WO2018020345A1 - Procédé de production d'une composition de gaz de synthèse pour l'oxosynthèse par hydrogénation à haute pression de co2 sur un catalyseur d'oxyde de chrome/aluminium usé - Google Patents

Procédé de production d'une composition de gaz de synthèse pour l'oxosynthèse par hydrogénation à haute pression de co2 sur un catalyseur d'oxyde de chrome/aluminium usé Download PDF

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WO2018020345A1
WO2018020345A1 PCT/IB2017/054155 IB2017054155W WO2018020345A1 WO 2018020345 A1 WO2018020345 A1 WO 2018020345A1 IB 2017054155 W IB2017054155 W IB 2017054155W WO 2018020345 A1 WO2018020345 A1 WO 2018020345A1
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mol
molar
mpa
reaction
synthesis
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PCT/IB2017/054155
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English (en)
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Aghaddin Mamedov
Clark Rea
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Sabic Global Technologies B.V.
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Publication of WO2018020345A1 publication Critical patent/WO2018020345A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/26—Chromium

Definitions

  • the invention generally concerns a process for hydrogenation of carbon dioxide (C0 2 ) to produce a synthesis gas (syngas) containing composition that includes hydrogen (H 2 ) and carbon monoxide (CO) in a molar ratio applicable for oxo-synthesis.
  • the process includes contacting a spent or used chromium oxide/alumina supported catalyst under high pressure conditions suitable to produce an oxo-synthesis syngas composition having a H 2 :CO molar ratio of 1.3 or less and at least 1 molar % of methane (CH 4 ).
  • Syngas (which includes carbon monoxide and hydrogen gases) is oftentimes used to produce chemicals such as methanol, tert-butyl. methyl ether, ammonia, fertilizers, 2-ethyl hexanol, formaldehyde, acetic acid, and 1,4-butane diol.
  • Syngas can be produced by common methods such as methane steam reforming technology as shown in reaction equation (1), partial oxidation of methane as shown in reaction (2), or dry reforming of methane as shown in reaction (3):
  • Equation (3) illustrates the catalyst deactivation event due to carbonization.
  • This process which is also known as a reverse water gas shift reaction, is mildly endothermic and generally takes place at temperatures of at least about 450 °C, with C0 2 conversion of 50% at temperatures between 560 °C to 580 °C.
  • methane is not detrimental to an oxo-synthesis reaction so it does not need to be removed from the syngas product stream prior to use in an oxy-synthesis reaction ⁇ e.g., a hydroformylation of olefins reaction, a carbonylation of methanol reaction, or a carbonylation of olefins reaction).
  • the discovery is premised on the use of a spent (the terms spent and used can be used interchangeably throughout the specification) supported chromium oxide/alumina catalyst under isothermal conditions of at least 550 °C, a pressure of at least 0.5 MPa, and a H 2 :C0 2 molar ratio of 1 or less.
  • a spent the terms spent and used can be used interchangeably throughout the specification
  • Such a process can surprisingly produce syngas compositions (e.g., a H 2 :CO molar ratio of 1.3 or less, preferably about 1 : 1) suitable for use as an intermediate or as feed material in the aforementioned oxo-synthesis reactions.
  • syngas compositions having higher ratios of H 2 :CO e.g., greater than 1.3
  • H 2 :CO e.g., greater than 1.3
  • the process of the present invention provides an elegant alternative to the highly endothermic process of methane steam reforming to produce syngas suitable for use in oxo-product synthesis.
  • Any unreacted C0 2 present in the produced syngas composition can be separated out (e.g., by amine adsorption) to be further used for carbonylation reactions.
  • an isothermal process for hydrogenating carbon dioxide (C0 2 ) to produce an oxo-synthesis syngas containing composition is described.
  • the process can include contacting a spent chromium oxide/alumina supported catalyst with hydrogen (H 2 ) and C0 2 at a H 2 :C0 2 molar ratio of 1 or less, a constant temperature of at least 550 °C, and a pressure of at least 0.5 MPa to produce the oxo- synthesis syngas containing composition that includes H 2 and CO at a H 2 :CO molar ratio of 1.3 or less and methane (CH 4 ) in an amount of at least 1 molar %.
  • the H 2 :C0 2 reactant feed stream can have a molar ratio from 0.2 to 1 or 0.5 to 1 and in some instances, does not contain CH 4 .
  • the reaction temperature can be from 550 °C to 650 °C or 575 °C to 625 °C and the reaction pressure can be from 0.5 MPa to 3.5 MPa or 1 MPa to 3 MPa.
  • the reaction can occur at 600 °C to 630 °C and 2.5 MPa to 3.5 MPa, and the H 2 gas flow rate in the reactant feed stream can be 40 to 60 mL/min and the C0 2 gas flow rate in the reactant feed stream can be 40 to 60 mL/min.
