US20170015912A1 - Process for treating a hydrocarbon feed - Google Patents

Process for treating a hydrocarbon feed Download PDF

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Publication number
US20170015912A1
US20170015912A1 US15/209,820 US201615209820A US2017015912A1 US 20170015912 A1 US20170015912 A1 US 20170015912A1 US 201615209820 A US201615209820 A US 201615209820A US 2017015912 A1 US2017015912 A1 US 2017015912A1
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liquid
gaseous
recontacting
carried out
effluent
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Alexandre Pagot
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IFP Energies Nouvelles IFPEN
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    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/22—Non-catalytic cracking in the presence of hydrogen
    • 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
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/22—Separation of effluents
    • 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/42—Refining of petroleum waxes
    • C10G73/44—Refining of petroleum waxes in the presence of hydrogen or hydrogen-generating compounds
    • 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
    • C10G2300/1037—Hydrocarbon fractions
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4081—Recycling aspects
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/42—Hydrogen of special source or of special composition
    • 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
    • C10G2400/28—Propane and butane

Definitions

  • the present invention relates to the field of the treatment of effluents from units for the conversion or refining of petroleum or petrochemicals which comprise hydrogen as well as hydrocarbons such as: methane, ethane, propane, butane, hydrocarbon fractions containing 5 to 11 carbon atoms (denoted C 5 -C 11 ), and optionally heavier hydrocarbons such as hydrocarbons containing in the range 12 to 30 carbon atoms (C 12 -C 30 ) or more, usually in small quantities.
  • hydrocarbons such as: methane, ethane, propane, butane, hydrocarbon fractions containing 5 to 11 carbon atoms (denoted C 5 -C 11 ), and optionally heavier hydrocarbons such as hydrocarbons containing in the range 12 to 30 carbon atoms (C 12 -C 30 ) or more, usually in small quantities.
  • an effluent from catalytic reforming or from aromatization of fractions with a distillation range in the gasoline range which can be used to provide an aromatic reformate, a hydrogen-rich gas and a liquefied petroleum gas (or “LPG”) essentially comprising hydrocarbons containing three or four carbon atoms (propane and/or propylene and/or butane and/or butenes and/or butadiene, and mixtures thereof).
  • LPG liquefied petroleum gas
  • the invention is also applicable to dehydrogenation effluents, for example butane, or pentane, or higher hydrocarbons, for example fractions essentially comprising hydrocarbons containing 10 to 14 carbon atoms, the olefins of which are used downstream for the production of linear alkylbenzenes.
  • the process in accordance with the invention may also be applicable to the hydrotreatment (and/or hydrodesulphurization and/or hydrodemetallization and/or total or selective hydrogenation) of all hydrocarbon cuts such as naphtha, gasoline, kerosene, light gas oil, heavy gas oil, vacuum distillate, or vacuum residue. More generally, it is applicable to any effluent comprising hydrogen, light hydrocarbons (methane and/or ethane), C 3 and C 4 hydrocarbons as well as heavier hydrocarbons.
  • the document FR 2 873 710 is also known, which describes a process for the treatment of a hydrocarbon feed comprising a liquid hydrocarbon phase and a hydrogen-rich gaseous phase, in which:
  • step b) the liquid obtained from step b) is then fractionated to obtain at least: a stabilized liquid which is substantially free of LPG and lighter products, a light liquid effluent essentially comprising LPG and a gaseous stream which is recycled at least in part,
  • step d) in which at least one of the gaseous streams obtained from step a) or step c) is brought into counter-current contact with a non-stabilized liquid obtained from steps a) or b).
  • the non-stabilized liquid is then supercooled to at least 10° C. below its bubble point at the contact pressure.
  • stabilized for a reformate (or another stabilized liquid in accordance with the invention denotes a reformate (or other liquid) which has been distilled in order to eliminate the major portion, and generally substantially all of the compounds containing 4 carbon atoms or fewer (C 4 ⁇ ).
  • One aim of the invention is to provide an alternative process that can be used to maximize the recovery of hydrogen and C 3 and C 4 hydrocarbons.
  • the present invention concerns a process for the treatment of a hydrocarbon feed containing hydrogen and hydrocarbons including C 1 to C 4 hydrocarbons, in which:
  • the hydrocarbon feed is separated into a gaseous phase and a liquid phase containing hydrocarbons ( 4 );
