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WO2015198186A1 - Réacteur de reformeur autothermique et système d'alimentation associé - Google Patents

Réacteur de reformeur autothermique et système d'alimentation associé Download PDF

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Publication number
WO2015198186A1
WO2015198186A1 PCT/IB2015/054541 IB2015054541W WO2015198186A1 WO 2015198186 A1 WO2015198186 A1 WO 2015198186A1 IB 2015054541 W IB2015054541 W IB 2015054541W WO 2015198186 A1 WO2015198186 A1 WO 2015198186A1
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Prior art keywords
autothermal reformer
catalyst bed
enables
reformer reactor
natural gas
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Ceased
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PCT/IB2015/054541
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English (en)
Inventor
Atilla ERSÖZ
Aslı KAYTAZ
Fehmi AKGÜN
Göktuğ Nezihi ÖZYÖNÜM
Murat BARANAK
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Scientific and Technological Research Council of Turkey TUBITAK
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Scientific and Technological Research Council of Turkey TUBITAK
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Publication of WO2015198186A1 publication Critical patent/WO2015198186A1/fr
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    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
    • B01J8/0221—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical shaped bed
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00407—Controlling the temperature using electric heating or cooling elements outside the reactor bed
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00628—Controlling the composition of the reactive mixture
    • B01J2208/00646—Means for starting up the reaction
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00938—Flow distribution elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • C01B2203/1282—Mixing of different feed components using static mixers
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1288—Evaporation of one or more of the different feed components
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature
    • C01B2203/1619—Measuring the temperature
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1628—Controlling the pressure
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/169—Controlling the feed
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus

Definitions

  • the present invention relates to an autothermal reformer reactor which enables to produce a gas mixture with enriched hydrogen content and a feeding system of an autothermal reformer reactor which enables to supply optimum flow regime to the said reactor.
  • Hydrogen (H 2 ) can be produced catalytically by water vapour from other hydrocarbon fuels (methanol, LPG, naphtha, gasoline) in addition to natural gas.
  • reaction no. 1 is endothermic whereas the reactions no. 2 and 3 are exothermic. Heat required for the reaction no. 1 is met by the heat produced in the reactions no. 2 and 3. Therefore, autothermal reformer system is provided without the need for heat supply to the system or heat removal.
  • autothermal reformer reactors have a simple design because they do not need an additional heat exchanger.
  • autothermal reformer systems are quite advantageous in terms of start-up time and time of being able to respond to capacity changes which are two of the most critical parameters.
  • the most important parameters determining operation conditions of the process and the product composition can be defined as ratio of the water supplied to the reactor to the total carbon inside the fuel (S/C), ratio of the molecular oxygen supplied to the reactor to the total carbon inside the fuel (0 2 /C), operating temperature of the reactor, operating pressure of the reactor and space velocity (GHSV) of the gas mixture supplied to the reactor.
  • S/C total carbon inside the fuel
  • GHSV space velocity
  • Control of amount of oxygen (0 2 ) supplied to the system is quite important in order that the operating temperature is kept in desired range. Oxidation reactions and conversion reaction by water vapour take place in temperatures above 500°C very quickly by means of catalysts. In these systems, a product composition close to the thermodynamic equilibrium conditions is obtained.
  • temperature distribution in autothermal reformer reactor is characterized by a sudden increase in inlet. Fast oxidation reactions occur in this region where temperature increases. Following this region, temperature decreases because of endothermic reactions.
  • Catalytic combustion can be used as a start-up step for autothermal reformer reactors. Thus, heat required for initiating autothermal reformer reactions is provided by catalytic combustion of methane (CH 4 ).
  • the reaction region is designed as a turnaround chamber and a turn-around wall. Accordingly, the stream of product obtained at the end of the reactor can be returned to the reactant stream. Thus, the stream supplied from the opposite direction and the turn-around stream is in a stream axially.
  • This design provides creation of a low-velocity zone and offers advantages by stabilizing location of a flame.
  • the Japanese patent document no. JP2007326777 discloses a catalyst pre-heating apparatus for start-up of a compact fuel processor unit and a method for providing this. The apparatus described in the said patent document is used for heating the catalyst area in a time elapsed until the heat needed for starting-up the reactions is reached.
  • An electrically-powered heating element is used for heating the catalyst bed directly or indirectly. Direct heating incident is ensured by direct contact of the electrical heating element with the catalyst. Whereas indirect heating incident is ensured by direct heating of the fluid (process flow) sent to the reactor and then passing this fluid through the catalyst bed. Additionally, the electrical heating may be placed within a sheath coating in direct contact with the catalyst or the fluid sent to the catalyst bed.
  • catalysts of many forms, including pellets, extrudates, spheres, and monoliths may be used together with the said catalyst heater.
  • the catalyst heater may be in the form of a resistive wire, cartridge or rod, in a double form such that it may be coupled to a power source.
  • An objective of the present invention is to realize an autothermal reformer reactor which enables to produce a gas mixture with enriched hydrogen content.
  • Another objective of the present invention is to realize a feeding system of an autothermal reformer reactor which enables to supply optimum flow regime to the said reactor.
  • Figure 1 is a front view of the inventive autothermal reformer reactor.
  • Figure 2 is a schematic view of the inventive feeding system of an autothermal reformer reactor.
  • An autothermal reformer reactor (1) which enables to produce a gas mixture with enriched hydrogen content essentially comprises:
  • At least one second inlet port (3) where how water is supplied
  • at least one mixing chamber (4) where hot natural gas, superheated water vapour and air are mixed homogeneously and which is located under the first inlet port (2) and the second inlet port (3);
  • At least one catalyst bed (5) where chemical reactions enabling to produce a gas mixture with enriched hydrogen from mixture of hot natural gas, superheated water vapour and air are realized;
  • At least one outlet port (6) which is located on the lower part of the catalyst bed (5) and where the product obtained in the catalyst bed (5) exits;
  • At least one feeding chamber (7) which is located between the mixing chamber (4) and the catalyst bed (5) and ensures that the mixture of hot natural gas, superheated water vapour and air becoming homogeneous in the mixing chamber (4) is supplied to the catalyst bed (5);
  • At least two distribution plates (8) which are located on the inlet and outlet of the catalyst bed (5), ensures that the stream arriving the catalyst bed (5) from the feeding chamber (7) and the stream leading from the catalyst bed
  • At least one heating unit (9) which is located on the outlet of the feeding chamber (7), ensures that the mixture of hot natural gas, superheated water vapour and air supplied from the feeding chamber (7) to the catalyst bed (5) is heated to the temperature level that will create the reaction to occur in the catalyst bed (5).
  • the inventive autothermal reformer reactor (1) which enables to produce a gas mixture with enriched hydrogen content also comprises at least one first insulating layer (10) which is located on the outer part of the mixing chamber (4) and the feeding chamber (7) and enables generation of heat insulation in the said mixing chamber (4) and the feeding chamber (7).
  • the first insulating layer (10) is made of glass wool.
  • the inventive autothermal reformer reactor (1) which enables to produce a gas mixture with enriched hydrogen content also comprises at least one second insulating layer (11) which wraps the outer part of the catalyst bed (5), enables the catalyst bed (5) to remain stable and ensures heat insulation by minimizing heat transfer from the walls of the catalyst bed (5) outwards.
  • the second insulating layer (11) is made of an insulating layer of a ceramic blanket type.
  • the inventive autothermal reformer reactor (1) which enables to produce a gas mixture with enriched hydrogen content also comprises a plurality of temperature measurement devices (12) enabling to measure temperatures of the inlet of the catalyst bed (5), the inner of the catalyst bed (5), the outlet of the catalyst bed (5) and the outer part of the catalyst bed (5).