  • the reaction can occur at 570 °C to 590 °C and 0.5 MPa to 3.5 MPa, preferably 0.5 MPa to 1.5 MPa or 2.5 MP to 3.5 MPa and the H 2 gas flow rate in the reactant feed stream can be 30 to 60 mL/min and the C0 2 gas flow rate in the reactant feed stream can be 50 to 70 mL/min.
  • the C0 2 conversion of the process can be at least 20%.
  • the spent chromium oxide/alumina supported catalyst can include from 5 wt.% to 30 wt. % of chromium (Cr), 10 wt.% to 20 wt.
  • the supported catalyst can be a used chromium oxide/alumina catalyst that has been previously used as a catalyst for a dehydrogenation reaction and has reduced dehydrogenation catalytic activity when compared to the unused form of the catalyst.
  • the spent catalyst includes ceramic particles.
  • the spent catalyst is a mixture of ceramic particles and catalyst that includes 30 to 50 wt.% ceramic particles with the balance (e.g., 70 to 50 wt.%) being catalyst (i.e., spent chromium oxide/alumina supported catalyst).
  • the H 2 :CO molar ratio of the produced oxo-synthesis gas can be from 0.1 to 1.3, 0.5 to 1.3 or 0.8 to 1.3, preferably 1 to 1.1.
  • the amount of H 2 in the syngas composition can be from 1 to 40 molar %, 3 to 30 molar %, or 5 to 25 molar % and the amount of CO in the syngas composition can be from 5 to 30 molar %, 10 to 25 molar %, or 15 to 20 molar %.
  • the amount of CH 4 in the syngas composition can be from 1 to 15 molar %, 3 to 10 molar %, or 5 to 10 molar %.
  • the syngas composition can be 15 mol.% to 20 mol.% CO, 45 mol.% to 55 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 20 mol.% to 25 mol.%) H 2 .
  • the syngas composition further includes an amount of C0 2 from 30 to 80 molar % or 45 to 65 molar % and the syngas composition can be further processed to remove C0 2 , for example, by amine adsorption.
  • the syngas composition can be 15 mol.% to 20 mol.% CO, 60 mol.% to 65 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 10 mol.% to 20 mol.% H 2 .
  • methane is not detrimental to an oxo-synthesis reaction so removal of the methane from the reaction mixture is not needed.
  • the syngas composition can include C0 2 and the process can further include removing the C0 2 from the product stream to obtain the oxo-synthesis syngas containing composition and providing the produced oxo-synthesis syngas to a hydroformylation of olefins reaction, a carbonylation of methanol reaction, or a carbonylation of olefins reaction.
  • the terms “about” or “approximately” are defined as being close to as understood by one of ordinary skill in the art, and in one non-limiting embodiment the terms are defined to be within 10%, preferably, within 5%, more preferably, within 1%, and most preferably, within 0.5%.
  • the terms “wt.%”, “vol.%”, or “mol.%” refers to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component. In a non-limiting example, 10 moles of component in 100 moles of the material is 10 mol.% of component.
  • the term “substantially” and its variations are defined to include ranges within 10%, within 5%, within 1%, or within 0.5%.
  • the process of the present invention can "comprise,” “consist essentially of,” or “consist of particular ingredients, components, compositions, etc., disclosed throughout the specification. With respect to the transitional phase “consisting essentially of,” in one non- limiting aspect, a basic and novel characteristic of the process of the present invention is the ability to hydrogenate carbon dioxide to produce a methane containing oxy-synthesis syngas. [0020] In the context of the present invention 20 Embodiments are now described. Embodiment 1 is an isothermal process for hydrogenating carbon dioxide (C0 2 ) to produce an oxo-synthesis syngas containing composition.
  • the process includes contacting a spent chromium oxide/alumina supported catalyst with a reaction feed containing hydrogen (H 2 ) and C0 2 at a H 2 :C0 2 molar ratio of 1 or less, wherein the reaction occurs at a constant temperature of at least 550 °C and a pressure of at least 0.5 MPa to produce the oxo-synthesis syngas containing composition comprising H 2 and CO at a H 2 :CO molar ratio of 1.3 or less and methane (CH 4 ) in an amount of at least 1 molar %.
  • Embodiment 2 the process of Embodiment 1, wherein the H 2 :C0 2 molar ratio is from 0.2 to 1 or 0.5 to 1.
  • Embodiment 3 the process of any one of Embodiments 1 to 2, wherein the reaction feed does not contain CH 4 .
  • Embodiment 4 is the process of any one of Embodiments 1 to 3, wherein the reaction temperature is 550 °C to 650 °C or 575 °C to 625 °C.
  • Embodiment 5 is the process of any one of Embodiments 1 to 4, wherein the reaction pressure is from 0.5 MPa to 3.5 MPa or 1 MPa to 3 MPa.
  • Embodiment 6 is the process of any one of Embodiments 1 to 5, wherein the amount of H 2 in the syngas composition is from 1 to 40 molar %, 10 to 30 molar %, 10 to 25 molar %, or 10 to 20 molar %.
