Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
  • C10G45/34—Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/44—Palladium
• • 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
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
  • B01J35/391—Physical properties of the active metal ingredient
  • B01J35/394—Metal dispersion value, e.g. percentage or fraction
• • 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
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
  • B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
• • 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
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
  • B01J35/61—Surface area
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
  • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
  • C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
  • C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C7/00—Purification; Separation; Use of additives
  • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
  • C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
  • C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
  • C10G45/34—Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used
  • C10G45/40—Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
  • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
  • C07C2523/42—Platinum
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
  • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
  • C07C2523/44—Palladium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
  • C07C2523/74—Iron group metals
  • C07C2523/755—Nickel
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1088—Olefins
  • C10G2300/1092—C2-C4 olefins
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/20—C2-C4 olefins
• • 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
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

• the subject of the invention is a process for the selective hydrogenation of polyunsaturated compounds in a hydrocarbon feedstock, in particular in the C2 cut from steam cracking, in the presence of a catalyst in the form of a metal or ceramic monolith.
• monolith-shaped support can be made of ceramic materials such as alumina or silicon carbide or zirconium or cordierite.
• Monolith supports also exist with metallic materials, for example steel, stainless steel and many other types of metals.
• Ceramic and metal monoliths can take different geometric shapes and sizes. They consist of parallel channels separated from each other by thin walls. These channels can have different section shapes: rectangular, cylindrical, triangular, hexagonal and many other more complex shapes.
• the monolith supports are generally characterized by the density and the size of the channels, more specifically by the number of channels per unit of length which is called CPSI (“Channels per square inch” according to the Anglo-Saxon terminology). ). As its abbreviation indicates, it corresponds to the number of channels intercepted by a section of 1 x 1 inch (“inch” according to English terminology) or 2.54 x 2.54 cm.
• Pmat with: s: porosity or void ratio of the monolith; p m density of the monolith;
• Pmat density of the monolith material.
• Metallic or ceramic monoliths can be used in various catalytic applications, in particular in the treatment of exhaust gases (US1969/3441381, US1971/35971653) or as NO X reduction catalyst (Tomasic, V. 2007), or still in selective hydrogenation of hydrocarbon feedstocks comprising polyunsaturated compounds.
• one of the objectives of the present invention is to propose a process for the selective hydrogenation of a C2 cut from steam cracking in the presence of a catalyst in the form of a metal or ceramic monolith supporting the active phase, making it possible to obtain performances in hydrogenation in terms of selectivity at least as good, or even better, than the processes known from the state of the art.
• a catalyst comprising an active phase based on at least one group VIII metal and a support in the form of a ceramic or metallic monolith with a particular geometric structure, said active phase in the form of a layer of determined thickness on the walls of said support, makes it possible to obtain catalytic performances at least as good, or even improved in terms of selectivity when it is used in a selective hydrogenation process of a C2 steam cracking cut containing acetylene, and this by reducing even at iso conversion the catalytic volume available for the charge and while limiting the pressure drops.
• the subject of the present invention is a process for the selective hydrogenation of a C2 cut from steam cracking comprising acetylene, said process being carried out in the gaseous phase at a temperature between 0° C. and 300° C., at a pressure between 0.1 MPa and 6.0 MPa, at a hydrogen/(polyunsaturated compounds to be hydrogenated) molar ratio of between 0.5 and 1,000, and at an hourly volume rate (VVH) of between 100 h -1 and 60,000 h -1 , preferably between 500 lr 1 and 30,000 h -1 , in the presence of a catalyst comprising, preferably consisting of, an active phase based on at least one group VIII metal and a support in the form of a ceramic or metallic monolith, characterized in that said support comprises a number of channels per unit length (CPSI) between 300 and 1200, and in that the active phase is in the form of a layer on the walls of said support , the thickness of said layer of active phase being between 30 ⁇
• the Applicant has found that the use of such a catalyst, having a support in the form of a ceramic or metallic monolith, said support comprising a specific number of channels per unit length, coupled with a specific thickness of the layer of the active phase on the walls of the support, allows iso-conversion to reduce the volume of catalytic bed necessary for carrying out a selective hydrogenation reaction of a C2 cut from steam cracking comprising acetylene, while significantly improving the selectivity of the reaction towards the desired products.