  • a first recontacting step is carried out by bringing the liquid phase into contact with a gaseous phase obtained from step c) at a temperature in the range ⁇ 20° C. to 60° C., then the recontacting mixture is separated into a first gaseous effluent which is rich in hydrogen and a first liquid hydrocarbon effluent;
  • a second recontacting step is carried out by bringing the first liquid hydrocarbon effluent into contact with the gaseous phase obtained from step a) and a recycle gas obtained from step f) at a temperature in the range ⁇ 20° C. to 60° C., then the recontacting mixture is separated into a second gaseous effluent and a second liquid hydrocarbon effluent;
  • the second liquid hydrocarbon effluent obtained from step d) is fractionated in a fractionation column in a manner such as to separate a gaseous overhead fraction and a liquid bottom fraction containing hydrocarbons containing more than 4 carbon atoms;
  • step f) the gaseous overhead fraction obtained from step e) is condensed and a liquid phase containing mainly C 3 and C 4 hydrocarbons and a gaseous phase are separated and said gaseous phase is recycled to step c),
  • step b) or step c) is carried out in a column in which the gaseous and liquid streams are brought into counter-current contact.
  • the inventors have established that a process employing two recontacting steps in which the liquid and gaseous phases move in counter-directions between the two recontacting steps and in which one of the recontacting steps is operated in a recontacting (or absorption) column with counter-current movement of the liquid and gaseous phases in the column, improves the recovery of hydrogen and C 3 and C 4 hydrocarbons (the cut known as the LPG cut) contained in the treated hydrocarbon feed and thus a hydrogen-rich gas with an increased purity can be provided.
  • the cut known as the LPG cut the cut known as the LPG cut
  • recontacting denotes an operation which can be used to extract compounds contained in a gaseous phase by means of a liquid phase which has an absorption capacity, by bringing the two phases into contact.
  • recontacting may be carried out by bringing about direct contact by in-line mixing of liquid and gaseous phases, or in a recontacting device dedicated for said unitary operation.
  • step b) is carried out in a recontacting column in which the liquid phase is brought into counter-current contact with the gaseous phase and step c) comprises in-line contact and a separation which is carried out using a separator drum.
  • step c) is carried out in a recontacting column in which the first liquid hydrocarbon effluent is brought into counter-current contact with the gaseous phase obtained from step a) and the recycle gas obtained from step f) and step b) comprises in-line contact and a separation which is carried out using a separator drum.
  • steps b) and c) are carried out in a column in which the gaseous and liquid streams are brought into counter-current contact.
  • step b contact is carried out at a pressure in the range 1.5 to 4.5 MPa.
  • step c contact is carried out at a pressure in the range 0.8 to 3 MPa.
  • step b) is carried out at a temperature in the range ⁇ 10° C. to 10° C.
  • This embodiment generally employs a cooling device such as a refrigeration device.
  • step c) is carried out at a temperature in the range 20° C. to 50° C.
  • FIG. 1 is a flow diagram of a process in accordance with the prior art
  • FIG. 2 is a flow diagram of a process in accordance with the invention, in accordance with a first embodiment
  • FIG. 3 is a flow diagram of a process in accordance with the invention, in accordance with a second embodiment
  • FIG. 4 is a flow diagram of a process in accordance with the inverse in accordance with a third embodiment.
  • the hydrocarbon feed which is treated by the process is, for example, an effluent from a catalytic reforming unit, dehydrogenation effluents, for example butane or pentane, or higher hydrocarbons, for example fractions essentially comprising hydrocarbons containing 10 to 14 carbon atoms, the olefins of which are used downstream for the manufacture of linear alkylbenzenes (generally termed LAB).
  • LAB linear alkylbenzenes
  • the process in accordance with the invention may also be applied to effluents from hydrotreatment units (hydrodesulphurization, hydrodemetallization, total or selective hydrogenation) of any hydrocarbon cuts such as naphtha, gasoline, kerosene, light gas oil, heavy gas oil, vacuum distillate, or vacuum residue. More generally, it is applicable to any effluent comprising hydrogen, light hydrocarbons (methane and/or ethane), LPGs (propane and/or butane) as well as heavier hydrocarbons.
  • the process in accordance with the invention can be used to treat effluents obtained from catalytic reforming units.
  • FIG. 1 shows a flow diagram of a process for the treatment of a hydrocarbon feed in accordance with the prior art.
  • the feed containing a gaseous phase comprising hydrogen and a hydrocarbon phase including C 1 , C 2 , C 3 and C 4 hydrocarbons is sent via the line 1 to a gas-liquid separation device 2 which may be a gas-liquid separator drum which is known to the person skilled in the art.