  • Embodiment 7 is the process of any one of Embodiments 1 to
  • Embodiment 8 is the process of any one of Embodiments 1 to
  • Embodiment 9 the process of any one of Embodiments 1 to 8, wherein the amount of CH 4 in the syngas composition is from 1 to 15 molar %, 3 to 10 molar %, or 5 to 10 molar %.
  • Embodiment 10 is the process of any one of Embodiments 1 to 9, further comprising providing the CH 4 containing syngas composition to an oxy-synthesis process.
  • Embodiment 11 is the process of any one of Embodiments 1 to 10, wherein the syngas composition further comprises an amount of C0 2 from 30 to 80 molar % or 45 to 65 molar %.
  • Embodiment 12 is the process of any one of Embodiments 1 to 11, wherein the chromium oxide/alumina supported catalyst contains from 5 wt.% to 30 wt. % of Cr, 10 wt.% to 20 wt. % of Cr, or 13 wt.% to 17 wt.% Cr.
  • Embodiment 13 is the process of any one of Embodiments 1 to 12, wherein the catalyst contains from 0.2 wt.% to 30 wt.%, 2 wt.% to 10 wt.%, or 2 wt.% to 5 wt.%) of at least one member selected from the group consisting of Li, K, Cs, and Sr.
  • Embodiment 14 is the process of any one of Embodiments 1 to 13, wherein the spent chromium oxide/alumina supported catalyst is a mixture of ceramic particles and spent catalyst and the mixture includes 50 to 70 wt.%> catalyst and 30 to 50 wt. %> ceramic particles, preferably about 60 wt. %> catalyst and about 40 wt. %> ceramic particles.
  • Embodiment 15 is the process of any one of Embodiments 1 to 14, wherein the C0 2 conversion is at least 20%>.
  • Embodiment 16 is the process of any one of Embodiments 1 to 15, wherein the reaction occurs at 600 °C to 630 °C and 2.5 MPa to 3.5 MPa, and wherein the H 2 gas flow rate in the reaction feed is 40 to 60 mL/min and the C0 2 gas flow rate in the reactant feed stream is 40 to 60 mL/min.
  • Embodiment 17 is the process of any one of Embodiments 1 to 16, wherein the oxy-synthesis syngas containing composition contains 15 mol.% to 20 mol.% CO, 45 mol.% to 55 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 20 mol.% to 25 mol.% H 2 .
  • Embodiment 18 is the process of any one of Embodiments 1 to 14, wherein the reaction occurs at 570 °C to 590 °C and 0.5 MPa to 3.5 MPa, preferably 0.5 MPa to 1.5 MPa, and wherein the H 2 gas flow rate in the reaction feed is 30 to 50 mL/min and the C0 2 gas flow rate in the reactant feed stream is 50 to 70 mL/min.
  • Embodiment 19 is the process of any one of Embodiments 1 to 18, wherein the oxy-synthesis syngas containing composition comprises 15 mol.% to 20 mol.% CO, 60 mol.% to 65 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 10 mol.% to 20 mol.% H 2 .
  • Embodiment 20 is the process of any one of Embodiments 1 to 19, wherein the oxy-synthesis syngas containing composition further includes C0 2 and wherein the process further includes the steps of removing the C0 2 from the oxo-synthesis syngas containing composition; and providing the oxo-synthesis syngas containing composition to a hydroformylation of olefins reaction, a carbonylation of methanol reaction, or a carbonylation of olefins reaction.
  • FIG. 1 is an illustration of a process of the present invention to produce oxo- synthesis syngas that includes methane using a combined C0 2 and H 2 containing reactant feed gas and the spent chromium oxide/alumina supported catalyst of the present invention.
  • FIG. 2 is an illustration of a process of the present invention to produce oxy- synthesis syngas that includes methane using a H 2 reactant feed gas source, a C0 2 reactant feed gas source, and the spent chromium oxide/alumina supported catalyst of the present invention.
  • the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawings. The drawings may not be to scale.
  • the discovery is premised on the use of a spent or used chromium oxide/alumina supported catalyst in the hydrogenation of carbon dioxide reaction using a H 2 :C0 2 molar ratio of 1 or less.
  • the described process results in the production of an oxo- synthesis syngas composition having a H 2 :CO molar ratio of 1.3 or less and at least 1 molar % of methane (CH 4 ) at elevated temperatures and pressures.
  • results can be achieved at isothermal processing conditions of at least 550 °C, preferably 550 °C to 650 °C or 575 °C to 625 °C, and at least 0.5 MPa, preferably from 0.5 MPa to 3.5 MPa, or 1 MPa to 3 MPa.
  • the oxo-synthesis syngas composition can have characteristics that make it acceptable for oxo-synthesis reactions, such as hydroformylation.
  • Conditions sufficient to produce oxo-synthesis syngas from the hydrogenation of C0 2 reaction include temperature, time, flow rate of feed gases, and pressure.