• said catalyst comprises a geometric surface of between 1500 m 2 /m 3 and 5000 m 2 /m 3 .
• the thickness of the catalyst wall is between 0.08 mm and 0.5 mm.
• the degree of porosity of said catalyst is between 20 and 90%.
• the thickness of said layer of active phase is between 60 ⁇ m and 100 ⁇ m.
• the support is a metallic monolith chosen from monoliths made of steel, stainless steel (316L, 310SS), nickel, aluminium, iron, copper, nickel-chromium, nickel-chromium-aluminum, iron- chrome-aluminum, Inconel®.
• the support is a ceramic monolith chosen from monoliths made of alumina (Al2O3), silica-alumina, silicon carbide (SiC), phosphorus-alumina, magnesia (MgO), zinc oxide, oxide zirconium (ZrO 2 ), cordierite (Al 3 Mg 2 AISi50i8).
• said Group VIII metal is selected from nickel, platinum and palladium. More preferably, said Group VIII metal is palladium.
• the palladium content is between 0.005 and 2% by weight of said element relative to the total weight of the catalyst.
• the number of channels per unit length (CPSI) of said medium is between 400 and 700.
• group VIII according to the CAS classification corresponds to the metals of columns 8, 9 and 10 according to the new IUPAC classification.
• the textural and structural properties of the support and of the catalyst described below are determined by characterization methods known to those skilled in the art.
• the total pore volume and the pore distribution are determined in the present invention by nitrogen porosimetry as described in the book “Adsorption by powders and porous solids. Principles, methodology and applications” written by F. Rouquérol, J. Rouquérol and K. Sing, Academic Press, 1999.
• specific surface area is meant the BET specific surface area (SBET in m 2 /g) determined by nitrogen adsorption in accordance with the ASTM D 3663-78 standard established from the BRUNAUER-EMMETT-TELLER method described in the periodical "The Journal of American Society, 1938, 60, 309.
• the monolith supports (ceramic or metallic) are characterized by the number of channels per unit length (CPSI). It should be noted that the value of the CPSI of a catalyst comprising such a monolithic support does not change, whatever the thickness of the layer of the active phase of the catalyst.
• Group VIII metal content is measured by X-ray fluorescence.
• Monounsaturated organic compounds such as ethylene, for example, are the source of the manufacture of polymers, plastics and other value-added chemicals. These compounds are obtained from natural gas, naphtha or gas oil which have been treated by steam cracking or catalytic cracking processes. These processes are operated at high temperature and produce, in addition to the desired monounsaturated compounds, polyunsaturated organic compounds such as acetylene, or diolefinic compounds. These polyunsaturated compounds are very reactive and lead to side reactions in the polymerization units. It is therefore necessary to eliminate them before recovering these cuts. Selective hydrogenation is the main treatment developed to specifically remove unwanted polyunsaturated compounds from these hydrocarbon feedstocks. It allows the conversion of polyunsaturated compounds to the corresponding alkenes by avoiding their total saturation and therefore the formation of the corresponding alkanes.
• the present invention relates to a process for the selective hydrogenation of a C2 cut from steam cracking comprising acetylene, said process being carried out in the gas phase at a temperature between 0° C. and 300° C., at a pressure between 0.1 MPa and 6.0 MPa, at a hydrogen/(polyunsaturated compounds to be hydrogenated) molar ratio of between 0.5 and 1,000, and at an hourly volumetric velocity (VVH) of between 100 lr 1 and 60,000 h -1 , preferably between 500 lr 1 and 50,000 h -1 , in the presence of a catalyst comprising, preferably consisting of, an active phase based on at least one group VIII metal and a support in the form of a ceramic or metallic monolith, said support comprising a number of channels per unit length (CPSI) between 300 and 1200, the active phase being in the form of a layer on the walls of said support, the thickness of said phase layer active being between 30 ⁇ m and 150 ⁇ m.
• the acetylene content included in the steam cracking charge C2 is advantageously between 0.1% and 5% by weight of acetylene relative to the total weight of the charge, preferably between 0.5% and 2.5% by weight of acetylene.