  • the separation device 2 allows the recovery of a gaseous phase 3 and a liquid hydrocarbon phase 4 , respectively from the head and bottom of said device 2 .
  • the gaseous overhead phase 3 which mainly contains hydrogen and light C 1 , C 2 , C 3 and C 4 hydrocarbons, may be divided into two streams 5 and 6 .
  • the stream 5 is recycled to a reaction unit located upstream, for example a catalytic reforming unit, as a recycle gas.
  • the stream 6 of gas is compressed using a compressor 7 to a pressure in the range 0.8 to 3 MPa.
  • the gas 6 is sent to a separation drum in order to separate any traces of liquid hydrocarbons before being compressed.
  • the liquid hydrocarbon phase 4 obtained from the separator drum 2 undergoes a first recontacting step which consists of bringing said liquid hydrocarbon phase into contact with a gas phase 8 which has been compressed using a compressor 9 .
  • the gas phase is at a pressure in the range 1.5 to 4.5 MPa.
  • the gas phase 8 is obtained from the second recontacting step which is described below.
  • the first recontacting step is carried out by direct contact by in-line mixing of the liquid 4 and gaseous 8 phases.
  • the gas/liquid mixture is then cooled to a temperature in the range ⁇ 20° C. to 60° C. using a device 10 and sent to a separator drum 11 which is operated at the pressure of the gaseous phase 8 , i.e. in the range 1.5 to 4.5 MPa.
  • the cooling device may be an air exchanger or a water exchanger or a refrigerating device.
  • the separator drum 11 separates a hydrogen-rich gaseous effluent which is evacuated from the process via the line 12 , and a liquid hydrocarbon effluent which is sent via the line 13 to a second recontacting step.
  • the liquid hydrocarbon phase 4 is sent to the first recontacting step and the gas phase 6 is treated in the second recontacting step, while the liquid effluent produced in the first recontacting step is sent to the second recontacting step and the gaseous effluent obtained from the second recontacting step is used in the first recontacting step.
  • the process is designed to be what is known as a “counter-current” process, in which the liquid hydrocarbon phase 4 obtained from the separator drum 2 moves in the opposite direction to that of the gaseous phase 6 obtained from the separator drum 2 . As can be seen in FIG.
  • the liquid effluent obtained at the end of the first step for recontacting and gas/liquid separation is sent to a second recontacting step which uses the compressed gaseous phase 6 and a gaseous recycle phase 14 originating from the reflux drum of the stabilization column as described below.
  • the liquid 13 and gaseous 6 , 14 phases are brought into contact by in-line mixing and cooled with the cooling device 15 , for example an air exchanger or a water exchanger or a refrigerating device, to a temperature in the range ⁇ 20° C. to 60° C.
  • the second recontacting step is carried out at the pressure of the compressed gas 6 , namely in the range 0.8 to 3 MPa.
  • the gas/liquid mixture is transferred to a separator drum 16 configured to separate a gaseous effluent containing hydrogen plus C 1 -C 2 hydrocarbons and a liquid effluent containing mainly hydrocarbons containing 3 and more than 3 carbon atoms (C 3 + cut) with a minor quantity of light C 1 and C 2 hydrocarbons.
  • a separator drum 16 configured to separate a gaseous effluent containing hydrogen plus C 1 -C 2 hydrocarbons and a liquid effluent containing mainly hydrocarbons containing 3 and more than 3 carbon atoms (C 3 + cut) with a minor quantity of light C 1 and C 2 hydrocarbons.
  • the gaseous effluent containing hydrogen and C 1 -C 2 hydrocarbons withdrawn from the separator drum 16 via the line 17 is compressed by the compressor 9 in a manner such as to provide the compressed gas 8 which is brought into contact with the liquid hydrocarbon phase 4 (first counter-current recontacting step), as described above.
  • a liquid hydrocarbon effluent 18 is obtained, the final product of the recontacting steps, which undergoes a stabilization step to recover a liquefied petroleum gas (C 3 and C 4 hydrocarbons) and a stabilized hydrocarbon cut containing 5 or more than 5 carbon atoms (C 5 + cut).
  • a stabilization step to recover a liquefied petroleum gas (C 3 and C 4 hydrocarbons) and a stabilized hydrocarbon cut containing 5 or more than 5 carbon atoms (C 5 + cut).
  • the liquid effluent 18 is heated before being sent to a stabilization unit.
  • the stabilization unit comprises a distillation column 19 the bottom of which is provided with a circulation conduit equipped with a recirculation circuit comprising a reboiler (not shown) and an evacuation conduit 20 for the stabilized liquid effluent.
  • the overhead gas from the column moves in a conduit 21 connected to a condensation system comprising a cooling device 22 for the overhead gas and a reflux drum 23 .