  • the temperature range for the hydrogenation reaction can be at least 550 °C, 550 °C to 650 °C, or 575 °C to 625 °C and all ranges and temperatures there between (e.g., 580 °C, 585 °C, 590 °C, 595 °C, 600 °C, 605 °C, 610 °C, 615 °C, 620 °C, or 625 °C).
  • the average pressure for the hydrogenation reaction can range from at least 0.5 MPa, 0.5 MPa to 3.5 MPa, 1 MPa to 3 MPa, and all pressures there between (e.g., 1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2, 2.1, 2.2, 2.3, 2.4, 2.5, 2.6, 2.7, 2.8, 2.9, 3, 3.1, 3.2, 3.3, 3.4, or 3.5 MPa).
  • the upper limit on pressure can be determined by the reactor used.
  • the conditions for the hydrogenation of C0 2 to syngas can be varied based on the type of the reactor used.
  • the combined flow rate for the for the reactants (e.g., combination of the H 2 and C0 2 flow rate) in hydrogenation reaction can range from at least 70 to 130 mL/min, 80 mL/min to 1 10 mL/min, 90 mL/min to 105 mL/ min or all ranges and values there between (e.g., at least 70 mL/min, 71 mL/min, 72 mL/min, 73 mL/min, 74 mL/min, 75 mL/min, 76 mL/min, 77 mL/min, 78 mL/min, 79 mL/min, 80 mL/min, 81 mL/min, 82 mL/min, 83 mL/min, 84 mL/min, 85 mL/min, 86 mL/min, 87 mL/min, 88 mL/min, 89 mL/min, 90 mL/
  • the H 2 gas flow rate can range from 30 mL/min to 70 mL/min or any range or value there between (e.g., 31 mL/min, 32 mL/min, 33 mL/min, 34 mL/min, 35 mL/min, 36 mL/min, 37 mL/min, 38 mL/min, 39 mL/min, 40 mL/min, 41 mL/min, 42 mL/min, 43 mL/min, 44 mL/min, 45 mL/min, 46 mL/min, 47 mL/min, 48 mL/min, 49 mL/min, 50 mL/min, 51 mL/min, 52 mL/min, 53 mL/min, 54 mL/min, 55 mL/min, 56 mL/min, 57 mL/min, 58 mL/min, 59 mL/min, 60 mL/min, 61
  • the C0 2 flow rate can range from 30 mL/min to 70 mL/min or any range or value there between (e.g., 31 mL/min, 32 mL/min, 33 mL/min, 34 mL/min, 35 mL/min, 36 mL/min, 37 mL/min, 38 mL/min, 39 mL/min, 40 mL/min, 41 mL/min, 42 mL/min, 43 mL/min, 44 mL/min, 45 mL/min, 46 mL/min, 47 mL/min, 48 mL/min, 49 mL/min, 50 mL/min, 51 mL/min, 52 mL/min, 53 mL/min, 54 mL/min, 55 mL/min, 56 mL/min, 57 mL/min, 58 mL/min, 59 mL/min, 60 mL/min, 61 mL/
  • the reaction can be carried out over the spent chromium oxide/alumina supported catalyst of the current invention having particular oxo-synthesis syngas selectivity and conversion results. Therefore, in one aspect, the reaction can be performed with a C0 2 conversion of at least 10 mol.%, at least 20 mol.%, at least 30 mol.%, at least 50 mol.%, at least 60 mol.%, at least 70 mol.%, at least 80 mol.%, or at least 99 mol.%).
  • the method can further include collecting or storing the produced oxo-synthesis syngas along with using the produced oxo-synthesis syngas as a feed source, solvent, or a commercial product in oxo-synthesis reactions.
  • Non-limiting examples of oxo-synthesis reactions include hydroformylation of olefins, carbonylation of methanol, or carbonylation of olefins.
  • the catalyst Prior to use, the catalyst can be subjected to reducing conditions to convert the spent chromium oxide and the other metals in the catalyst to a lower valance state or the metallic form.
  • a non-limiting example of reducing conditions includes flowing a gaseous stream that includes a hydrogen gas or a hydrogen gas containing mixture (e.g., a H 2 and argon gas stream) at a temperature of 500 °C to 700 °C for a period of time (e.g., 1 to 8 hours) under atmospheric pressure over the catalyst.
  • a system 100 which can be used to convert a reactant gas stream of carbon dioxide (C0 2 ) and hydrogen (H 2 ) into syngas using the spent chromium oxide/alumina supported catalyst of the present invention.
  • the produced syngas can be suitable for oxo-synthesis reactions.
  • the system 100 can include a combined reactant gas source 102, a reactor 104, and a collection device 106.
  • the combined reactant gas source 102 can be configured to be in fluid communication with the reactor 104 via an inlet 108 on the reactor.
  • the combined reactant gas source 102 can be configured such that it regulates the amount of reactant feed (e.g., C0 2 and H 2 ) entering the reactor 104.
  • FIG. 2 depicts a system 200 for the process of the present invention having two feed inlets.
