EP4638917A1 - Combustion of off-gasses using enriched air from an electrolytic process - Google Patents

Combustion of off-gasses using enriched air from an electrolytic process

Info

Publication number
EP4638917A1
EP4638917A1 EP23833379.3A EP23833379A EP4638917A1 EP 4638917 A1 EP4638917 A1 EP 4638917A1 EP 23833379 A EP23833379 A EP 23833379A EP 4638917 A1 EP4638917 A1 EP 4638917A1
Authority
EP
European Patent Office
Prior art keywords
stream
steam
section
heat exchanger
gas stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP23833379.3A
Other languages
German (de)
French (fr)
Inventor
Casper Funk JACOBSEN
Troels Dahlgaard Stummann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Topsoe AS
Original Assignee
Haldor Topsoe AS
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Haldor Topsoe AS filed Critical Haldor Topsoe AS
Publication of EP4638917A1 publication Critical patent/EP4638917A1/en
Pending legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/064—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle in combination with an industrial process, e.g. chemical, metallurgical
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C25B1/044—Hydrogen or oxygen by electrolysis of water producing mixed hydrogen and oxygen gas, e.g. Brown's gas [HHO]
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a chemical plant and a process for production of a steam stream using a combustible off-gas stream.
  • purge stream When producing e.g. ammonia or methanol, in a chemical plant, a purge of combustible gases is emitted from the synthesis loop (a "purge stream” or “off-gas stream”). In conventional natural gas plants these purge streams are normally used as fuel in the reformer or fired heater.
  • This invention utilizes the heating value of the purge stream by combusting the stream in a duct burner with the enriched air from the electrolysis process. This improves the efficiency of the plant and make use of a stream, which is otherwise treated as a waste stream.
  • the present invention relates to a chemical plant, said plant comprising : a combustible off-gas stream, an electrolysis section, a first steam feed, at least one burner, a first heat exchanger, a water stream, wherein said electrolysis section is arranged to receive at least a portion of said first steam feed and electrolyze it to provide a hydrogen stream and an oxygen- enriched stream; wherein at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream are arranged to be combusted in said at least one burner so as to provide a combusted gas stream; wherein said first heat exchanger is arranged to receive at least a portion of said combusted gas stream, and said water stream, where said first heat exchanger is arranged to transfer heat from the at least a portion of said combusted gas stream to said water stream so as to provide a cooled combusted gas stream and a steam stream, and wherein said plant comprises a steam drum, said stream drum being
  • a process for production of a steam stream is provided using a combustible off-gas stream in a chemical plant as described herein, said process comprising the steps of: providing a plant as described herein; feeding at least a first portion of said first steam feed to said electrolysis section and electrolyzing said first portion to provide a hydrogen stream and an oxygen- enriched stream; feeding at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream to at least one burner to provide a combusted gas stream; supplying at least a portion of said combusted gas stream and said water stream to said first heat exchanger and allowing heat transfer from the at least a portion of said combusted gas stream to said water stream to take place, so as to provide a cooled combusted gas stream and a steam stream, and feeding at least a portion of said steam stream from the first heat exchanger to said steam drum and providing a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
  • Figure 1 shows a simple layout of one aspect of the system of the invention.
  • Figure 2 shows a more developed layout of the system of the invention.
  • Figure 3 shows a further developed layout of the system of the invention.
  • Figure 4 shows a further developed layout of the system of the invention.
  • Figure 5 shows a further developed layout of the system of the invention.
  • Figure 6 shows a further developed layout of the system of the invention.
  • any given percentages for gas content are % by volume. All feeds are preheated as required.
  • a “stage” comprises one or more “units” which perform a change in the chemical composition of a feed, and may additionally comprise elements such as e.g. heat exchanger, mixer or compressor, which do not change the chemical composition of a feed or stream.
  • synthesis gas (abbreviated to “syngas”) is meant to denote a gas comprising hydrogen, carbon monoxide, carbon dioxide and small amounts of other gasses, such as argon, nitrogen, methane, steam, etc.
  • a chemical plant comprises: a combustible off-gas stream, an electrolysis section, a first steam feed, at least one burner, a first heat exchanger, a water stream, and a steam drum.