  • the condensed liquid separated at the reflux drum 23 is evacuated via the line 24 and is divided into two streams, one stream being recycled to the column 19 via the line 25 , while the complementary stream which has not been recycled is evacuated from the process as a LPG stream via the line 26 .
  • the residual gas withdrawn from the head of the reflux drum 23 which has not been condensed and comprises C 3 and C 4 hydrocarbons and C 1 -C 2 hydrocarbons, is evacuated via the line 14 and recycled to the second recontacting step with the liquid effluent 13 (obtained from the first recontacting step), as described above.
  • the stabilized liquid effluent 20 recovered from the bottom of the distillation column 19 advantageously serves to supply an indirect heat exchanger system 27 , 28 in order to preheat the liquid effluent 18 before it enters the distillation column 19 . This thermal integration can thus be used to reduce the heating energy which has to be supplied to the reboiler in order to operate the distillation column 19 .
  • FIG. 2 is a flow diagram of a first embodiment of the process in accordance with the invention based on the flow diagram of FIG. 1 , and in which the second step for recontacting and separation of the liquid and gaseous phases is operated in a recontacting (or absorption) column 30 .
  • the recontacting column 30 may comprise perforated or bubble plates, or any other contacting plate, or may even be packed with structured or unstructured packing elements (Pall rings, Raschig rings or the like).
  • the column may have in the range 5 to 15 theoretical separation plates, preferably in the range 7 to 10.
  • the liquid effluent 13 obtained from the separator drum 11 is sent to the head of the column 30 , while the gaseous mixture comprising the compressed gaseous phase 6 and a gaseous recycle phase 14 originating from the reflux drum of the stabilization column is sent to the bottom of said column 30 in order to carry out a counter-current contact and so as to recover the gaseous effluent 17 containing hydrogen and C 1 -C 2 hydrocarbons and the liquid hydrocarbon effluent 18 respectively overhead and from the bottom of the column.
  • the liquid hydrocarbon phase 4 is cooled by a cooling device 15 which may be an air exchanger or a water exchanger or a refrigeration device.
  • the recontacting step is operated at a temperature in the range ⁇ 20° C. to 60° C., preferably in the range ⁇ 10° C. to 10° C., and at a pressure in the range 0.8 to 3 MPa.
  • Using a column 30 with counter-current contact of a non-stabilized liquid hydrocarbon phase 13 with low content of hydrogen and of light C 1 and C 2 hydrocarbons means that residual hydrocarbons contained in the vapour phase can be absorbed by the liquid phase.
  • the liquid hydrocarbon effluent recovered from the bottom of the column 30 is the hydrocarbon stream which is supplied to the stabilization column 19 , while the gas effluent 17 from the column head 30 which contains hydrogen and the residual hydrocarbons, essentially C 1 and C 2 , is sent to the compressor 9 in order to supply the compressed gas 8 at a pressure in the range 1.5 to 4.5 MPa.
  • said first recontacting step is carried out in-line, by bringing the compressed gas 8 into contact with the liquid hydrocarbon phase 4 obtained from the separator drum 2 .
  • contact is carried out at a temperature in the range ⁇ 20° C. to 60° C. (preferably in the range ⁇ 10° C. to 10° C.).
  • the gas/liquid mixing which was carried out in-line is cooled by the cooling device 10 .
  • the cooled mixture is sent to the separator drum 11 so as to separate a hydrogen-rich gas 12 containing C 1 and C 3 hydrocarbons and a liquid hydrocarbon effluent 13 which is recycled to the second recontacting step carried out in the column 30 .
  • the step for stabilization of the effluent 18 in the distillation column 19 is similar to that described with reference to FIG. 1 .
  • FIG. 3 represents another embodiment of the process of the invention, which differs from that of FIG. 1 by using a recontacting column 40 with a counter-current flow of liquid and gaseous phases in order to carry out the first step for recontacting and separation of the liquid and gaseous phases.
  • the liquid hydrocarbon phase 4 collected from the separator drum 2 and the compressed gaseous phase 8 are sent at the head and at the bottom of the column 40 respectively.
  • the liquid hydrocarbon phase 4 is cooled with the device 41 to a temperature in the range ⁇ 20° C. to 60° C., preferably in the range ⁇ 10° C. to 10° C.
  • Recontacting is carried out in the column at a pressure corresponding to that of the compressed gas 8 , i.e. in the range 1.5 to 4.5 MPa.
  • the hydrogen-rich gas 12 also containing C 1 and C 2 hydrocarbons is withdrawn from the head of the column 40 , while the liquid hydrocarbon phase 13 is sent to the second recontacting step where it is brought into contact with a gaseous stream resulting from mixing the compressed gaseous phase 6 and recycle gas 14 obtained from the reflux drum 23 of the stabilization column 19 .
  • contact of the liquid and gaseous phases is carried out by in-line mixing, at a temperature in the range ⁇ 20° C. to 60° C.