  • a hydrogen gas reactant feed source 202 and a carbon dioxide reactant gas feed source 204 are in fluid communication with reactor 104 via hydrogen gas inlet 206 and carbon dioxide gas inlet 208, respectively.
  • the reactor 104 can include a reaction zone 1 10 having the spent chromium oxide/alumina supported catalyst 1 12 of the present invention.
  • the reactor can include various automated and/or manual controllers, valves, heat exchangers, gauges, etc., for the operation of the reactor.
  • the reactor can have insulation and/or heat exchangers to heat or cool the reactor as desired.
  • the amounts of the reactant feed and the spent chromium oxide/alumina catalyst 1 12 used can be modified as desired to achieve a given amount of product produced by the systems 100 or 200.
  • a continuous flow reactor can be used.
  • Non- limiting examples of continuous flow reactors include fixed-bed reactors, fluidized reactors, bubbling bed reactors, slurry reactors, rotating kiln reactors, moving bed reactors or any combinations thereof when two or more reactors are used.
  • the reactor can be made of materials that are corrosion and/or oxidation resistant.
  • the reactor can be lined with, or made from Inconel, or be a quartz reactor.
  • the reactant gas is preheated prior to being fed to the reactor.
  • reaction zone 1 10 is a multi-zone reactor with different stages of heating in each zone.
  • the reactor 104 can include an outlet 1 14 configured to be in fluid communication with the reaction zone 1 10 and configured to remove a first product stream comprising oxo-synthesis syngas from the reaction zone.
  • Reaction zone 1 10 can further include the reactant feed and the first product stream.
  • the products produced can include hydrogen and carbon monoxide.
  • the product stream can also include unreacted carbon dioxide, water, and at least 1 molar % of alkanes (e.g., methane).
  • the spent catalyst can be included in the product stream.
  • the collection device 106 can be in fluid communication with the reactor 104 via the product outlet 1 14. Reactant gas inlets 108, 206, and 208, and the outlet 1 14 can be opened and closed as desired.
  • the collection device 106 can be configured to store, further process, or transfer desired reaction products (e.g., oxo-synthesis syngas) for other uses.
  • collection device 106 can be a separation unit or a series of separation units that are capable of separating the gaseous components from each other (e.g., separate C0 2 or water from the stream). Water can be removed from the product stream with any suitable method known in the art (e.g., condensation, liquid/gas separation, etc.).
  • C0 2 can be removed or scrubbed from the product stream with any suitable method known in the art (e.g., physical absorption, chemical absorption, adsorption, membrane or supercritical technologies, etc.).
  • a preferred method of removing C0 2 can be adsorption, such as an amine-based chemical adsorbent, an amine-impregnated adsorbent, or an amine-grafted adsorbent.
  • any unreacted reactant gas can be recycled and included in the reactant feed to maximize the overall conversion of C0 2 to oxo-synthesis syngas.
  • This increases the efficiency and commercial value of the C0 2 to oxo-synthesis syngas conversion process of the present invention.
  • the resulting oxo-synthesis syngas can be sold, stored, or used in other processing units (e.g., hydroformylation processing unit to produce C 2 + alcohols) as a feed source.
  • the systems 100 or 200 can also include a heating/cooling source (not shown).
  • the heating/cooling source can be configured to heat or cool the reaction zone 1 10 to a temperature sufficient (e.g., at least 550 °C) to convert C0 2 in the reactant feed to oxo-synthesis syngas via hydrogenation.
  • a heating/cooling source can be a temperature controlled furnace or an external, electrical heating block, heating coils, or a heat exchanger.
  • the catalyst used in the process according to the invention is a used or spent catalyst.
  • Used or spent catalysts in the context of the present invention can refer to a chromium oxide supported catalyst that has been used in an alkane dehydrogenation process, for example a propane or z ' so-butane dehydrogenation process. Such specific catalysts can be referred to herein as a used or spent dehydrogenation catalyst.
  • the spent catalyst has not been regenerated prior to being used in the processes of the present invention.
  • the spent catalyst can include chromium (Cr) as the catalytic active metal.
  • the chromium can be in the form of one or more oxides (e.g., Cr 2 0 3 , Cr0 2 , and/or CrO) on a metal oxide support (e.g., alumina, A1 2 0 3 ).
  • the catalyst can also include a promotor (e.g., alkali metal, alkaline earth metals, or both), a binder material, or usual impurities, as known to the skilled person.
  • the chromium (Cr) content of the spent catalyst can be 5 to 30 wt.%, 10 to 20 wt.%), or 13 to 17 wt. %, or any range or value there between (e.g., 5 wt.%, 6 wt.%, 7 wt.%, 8 wt.%, 9 wt.%, 10 wt.%, 1 1 wt.%, 12 wt.%, 13 wt.%, 14 wt.%, 15 wt.%, 16 wt.%, 17 wt.%, 18 wt.%, 19 wt.%, 20 wt.%, 21 wt.%, 22 wt.%, 23 wt.%, 24 wt.%, 25 wt.%, 26 wt.%, 27 wt.%, 28 wt.%, 29 wt.%, or 30 wt.%)
  • the spent catalyst can also include at least one alkali metal (Column 1 of the Periodic Table) or alkaline earth metal (Column 2 of the Periodic Table) as a promoter.