  • a thermocouple is used as the temperature measurement devices (12).
  • the heating unit (9) included in the inventive autothermal reformer reactor (1) which enables to produce a gas mixture with enriched hydrogen content is preferably an electric heater.
  • the feeding system (13) which enables to supply optimum flow regime to the inventive autothermal reformer reactor (1) described above comprises:
  • At least one natural gas feeding line (14) which enables to provide the natural gas to be supplied to the autothermal reformer reactor (1);
  • At least one water feeding line (15) which enables to provide the demineralised water to be supplied to the autothermal reformer reactor (1); at least one air feeding line (16) which enables to provide the hot air to be supplied to the autothermal reformer reactor (1);
  • At least one catalytic burner unit (17) which enables to pre-heat the natural gas received from the natural gas feeding line (14) and gives only hot exhaust gas (EGR) as output;
  • At least one first heat exchanger (18) which enables to turn the water (DW) received from the water feeding line (15) into saturated water vapour (SV) by heating it by means of the exhaust gas (EG) exiting the catalytic burner unit (17);
  • At least one second heat exchanger (19) which enables to heat the natural gas (NG) received from the natural gas feeding line (14), by means of the exhaust gas (EG) exiting the catalytic burner unit (17);
  • At least one pre-mixture unit (20) which enables to mix the saturated water vapour (SV) exiting the first heat exchanger (18) and the natural gas (NG) exiting the second heat exchanger (19); and
  • At least one third heat exchanger (21) which enables to heat the mixture of water vapour natural gas (SV+NG) exiting the pre-mixture unit (20) to higher temperatures by means of the gas mixture with enriched hydrogen exiting the autothermal reformer reactor (1).
  • the feeding system (13) which enables to supply optimum flow regime to the inventive autothermal reformer reactor (1) also comprises at least one first control valve (22) which is located between the first heat exchanger (18) and the pre- mixture unit (20) and enables to control temperature and pressure of the saturated water vapour (SV) exiting the first heat exchanger (18).
  • the feeding system (13) which enables to supply optimum flow regime to the inventive autothermal reformer reactor (1) also comprises at least one second control valve (23) which is located between the second heat exchanger (19) and the pre-mixture unit (20) and enables to control temperature and pressure of the hot natural gas (NG) exiting the second heat exchanger (19).
  • the feeding system (13) which enables to supply optimum flow regime to the inventive autothermal reformer reactor (1) also comprises at least one third control valve (24) which is located on the hot air feeding line (16) and enables to control temperature and pressure of the air passing through the line (16).
  • the natural gas feeding line (14) is opened and the natural gas (NG) stream is transmitted to the catalytic burner unit (17).
  • the hot exhaust gas (EG) generated after the catalytic burner unit (17) fires the natural gas (NG) is sent to the first heat exchanger (18) and the second heat exchanger (19).
  • the water feeding line (15) is in off-position and no water supply is realized to the system (1).
  • the natural gas (NG) heated by the hot air received from the hot air feeding line (16) and the gas exiting the catalytic burner unit (17) is supplied into the autothermal reformer reactor (1) from the first inlet port (2) and the second inlet port (3) of the autothermal reformer reactor (1).
  • the streams supplied to the autothermal reformer reactor (1) are almost at temperature of 150°C.
  • the said streams are mixed in the mixing chamber (4) inside the autothermal reformer reactor (1) in a homogeneous way.
  • the mixture reaches the temperature value defined as the ignition moment, it is supplied into the catalyst bed (5) over the distribution plate (8) and partial oxidation reaction starts here.
  • the autothermal reformer reactor (1) is supplied such that desired oxygen/carbon (CVC) value, preferably 0.5, is provided.
  • CVC desired oxygen/carbon
  • the demineralised water feeding line (15) is opened and the demineralised water is (DW) supplied to the first heat exchanger (18).
  • the temperature of the water (DW) heated by means of the exhaust gas (EG) reaches a value predetermined in the outlet of the first heat exchanger (18)
  • the natural gas feeding line (14) is opened.
  • Temperature of the natural gas (NG) supplied from the natural gas feeding line (14) is increased to a predetermined value in the second heat exchanger (19) and the saturated water vapour (SV) and the heated natural gas (NG) obtained in the first heat exchanger (18) are supplied to the pre- mixture unit (20) simultaneously and they are mixed with each other here.
  • the mixture of water vapour natural gas (SV+NG) prepared in the pre-mixture unit (20) also passes through the third heat exchanger (21) before the autothermal reformer reactor (1) is supplied and the temperature of the mixture is increased to almost 450°C.
  • the high-temperature water vapour-natural gas mixture (SV+NG) is supplied from the first inlet port (2) of the autothermal reformer reactor (1) and the hot water is supplied into the autothermal reformer reactor (1) from the second inlet port (3).
  • the mixture of high-temperature water vapour- natural gas mixture (SV+NG) and hot air supplied to the autothermal reformer reactor (1) is mixed with each other in the mixing chamber (4) homogeneously and supplied to the catalyst bed (5) over the distribution plate (8) without needing to operate the heating unit (9) and water vapour conversion reaction starts in the catalyst bed (5).
  • the autothermal reformer reactor (1) switches to autothermal mode.
  • Suitable steam/carbon adjustment is made by natural gas (NG) and water vapour (SV) until the temperature in the outlet port (6) of the autothermal reformer reactor (1) switching to the autothermal mode reaches around 750°C.
  • suitable ratio is between the values of 3-3,5.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un réacteur de reformeur autothermique (1) qui permet de produire un mélange de gaz avec une teneur enrichie en hydrogène et un système d'alimentation d'un réacteur de reformeur autothermique qui permet d'alimenter un régime optimal d'écoulement vers ledit réacteur de reformeur autothermique (1). Le réacteur comprend au moins deux entrées (2, 3) qui mènent à une chambre de mélange (4) qui à son tour est reliée à une chambre d'alimentation (7) placée en amont d'au moins un lit de catalyseur (5). Le lit de catalyseur (5) est situé entre deux plaques de distribution (8). Le réacteur comprend en outre au moins une unité chauffante (9), qui est située sur la sortie de la chambre d'alimentation (7).
PCT/IB2015/054541 2014-06-23 2015-06-16 Réacteur de reformeur autothermique et système d'alimentation associé Ceased WO2015198186A1 (fr)