• the C2 cut from steam cracking used for carrying out the selective hydrogenation process according to the invention comprises the following composition: between 40 and 95% by weight of ethylene, between 0.1 and 5% weight of acetylene, the remainder being ethane and/or methane. In some cuts C2 from steam cracking, between 0.1 and 1% by weight of C3 compounds may also be present.
• the selective hydrogenation process according to the invention aims to eliminate the acetylene in the said feed to be hydrogenated without hydrogenating the monounsaturated hydrocarbons, that is to say ethylene.
• the technological implementation of the selective hydrogenation process is for example carried out by injection, in ascending or descending current, of the charge of polyunsaturated hydrocarbons and of hydrogen into at least one fixed-bed reactor.
• Said reactor can be of the isothermal type or of the adiabatic type. An adiabatic reactor is preferred.
• the charge of polyunsaturated hydrocarbons can advantageously be diluted by one or more re-injection(s) of the effluent, from said reactor where the selective hydrogenation reaction takes place, at one or more points of the reactor, located between the inlet and outlet of the reactor in order to limit the temperature gradient in the reactor.
• the technological implementation of the selective hydrogenation process according to the invention can also be advantageously carried out by the implantation of said catalyst in a reactive distillation column or in reactor-exchangers or in a slurry type reactor.
• the hydrogen flow can be introduced at the same time as the charge to be hydrogenated and/or at one or more different points of the reactor.
• the selective hydrogenation of the C2 cut from steam cracking is carried out in the gas phase.
• the selective hydrogenation of the C2 steam cracking cut is carried out at a temperature between 0° C. and 300° C., preferably between 15° C. and 280° C., at a pressure between 0. 1 MPa and 6.0 MPa, preferably between 0.2 MPa and 5.0 MPa, at a hydrogen/(polyunsaturated compounds to be hydrogenated) molar ratio of between 0.5 and 1000, preferably between 0.7 and 800, and at an hourly volume velocity (VVH) of between 100 h 1 and 60,000 h 1 , preferably between 500 h 1 and 50,000 h 1 .
• VVH hourly volume velocity
• the catalyst used in the context of the selective hydrogenation process comprises, preferably consists of, an active phase based on at least one group VIII metal and a support in the form of a ceramic or metallic monolith, characterized in that said support comprises a number of channels per unit length (CPSI) between 300 and 1200, and in that the active phase is in the form of a layer on the walls of said support, the thickness of said active phase layer being between 30 ⁇ m and 150 ⁇ m.
• CPSI channels per unit length
• the number of channels per unit length (CPSI) of said support is between 300 and 1200, preferably between 350 and 1000, more preferably between 400 and 700, and even more preferably between 450 and 750.
• the geometric surface of said catalyst is between 1500 m 2 /m 3 and 5000 m 2 /m 3 , preferably between 1500 m 2 /m 3 and 4000 m 2 /m 3 , and even more preferably between 2000 m 2 /m 3 and 4000 m 2 /m 3 .
• the thickness of the catalyst wall is between 0.08 mm and 0.5 mm, more preferably between 0.1 mm and 0.4 mm.
• the degree of porosity of said catalyst is between 15% and 90%, preferably between 20% and 90%, and more preferably between 20% and 70%.
• the thickness of said layer of active phase is between 60 ⁇ m and 100 ⁇ m, and even more preferably between 60 ⁇ m and 90 ⁇ m.
• said monolith is preferably chosen from monoliths made of steel, stainless steel (316L, 310SS), nickel, aluminium, iron, copper, nickel-chromium, nickel-chromium -aluminum, iron-chromium-aluminum, Inconel®.
• said monolith is preferably chosen from alumina (Al2O3), silica-alumina, silicon carbide (SiC), phosphorus-alumina, magnesia (MgO) monoliths. , zinc oxide, zirconium oxide (ZrC>2), cordierite (Al 3 Mg 2 AISi50i8).
• said ceramic monolith is made of alumina (Al2O3), silica-alumina, phosphorus-alumina, or silicon carbide (SiC).
• the group VIII metal of the active phase is preferably chosen from nickel, platinum and palladium.
• the Group VIII metal is palladium.