  • a combustible off-gas stream refers to an off-gas stream comprising at least one combustible component, wherein said off-gas stream is produced within said chemical plant e.g. a purge gas stream or a waste gas stream from a purification section.
  • a typical combustible off-gas stream composition may e.g comprise CO, CO 2 , H 2 , CH 4 and inert gases (N 2 , Ar etc.).
  • the off-gas stream may further comprise unsaturated hydrocarbons, such as olefins or alkenes (C n H 2n ; n>2).
  • the specific composition of the combustible off-gas stream may vary, depending on the production purpose of the chemical plant.
  • the combustible off-gas stream may in an embodiment comprise 15-70 mole % H 2 , such as 20-70 mole %.
  • the combustible off-gas stream may in an embodiment comprise less than 25 mole % CO.
  • the combustible off-gas stream may in an embodiment comprise 0-25 mole % CO, such as 0.1-5 mole % or 10-25 mole %.
  • the combustible off-gas stream may in an embodiment comprise less than 35 mole % CH 4 .
  • the combustible off-gas stream may in an embodiment comprise 0-35 mole % CH 4 , such as 0.1-5 mole % or 10-25 mole %.
  • the combustible off-gas stream may in an embodiment comprise less than 20 mole % NH 3 .
  • the combustible off-gas stream may in an embodiment comprise 0-20 mole % NH 3 , such as 0.1- 10 mole %.
  • the combustible off-gas stream may comprise one or more of these combustible components in any combination with the proviso that the total amount of these combustible components amounts to 100% or less of the total combustible off-gas stream.
  • the total amount of these combustible components may thus amount to 40 - 100 mole % of the total combustible off-gas stream, such as 50 - 90 mole % or 50-80 mole % of the total combustible off-gas stream.
  • Other components may be present such as CO 2 , Argon and/or N 2 .
  • said chemical plant further comprises a syngas stream and a synthesis section wherein said synthesis section is arranged to receive said syngas stream and convert it into a product stream and an off-gas stream, and wherein said synthesis section is arranged to provide at least a portion of said off-gas stream to said burner.
  • the synthesis section (also referred to as a synthesis loop) is arranged to provide at least a portion of the off-gas stream to said burner, wherein said off-gas stream is a purge gas stream.
  • the synthesis section partly converts the syngas stream to a product stream and a recycle stream, where the recycle stream receives a second syngas steam (referred to as make-up syngas stream) followed by the recycle stream being recycled such that it re-enters the synthesis section such as into a synthesis reactor.
  • a second syngas steam referred to as make-up syngas stream
  • the recycle stream receives a second syngas steam (referred to as make-up syngas stream) followed by the recycle stream being recycled such that it re-enters the synthesis section such as into a synthesis reactor.
  • make-up syngas stream referred to as make-up syngas stream
  • the recycle stream is provide as an off-gas stream to said burner, preferably before adding make-up syngas.
  • the off-gas stream may comprise unconverted syn
  • the chemical plant comprises a syngas stream, a synthesis section, and a purification section, wherein said synthesis section is arranged to receive said syngas stream and convert it into a product stream and an off-gas stream and wherein said purification section is arranged to receive said product stream and convert it into a purified product stream and a further off-gas stream, and wherein said purification section is arranged to provide at least a portion of said further off-gas stream to said burner.
  • At least a portion of said off-gas stream arranged to be combusted in said at least one burner may be provided i) solely from one or more synthesis section(s), ii) solely from one or more purification section(s) or iii) a combination of off-gas streams from said synthesis section(s) and purification section(s) or iv) any of i-iii) combined with one or more alternative streams.
  • the specific composition depends on conditions comprising the following conditions: a) the composition of the provided feed(s) e.g.
  • stage/section/reactor(s) specifically the specification of the synthesis section and hence optionally the applied catalysts
  • arrangement of optional purification sections comprising recovery and/or separation section or units such as CO 2 recovery units and d) process conditions applied throughout the chemical plant such as temperature and pressure.
  • the chemical plant comprises a syngas stream.
  • Said syngas stream may be a gas stream comprising primarily hydrogen (H 2 ) and nitrogen (N 2 ).