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TR201407262 2014-06-23
TR2014/07262 2014-06-23

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WO2015198186A1 true WO2015198186A1 (fr) 2015-12-30

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Publication number Priority date Publication date Assignee Title
RU2677146C1 (ru) * 2018-05-04 2019-01-15 Андрей Владиславович Курочкин Установка для получения синтез-газа с каталитическим нагревателем
RU2677142C1 (ru) * 2018-05-04 2019-01-15 Андрей Владиславович Курочкин Устройство нагрева реакционной зоны каталитического реактора
EP3441360A1 (fr) 2017-08-10 2019-02-13 Sener Ingenieria Y Sistemas, S.A. Système de reformage d'alcools et de la production d'hydrogène, des unités de système et procédé associé
EP3693338A1 (fr) 2019-02-07 2020-08-12 Sener Ingenieria Y Sistemas, S.A. Système auto-thermique haute pression pour réformer de l'alcool et produire de l'hydrogène, procédé et unités correspondants
US20220119255A1 (en) * 2019-02-28 2022-04-21 Haldor Topsøe A/S Synthesis gas production by steam methane reforming

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WO1999065097A1 (fr) * 1998-06-09 1999-12-16 Mobil Oil Corporation Procede et systeme d'apport d'hydrogene pour cellules electrochimiques
WO2002066403A1 (fr) * 2001-02-16 2002-08-29 Conoco Inc. Catalyseurs sur support de rhodium-oxyde de type spinelle et procede de production de gaz de synthese
US20030129123A1 (en) * 2000-07-25 2003-07-10 Conocophillips Company Catalysts for SPOCTM enhanced synthesis gas production
JP2007326777A (ja) 2000-12-05 2007-12-20 Texaco Development Corp コンパクト燃料プロセッサーの起動のために触媒を加熱する装置及び方法
WO2008131562A1 (fr) 2007-05-01 2008-11-06 Nxtgen Emission Controls Inc. Processeur de combustible compact
US20100015479A1 (en) * 2006-06-01 2010-01-21 Klaus Rusch Assembly for producing a hydrogenous gas
EP2455334A1 (fr) * 2010-11-18 2012-05-23 Tecnicas Reunidas, S.A. Système pour le traitement de l'éthanol

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WO1999065097A1 (fr) * 1998-06-09 1999-12-16 Mobil Oil Corporation Procede et systeme d'apport d'hydrogene pour cellules electrochimiques
US20030129123A1 (en) * 2000-07-25 2003-07-10 Conocophillips Company Catalysts for SPOCTM enhanced synthesis gas production
JP2007326777A (ja) 2000-12-05 2007-12-20 Texaco Development Corp コンパクト燃料プロセッサーの起動のために触媒を加熱する装置及び方法
WO2002066403A1 (fr) * 2001-02-16 2002-08-29 Conoco Inc. Catalyseurs sur support de rhodium-oxyde de type spinelle et procede de production de gaz de synthese
US20100015479A1 (en) * 2006-06-01 2010-01-21 Klaus Rusch Assembly for producing a hydrogenous gas
WO2008131562A1 (fr) 2007-05-01 2008-11-06 Nxtgen Emission Controls Inc. Processeur de combustible compact
EP2455334A1 (fr) * 2010-11-18 2012-05-23 Tecnicas Reunidas, S.A. Système pour le traitement de l'éthanol

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3441360A1 (fr) 2017-08-10 2019-02-13 Sener Ingenieria Y Sistemas, S.A. Système de reformage d'alcools et de la production d'hydrogène, des unités de système et procédé associé
RU2677146C1 (ru) * 2018-05-04 2019-01-15 Андрей Владиславович Курочкин Установка для получения синтез-газа с каталитическим нагревателем
RU2677142C1 (ru) * 2018-05-04 2019-01-15 Андрей Владиславович Курочкин Устройство нагрева реакционной зоны каталитического реактора
EP3693338A1 (fr) 2019-02-07 2020-08-12 Sener Ingenieria Y Sistemas, S.A. Système auto-thermique haute pression pour réformer de l'alcool et produire de l'hydrogène, procédé et unités correspondants
WO2020160935A1 (fr) 2019-02-07 2020-08-13 Sener, Ingeniería Y Sistemas, S.A. Système auto-thermique haute pression pour le reformage d'alcool et la production d'hydrogène, procédé et unités associés
US20220119255A1 (en) * 2019-02-28 2022-04-21 Haldor Topsøe A/S Synthesis gas production by steam methane reforming
US12398035B2 (en) * 2019-02-28 2025-08-26 Haldor Topsøe A/S Synthesis gas production by steam methane reforming

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