oxidative coupling of methane for olefin production
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US11001542B2 (en) 2017-05-23 2021-05-11 Lummus Technology Llc Integration of oxidative coupling of methane processes
US11001543B2 (en) 2015-10-16 2021-05-11 Lummus Technology Llc Separation methods and systems for oxidative coupling of methane
US11008265B2 (en) 2014-01-09 2021-05-18 Lummus Technology Llc Reactors and systems for oxidative coupling of methane
US11186529B2 (en) 2015-04-01 2021-11-30 Lummus Technology Llc Advanced oxidative coupling of methane
US11242298B2 (en) 2012-07-09 2022-02-08 Lummus Technology Llc Natural gas processing and systems
US11254626B2 (en) 2012-01-13 2022-02-22 Lummus Technology Llc Process for separating hydrocarbon compounds

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BR122015010598A2 (en) * 2012-06-26 2019-08-20 Cytec Industries Inc. QUARTERNARY PHOSPHONE HALOALUMINATE COMPOUND AND IONIC LIQUID CATALYST
US10179753B2 (en) * 2015-10-21 2019-01-15 Exelus, Inc. Process of making olefins or alkylate by reaction of methanol and/or DME or by reaction of methanol and/or DME and butane
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US11530172B2 (en) 2020-11-18 2022-12-20 Kellogg Brown & Root Llc Integration of a steam cracker with acid alkylation
US11905241B2 (en) * 2020-12-22 2024-02-20 Kellogg Brown & Root Llc Recovery of light olefins from dry hydrocarbon gas from refinery and petrochemical production processes for production of alkylate
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US11724972B2 (en) * 2021-12-15 2023-08-15 Uop Llc Combined process for alkylation of light olefins using ionic liquid catalysts
US11643374B1 (en) 2021-12-15 2023-05-09 Chevron U.S.A. Inc. Ionic liquid alkylation of isobutane with bio-ethylene to produce alkylate
CN115501887B (en) * 2022-08-18 2024-06-14 浙江鸿盛化工有限公司 Catalyst and preparation method and application thereof
WO2024107999A1 (en) * 2022-11-16 2024-05-23 ExxonMobil Technology and Engineering Company Heterodimers of terpenes and linear or branched alkenes
US11958046B1 (en) 2023-06-16 2024-04-16 Kellogg Brown & Root Llc Methods and systems for alkylate production involving a multi-zone alkylation reactor

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3795714A (en) 1968-06-26 1974-03-05 Union Carbide Corp Isoparaffin alkylation process and catalyst for use therein
US3893942A (en) 1973-09-27 1975-07-08 Union Carbide Corp Isoparaffin alkylation process with periodic catalyst regeneration
US5073665A (en) 1990-07-31 1991-12-17 Mobil Oil Corp. Process for alkylating olefins and isoparaffins in a fixed bed reactor
US20040158113A1 (en) 2003-02-06 2004-08-12 Girish Srinivas Catalysts and process for converting fuel gases to gasoline

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3761540A (en) * 1971-04-30 1973-09-25 Phillips Petroleum Co Alkylation of isoparaffin with ethylene and a higher olefin
US3754052A (en) 1972-01-14 1973-08-21 Sun Research Development Ethylene alkylation resulting in alkylate with high proportion of 2,3-dimethylbutane
US4211885A (en) 1979-05-15 1980-07-08 Phillips Petroleum Company High octane gasoline components from catalytic cracking gasoline, propylene, and isobutane by disproportionation, cleavage and alkylation
US5449849A (en) * 1994-04-18 1995-09-12 Mobil Oil Corporation Selectivated ZSM-035 catalyst and process for selectively converting ethene to linear butenes therewith
JP2000511107A (en) * 1996-05-29 2000-08-29 エクソン・ケミカル・パテンツ・インク Metal-containing zeolite catalyst, its preparation and use for the conversion of hydrocarbons
US6025534A (en) * 1998-04-07 2000-02-15 Bp Amoco Corporation Olefin polymerization process
US7550644B2 (en) * 2004-05-10 2009-06-23 Precision Combustion, Inc. Isobutane alkylation

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3795714A (en) 1968-06-26 1974-03-05 Union Carbide Corp Isoparaffin alkylation process and catalyst for use therein
US3893942A (en) 1973-09-27 1975-07-08 Union Carbide Corp Isoparaffin alkylation process with periodic catalyst regeneration
US5073665A (en) 1990-07-31 1991-12-17 Mobil Oil Corp. Process for alkylating olefins and isoparaffins in a fixed bed reactor
US20040158113A1 (en) 2003-02-06 2004-08-12 Girish Srinivas Catalysts and process for converting fuel gases to gasoline

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2625251A4

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US11242298B2 (en) 2012-07-09 2022-02-08 Lummus Technology Llc Natural gas processing and systems
US10183900B2 (en) 2012-12-07 2019-01-22 Siluria Technologies, Inc. Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products
US10787398B2 (en) 2012-12-07 2020-09-29 Lummus Technology Llc Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products
US11168038B2 (en) 2012-12-07 2021-11-09 Lummus Technology Llc Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products
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US11254627B2 (en) 2014-01-08 2022-02-22 Lummus Technology Llc Ethylene-to-liquids systems and methods
US10301234B2 (en) 2014-01-08 2019-05-28 Siluria Technologies, Inc. Ethylene-to-liquids systems and methods
US10894751B2 (en) 2014-01-08 2021-01-19 Lummus Technology Llc Ethylene-to-liquids systems and methods
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