  • the gas/liquid mixture is cooled in the heat exchanger 15 .
  • the gas/liquid mixture cooled to a temperature in the range ⁇ 20° C. to 60° C. is introduced into the separator drum which separates a gaseous effluent 17 and a liquid effluent 18 which respectively supply the compressor 9 and the stabilization column 19 .
  • the step for stabilization of the effluent 18 in the distillation column 19 is similar to that described with reference to FIG. 1 .
  • FIG. 4 is another embodiment employing two recontacting columns 40 , 30 to respectively carry out the first and second recontacting and separation steps.
  • the bottom of the recontacting column 40 is supplied with a compressed gaseous stream obtained from the recontacting column 30 and with a liquid hydrocarbon stream which is the liquid hydrocarbon phase 4 originating from the step for separation of the treated feed 1 by the separator drum 2 .
  • the liquid hydrocarbon effluent 13 evacuated via the bottom of the column 40 is sent to the second recontacting step where it is brought into counter-current contact in the column 30 with the gaseous mixture 6 and 14 cooled in the exchanger 15 .
  • the liquid hydrocarbon effluent 18 which undergoes the stabilization step is withdrawn from the recontacting column 30 , enabling a stream of C 3 and C 4 hydrocarbons and a stabilized hydrocarbon cut to be provided.
  • the step for stabilization of the effluent 18 in the distillation column 19 is similar to that described with reference to FIG. 1 .
  • gaseous effluent 17 As was the case in the preceding embodiments, it is compressed then cooled before being supplied to the column 40 in order to bring it into counter-current contact with the cooled liquid hydrocarbon phase 4 .
  • This Example illustrates the process of FIG. 1 , in which two in-line recontacting steps are carried out, each recontacting step being followed by a gas/liquid separation step employing a separator drum.
  • the treated hydrocarbon feed is a reaction effluent obtained from a catalytic reforming unit and of which composition given in Table 1 below:
  • the feed was treated in a separator drum 2 at a temperature of approximately 40° C. and a pressure of approximately 0.33 MPa in order to provide a liquid hydrocarbon phase 4 and a gaseous phase 6 .
  • the first recontacting step was carried out in-line by mixing a gaseous stream obtained from the second recontacting step compressed to a pressure of 3.3 MPa and the liquid hydrocarbon phase 4 .
  • the gas/liquid mixture was cooled to a temperature of 0° C. then separated in a separation drum 11 which provided a hydrogen-rich gas 12 and the liquid effluent 13 .
  • the second recontacting step was also operated by in-line mixing of the gaseous phase 6 , compressed to a pressure of 1.67 MPa, with a recycle gas 14 obtained from the reflux drum of the stabilization column 19 and the liquid effluent 13 withdrawn from the separator drum 11 of the first recontacting step.
  • Gas/liquid contacting was carried out at a temperature of 43° C. and the mixture was sent to the separator drum 16 .
  • the liquid hydrocarbon effluent 18 was sent as a feed to the stabilization column operated to separate an overhead gas 21 containing C 3 and C 4 hydrocarbons and a stabilized liquid bottom fraction 20 containing hydrocarbons containing more than 4 carbon atoms.
  • the overhead gas 21 was condensed in a reflux drum which was operated at a pressure of 1.6 MPa and at a temperature of 43° C. in a manner such as to provide a liquid stream 24 containing LPG (C 3 and C 4 hydrocarbons).
  • This example is based on the flow diagram of FIG. 3 , in which the first step for recontacting and gas/liquid separation was carried out using a recontacting column 40 comprising 9 theoretical separation plates.
  • the treated feed was identical to that of Example 1; the composition is given in Table 1.
  • the recontacting column 40 was supplied overhead by the liquid hydrocarbon phase 4 cooled to a temperature of 0° C. and to the bottom with the gaseous mixture compressed to 3.3 MPa and at a temperature of 0° C.
  • the second recontacting step was operated by in-line mixing of the gaseous phase 6 compressed to a pressure of 1.6 MPa with a recycle gas 14 obtained from the reflux drum of the stabilization column 19 , then by cooling the mixture to a temperature of 43° C.
  • the cooled gaseous mixture was then brought into contact with the liquid hydrocarbon effluent withdrawn from the bottom of the column 40 , the temperature of which was approximately 12° C.
  • the cold gas/liquid mixture (approximately 25° C.) was sent to the gas/liquid separator 16 .
  • Table 2 provides the percentage recovery of hydrogen, LPG and reformate for the various streams generated by the processes of Examples 1 and 2.
  • Example 1 (FIG. 1) (FIG. 3) Recovery of hydrogen in gas (12) 100.0% by wt 100.0% by wt Purity of hydrogen in stream (12) 93.6 (mol %) 95.3 (mol %) Recovery of C 3 and C 4 52.9% by wt 82.1% by wt hydrocarbons in stream (26) Recovery of C 5 + hydrocarbons in 99.7% by wt 99.7% by wt stream (20)