  • alkali metal include lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), or any combination thereof.
  • alkaline earth metals include magnesium (Mg), calcium (Ca), strontium (Sr), and barium (Ba).
  • the alkali metal or alkaline earth metal content can be 0.2 to 30 wt.%, 2 to 10 wt.%, or 2 to 5 wt.
  • % or any range or value there between (e.g., 0.2 wt.%, 0.3 wt.%, 0.4 wt.%, 0.5 wt.%, 0.6 wt.%, 0.7 wt.%, 0.8 wt.%, 0.9 wt.%, 1.0 wt.%, 1 wt.%, 2 wt.%, 3 wt.%, 4 wt.%, 5 wt.%, 6 wt.%, 7 wt.%, 8 wt.%, 9 wt.%, 10 wt.%, 1 1 wt.%, 12 wt.%, 13 wt.%, 14 wt.%, 15 wt.%, 16 wt.%, 17 wt.%, 18 wt.%, 19 wt.%, 20 wt.%, 21 wt.%, 22 wt.%, 23 wt.%, 24 wt.
  • the promoter can be Li, K, Cs, Sr, or any combination thereof.
  • an alkali metal or alkaline earth metal can suppress coke formation and/or methanation reactions, thereby improving the catalyst stability/life-time and reducing the amount of unwanted by-products.
  • the spent catalyst used in the process according to the invention can have alumina as carrier or support material. Without wishing to be bound to any theory, it is believed that chemical interactions between chromium and alumina lead to structural properties (e.g., spinel type structures) that enhance catalytic performance in the targeted reaction. In some instances, the spent catalyst has a surface area of at least 50 m 2 /g.
  • the spent catalyst composition according to the invention may further contain an inert binder or support material other than alumina (e.g., silica or titanium oxides).
  • an inert binder or support material other than alumina e.g., silica or titanium oxides.
  • the catalyst that is used in the process of the invention may be prepared by any conventional catalyst synthesis method as known in the art.
  • the catalyst can be prepared by making aqueous solutions of the desired metal components, for example from their nitrate or other soluble salt, mixing the solutions with alumina, forming a solid catalyst precursor by precipitation (or impregnation) followed by removing water and drying, and then calcining the precursor composition by a thermal treatment in the presence of oxygen.
  • the catalyst may be applied in the process of the invention in various geometric forms, for example as spherical pellets.
  • Non-limiting examples of chromium oxide/alumina supported catalysts that can be used in dehydrogenation reactions include the CATOFIN® catalysts (Clariant, U.S.A.). After being used in a dehydrogenation reaction, the used catalyst typically has low residual activity for such reaction. The low catalytic activity is most likely due to deactivation caused by coke formation. Coke deposition on the spent catalyst is generally thought to result in a change in physical properties of the catalyst particles, like a lower surface area and increased pore size; and the resulting decreased activity of the dehydrogenation catalyst cannot be increased again by a regeneration process. Regeneration with oxygen can remove coke, but will not restore the original structure.
  • Such a used catalyst therefore has typically been disposed of after its use in alkane dehydrogenation reactions. It is therefore a great advantage and highly surprising that such a spent/used dehydrogenation catalyst can be used in the process according to the invention, and that this process can be operated during prolonged times with good stability.
  • the spent catalyst can include ceramic particles.
  • the spent catalyst can be a mixture of ceramic particles and spent chromium oxide supported catalyst.
  • the spent catalyst includes 50 to 70 wt.% spent chromium oxide supported catalyst, including all values there between (e.g.
  • the spent catalyst includes about 60 wt. % spent catalyst and about 40 wt. % ceramic particles.
  • Carbon dioxide gas and hydrogen gas can be obtained from various sources.
  • the carbon dioxide can be obtained from a waste or recycle gas stream (e.g., from a plant on the same site such as from ammonia synthesis, or a reverse water gas shift reaction) or after recovering the carbon dioxide from a gas stream.
  • a benefit of recycling carbon dioxide as a starting material in the process of the invention is that it can reduce the amount of carbon dioxide emitted to the atmosphere (e.g., from a chemical production site).
  • the hydrogen can be from various sources, including streams coming from other chemical processes, like water splitting (e.g., photocatalysis, electrolysis, or the like), additional syngas production, ethane cracking, methanol synthesis, or conversion of methane to aromatics.
  • the molar ratio of H 2 :C0 2 in the reactant stream can be 1 or less. In some embodiments, the H 2 :C0 2 molar ratio can be from 0.1 : 1 to 0.9: 1, from 0.2: 1 to 0.8: 1, or 0.4: 1 to 0.7: 1.