• the palladium content is generally between 0.005 and 2% by weight of said element relative to the total weight of the catalyst, preferably between 0.01 and 2% by weight, and more preferably between 0. 05 and 1% by weight, relative to the total weight of the catalyst.
• the catalyst may also comprise, as active phase, an element from group IB, preferably chosen from silver and copper.
• group IB element is silver.
• the group IB element content is preferably between 0.01 and 0.3% by weight relative to the total weight of the catalyst, more preferably between 0.015 and 0.2% by weight.
• the deposition of the active phase of the catalyst on the support in the form of a monolith can be carried out by conventional methods well known to those skilled in the art, and is carried out in particular by coating (“washcoat” according to the English terminology). - Saxon).
• This impregnation technique is carried out by completely immersing the support in the form of a ceramic or metallic monolith in a solution containing the the precursor salts of the desired active phase(s) and then bringing out said impregnated monolith for drying in air (preferably a stream of air).
• the operation can be repeated several times.
• the catalyst precursor is generally dried at a temperature between 50°C and 550°C, more preferably between 70°C and 200°C.
• the drying time is generally between 0.5 hour and 20 hours.
• This preparation route is carried out in such a way as to obtain a layer of active phase on the walls of the support, the thickness of said layer being between 30 ⁇ m and 150 ⁇ m, preferentially between 60 ⁇ m and 100 ⁇ m, and even more preferentially between 60pm and 90pm.
• the catalyst can be used in a catalytic bed in a selective hydrogenation reactor in the form of blocks of elements of cubic or parallelepipedal shape packed on top of each other.
• the blocks of catalyst in monolithic support can have a rounded shape to properly match the shape of the reactor.
• the selective hydrogenation reactor used in the context of the process according to the invention can be equipped with a plurality of tubes filled with the catalyst as described previously.
• the tubes can have a circular, square or rectangular section.
• the wall of the tubes can be porous or non-porous.
• the maximum spacing between the tubes is between 0 and 100 mm, preferably between 0 and 20 mm.
• the height of the reaction section can be composed of several tubes connected to each other.
• the selective hydrogenation reactor used in the context of the process according to the invention can be of the reactor-exchanger type.
• the exchanger reactor is equipped with a multitude of tubes filled with the catalyst as described previously.
• the tubes can have a circular, square or rectangular section.
• a heat transfer fluid circulates to dissipate the heat generated by the exothermic reactions of selective hydrogenation.
• the direction of flow of the heat transfer fluid can be in the same direction as in the opposite direction to the flow of the load in the tubes.
• the counter-current direction remains the preferred embodiment.
• the heat transfer fluid can be a liquid or a vapor which condenses. Examples
• - catalyst B (non-compliant): a catalyst based on palladium on a support in the form of a ceramic monolith whose geometric characteristics are not in accordance with the invention (see Table 1 below);
• - catalyst C (compliant): a palladium-based catalyst on a support in the form of a monolith in accordance with the invention (see Table 1 below);
• - catalyst D (non-compliant): a catalyst based on palladium on a support in the form of a ceramic monolith whose geometric characteristics are not in accordance with the invention (see Table 1 below);
• - catalyst E (non-compliant): a catalyst based on palladium on a support in the form of a ceramic monolith whose geometric characteristics and the thickness of the active layer are not in accordance with the invention (see Table 1 below). after).
• the active phase of palladium was deposited by the coating technique at a desired concentration to obtain on the final catalyst a palladium element content of: B: 0.028% Pd, C 0.042% Pd, D : 0.054% Pd and E: 0.015% Pd by weight relative to the total weight of the catalyst.
• Table 1 gives the operating conditions considered. They are identical for the five cases studied.
• the non-compliant catalyst E although having a higher selectivity than the catalyst C according to the invention, the latter has a lower conversion (and therefore an acetylene content at the outlet of the reactor that is too high) with an increased pressure drop, which is due respectively to a too high density of channels and a low layer thickness of the active phase.
• catalyst C according to the invention makes it possible to have a compromise between selectivity for acetylene, pressure drop, and catalytic reaction volume.

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• 2020
  • 2020-12-10 FR FR2013013A patent/FR3117504B1/fr active Active
• 2021
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