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  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US15/209,820 2015-07-15 2016-07-14 Process for treating a hydrocarbon feed Abandoned US20170015912A1 (en)

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FR1501493A FR3038905B1 (fr) 2015-07-15 2015-07-15 Procede de traitement d'une charge hydrocarbonee
FR15/01493 2015-07-15

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CN114570165A (zh) * 2020-11-30 2022-06-03 中国石油天然气集团有限公司 重整产氢的再接触系统

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US4333820A (en) * 1981-01-26 1982-06-08 Uop Inc. Recovery of normally gaseous hydrocarbons from net excess hydrogen in a catalytic reforming process
US4673488A (en) * 1985-08-26 1987-06-16 Uop Inc. Hydrocarbon-conversion process with fractionator overhead vapor recycle
US5238555A (en) * 1991-11-27 1993-08-24 Uop Process for purifying a hydrogen gas and recovering liquifiable hydrocarbons from hydrocarbonaceous effluent streams

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US4212726A (en) * 1977-11-23 1980-07-15 Cosden Technology, Inc. Method for increasing the purity of hydrogen recycle gas
DE3511636A1 (de) * 1984-12-17 1986-07-10 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung von c(pfeil abwaerts)2(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)- oder von c(pfeil abwaerts)3(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen

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US4333820A (en) * 1981-01-26 1982-06-08 Uop Inc. Recovery of normally gaseous hydrocarbons from net excess hydrogen in a catalytic reforming process
US4673488A (en) * 1985-08-26 1987-06-16 Uop Inc. Hydrocarbon-conversion process with fractionator overhead vapor recycle
US5238555A (en) * 1991-11-27 1993-08-24 Uop Process for purifying a hydrogen gas and recovering liquifiable hydrocarbons from hydrocarbonaceous effluent streams

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114570165A (zh) * 2020-11-30 2022-06-03 中国石油天然气集团有限公司 重整产氢的再接触系统

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BR102016015529A2 (pt) 2017-01-24
CN106350113A (zh) 2017-01-25
CN106350113B (zh) 2020-10-16
BR102016015529B1 (pt) 2022-05-03
FR3038905A1 (fr) 2017-01-20

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