  • the volume ratio of H 2 :C0 2 reactant gas for the hydrogenation reaction can range from 0.2: 1 to 0.8: 1, from 0.3 : 1 to 0.7: 1.
  • the reactant gas stream includes 20 to 60 vol.% H 2 and 50 to 75 vol.% C0 2 , or 25 to 55 vol.% H 2 , and 55 to 70 vol.% C0 2 , preferably, 40 vol.% H 2 and 60 vol.% C0 2 or 50 vol.% H 2 and 50 vol.% C0 2 .
  • the streams are not combined.
  • the hydrogen and carbon dioxide can be delivered at the same H 2 :C0 2 ratios and volume percentages such as those discussed above for a combined reactant stream.
  • the remainder of the reactant gas stream can include another gas or gases provided the gas or gases are inert, such as argon (Ar), nitrogen (N 2 ), or methane and further provided that they do not negatively affect the reaction. All possible percentages of C0 2 plus H 2 plus inert gas in the current embodiments can have the described H 2 :C0 2 ratios herein.
  • the reactant mixture is highly pure and substantially devoid of water or steam.
  • the carbon dioxide can be dried prior to use (e.g., pass through a drying media) or contain a minimal amount of water or no water at all.
  • the process of the present invention can produce a product stream that includes a mixture of H 2 and CO having a molar H 2 :CO ratio suitable as an intermediate or as feed material in a subsequent synthesis to form a chemical product or a plurality of chemical products.
  • Non-limiting examples of synthesis include methanol production, olefin synthesis, aromatics production, hydroformylation of olefins, carbonylation of methanol, and carbonylation of olefins.
  • Non-limiting examples of products that can be produced include aliphatic oxygenates, methanol, olefin synthesis, aromatics production, carbonylation of methanol, carbonylation of olefins, or reduction of iron oxide in steel production.
  • the oxo-synthesis syngas composition is used in the hydroformylation of olefins (e.g., production of C 2 + alcohols, ethers, and the like).
  • the molar H 2 :CO ratio can be about 0.1 to 1.3, 0.5 to 1.3, 0.8 to 1.3, or 1 to 1.1, which is suitable for oxo-synthesis to avoid over-hydrogenation.
  • the amount of H 2 in the syngas composition can be from 1 to 40 molar %, 10 to 30 molar %, or 10 to 25 molar % and the amount of CO in the syngas composition can be from 5 to 30 molar %, 10 to 25 molar %, or 15 to 20 molar %.
  • a purge gas from the oxo-synthesis reaction containing hydrogen and carbon dioxide, is recycled back to the carbon dioxide hydrogenation step.
  • the C0 2 can be removed (e.g., by amine adsorption).
  • the amount of alkane (e.g., methane) produced in the process of the present reaction can be at least 1 molar %, 1 to 15 molar %, 3 to 10 molar %, or 5 to 10 molar % based on the total moles of components in the product stream.
  • the product stream can include 15 mol.% to 20 mol.% CO, 45 mol.% to 55 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 20 mol.% to 25 mol.% H 2 .
  • the product stream can include 15 mol.% to 20 mol.% CO, 60 mol.% to 65 mol.% C0 2 , 5 mol.% to 10 mol.% CH 4 , and 10 mol.% to 20 mol.% H 2 .
  • Catofin® for dehydrogenation of propane or iso-butane
  • Catofin® catalyst had been previously used in a dehydrogenation reaction and had not been regenerated. It had reduced dehydrogenation catalytic activity when compared to the unused form of the catalyst.
  • This spent catalyst used was 20-50 mesh and contains about 13 wt.% of Cr.
  • Catalyst testing was performed in a high throughput metal reactor system.
  • the reactors are fixed bed type reactor with a 2.5 cm inner diameter and 40 cm in length. Gas flow rates were regulated using two mass flow controllers. Reactor pressure was maintained by using a back pressure regulator. The reactor temperature was maintained by an external, electrical heating block. The effluent of the reactors was connected to a gas chromatograph for online gas analysis using a molecular sieve and Hayesep D column and thermal conductivity detector (TCD). The catalyst (3 mL) was placed on top of inert material inside the reactor. Prior to the reaction test, the catalyst was reduced at 600 °C under 25 vol.% H 2 in Ar for 2 h.
  • C0 2 conversion was calculated by the following formula.
  • C0 2 conversion, % mol (%CO + %CH 4 ) / (%CO + %CH 4 + %C0 2 ) (8) which presents the reactions of equations (5) and (7) discussed above
  • equation (8) presents the sum of all carbon, products divided by the total number of carbons.
  • Example 1 The general procedure of Example 1 was followed with the following conditions: a pressure of 2.8 MPa, a temperature of 620 °C, a H 2 flow rate of 50 cubic centimeter (cc)/min, and a C0 2 flow rate of 50 cc/min.
  • Time on stream (TOS) Time on stream
  • molar percentage of components in the product stream and percent (%) carbon dioxide conversion and results are listed in Table 1.
  • Example 2 The general procedure of Example 1 was followed using the following conditions: a pressure of 2.8 MPa, a temperature of 580 °C, a H 2 flow rate of 40 cc/min, and a C0 2 flow rate of 60 cc/min. Results are listed in Table 2.
  • Example 1 The general procedure of Example 1 was followed using the following conditions: a pressure of 1 MPa, a temperature of 580 °C, a H 2 flow rate of 40 cc/min and a C0 2 flow rate of 60 cc/min. Results are listed in Table 3.
  • the hydrogenation of C0 2 at high pressure provides a product gas stream composition that contains H 2 , CO, CH 4 , and C0 2 , with a H 2 :CO molar ratio of 1.3 or less and CH 4 in an amount of at least 1 molar %, which is suitable for use in production of oxo-synthesis reactions (e.g., hydroformylation of olefins, carbonylation of methanol, and carbonylation of olefins).
  • oxo-synthesis reactions e.g., hydroformylation of olefins, carbonylation of methanol, and carbonylation of olefins.
  • CH 4 can remain in the product gas stream but C0 2 is first removed from the product gas stream for oxo-synthesis reactions.

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Abstract

L'invention concerne des procédés et des catalyseurs pour l'hydrogénation de dioxyde de carbone pour produire une composition contenant un gaz de synthèse pour l'oxosynthèse. Les procédés comprennent la mise en contact d'un catalyseur supporté à base d'oxyde de chrome/alumine usé avec de l'hydrogène (H2) et CO2 à une température constante et à une pression élevée pour produire la composition contenant un gaz de synthèse pour l'oxosynthèse ayant un H2: un rapport molaire de 1,3 de CO ou moins et du méthane (CH4) dans une quantité d'au moins 1% molaire.
PCT/IB2017/054155 2016-07-25 2017-07-10 Procédé de production d'une composition de gaz de synthèse pour l'oxosynthèse par hydrogénation à haute pression de co2 sur un catalyseur d'oxyde de chrome/aluminium usé WO2018020345A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115716781A (zh) * 2022-10-27 2023-02-28 万华化学集团股份有限公司 一种丙烷脱氢耦合羰基合成制备丁醛的工艺

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060004241A1 (en) * 2002-08-16 2006-01-05 Schindler Gotz P Isothermal method for the dehydrogenating alkanes
US20100105962A1 (en) * 2007-06-25 2010-04-29 Saudi Basic Industries Corporation Catalytic hydrogenation of carbon dioxide into syngas mixture
US20130150466A1 (en) * 2011-12-08 2013-06-13 Saudi Basic Industries Corporation, Riyadh (Sa) Mixed oxide based catalyst for the conversion of carbon dioxide to syngas and method of preparation and use
US8551434B1 (en) * 2012-06-29 2013-10-08 Saudi Basic Industries Corporation Method of forming a syngas mixture
US20140316016A1 (en) * 2011-11-25 2014-10-23 Air Fuel Synthesis Limited Conversion of Carbon Dioxide to Hydrocarbons Via Hydrogenation
WO2015069840A1 (fr) * 2013-11-11 2015-05-14 Saudi Basic Industries Corporation Procédé pour l'hydrogénation du co2 dans des réacteurs métalliques adiabatiques
WO2015103592A1 (fr) * 2014-01-06 2015-07-09 Saudi Basic Industries Corporation Procédé d'hydrogénation du dioxyde de carbone d'un gaz de synthèse

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060004241A1 (en) * 2002-08-16 2006-01-05 Schindler Gotz P Isothermal method for the dehydrogenating alkanes
US20100105962A1 (en) * 2007-06-25 2010-04-29 Saudi Basic Industries Corporation Catalytic hydrogenation of carbon dioxide into syngas mixture
US20140316016A1 (en) * 2011-11-25 2014-10-23 Air Fuel Synthesis Limited Conversion of Carbon Dioxide to Hydrocarbons Via Hydrogenation
US20130150466A1 (en) * 2011-12-08 2013-06-13 Saudi Basic Industries Corporation, Riyadh (Sa) Mixed oxide based catalyst for the conversion of carbon dioxide to syngas and method of preparation and use
US8551434B1 (en) * 2012-06-29 2013-10-08 Saudi Basic Industries Corporation Method of forming a syngas mixture
WO2014003817A1 (fr) * 2012-06-29 2014-01-03 Saudi Basic Industries Corporation Procédé de formation d'un mélange de gaz de synthèse
WO2015069840A1 (fr) * 2013-11-11 2015-05-14 Saudi Basic Industries Corporation Procédé pour l'hydrogénation du co2 dans des réacteurs métalliques adiabatiques
WO2015103592A1 (fr) * 2014-01-06 2015-07-09 Saudi Basic Industries Corporation Procédé d'hydrogénation du dioxyde de carbone d'un gaz de synthèse

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115716781A (zh) * 2022-10-27 2023-02-28 万华化学集团股份有限公司 一种丙烷脱氢耦合羰基合成制备丁醛的工艺

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