  • said syngas stream may be a gas stream comprising hydrogen, carbon monoxide, carbon dioxide and small amounts of other gasses, such as argon, nitrogen, methane, steam.
  • Said syngas stream may be fed as a feed to said synthesis section.
  • the chemical plant comprises a synthesis section, wherein said synthesis section is an ammonia synthesis section, a methanol synthesis section, a methanol-to-olefins synthesis section, methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section.
  • synthesis section is an ammonia synthesis section, a methanol synthesis section, a methanol-to-olefins synthesis section, methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section.
  • TIGAS methanol-to-olefins
  • FT Fischer-Tropsch
  • the chemical plant comprises an ammonia synthesis section.
  • the chemical plant comprises a syngas stream comprising primarily H 2 and N 2 .
  • An electrolysis section may provide the H 2 or alternatively the H 2 may be provided from a production plant, wherein H 2 is produced from natural gas or fossil fuel.
  • An air fractionation unit may provide the N 2 .
  • the ammonia synthesis section may receive the syngas and provide an off-gas stream, which is fed to the burner.
  • the chemical plant comprises a methanol synthesis section, a methanol-to-olefins synthesis section, a methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section.
  • TIGAS methanol-to-olefins
  • FT Fischer-Tropsch
  • the syngas stream fed to the synthesis may comprise H 2 and CO 2 .
  • An electrolysis section may provide the H 2 or alternatively the H 2 may be provided from said chemical plant such that H 2 is produced from natural gas or fossil fuel.
  • the provided CO 2 is recovered from a flue gas from combustion of a fossil fuel or a non-fossil biomass.
  • the synthesis section receives the syngas and provide an off-gas stream, which is fed to the burner.
  • said purification section may comprise a CO 2 recovery unit.
  • the electrolysis section is arranged to receive at least a portion of said first steam feed and electrolyze it to provide a hydrogen stream and an oxygen-enriched stream.
  • a first steam feed is required as a feed for the electrolysis section.
  • the first steam feed is a dry steam feed of high purity.
  • a steam feed of high purity it is generally known to expose a water stream to some kind of water treatment prior to using it in industrial systems (may be referred to as a process steam).
  • Untreated water may contain impurities causing damage or wear to the system. Such impurities may cause formation of scales, corrosion, deposits etc.
  • oxygen may be unwanted in the process steam since it may cause corrosion, e.g. in piping and heat exchangers.
  • droplets/entrainment are unwanted due to high concentration of impurities in the boiler water.
  • One way of obtaining a steam feed of high purity is to first treat raw water in an ionexchanger to remove minerals. Demineralized water is then passed through a deaerator to produce deaerated water which is then passed to a boiler with a steam drum where dry steam is produced, which is then ready for use as a process steam. In the deaerator oxygen is stripped from the water and the stripped water is collected in a surge vessel. In the boiler, the deaerated water is heated in a heat exchanger and the heated mixture of water and steam is then separated in a steam drum to produce the dry steam for use as feed.
  • the electrolysis section may comprise solid oxide electrolysis cell (SOEC) electrodes such that the splitting of H 2 O occurs within a SOEC. Multiple cells may be combined into SOEC stacks, and multiple stacks may in turn be combined into an SOEC plant.
  • SOEC solid oxide electrolysis cell
  • a solid oxide cell (SOC) is an electrochemical conversion device having two compartments (an anode side and a cathode side) divided by an electrolyte material made of a solid oxide or a ceramic electrolyte. Such a cell is fully reversible e.g. for the components H 2 O ⁇ ->H 2 .
  • the first steam feed may enter the process side of the SOEC where it is (partly) converted into the hydrogen stream which is the fuel stream and an oxygen-enriched stream.
  • the oxygen produced in the conversion on the fuel side is transferred through the electrochemical cell to the oxy side of the SOEC, where it is recombined as gaseous oxygen. It is typically transported away from the SOEC with a flushing stream.
  • said plant comprises a flushing stream where the flushing stream is arranged to be supplied to the anode of said electrolysis section as flushing stream for flushing of oxygen, and thereby provide an oxygen-enriched stream.
  • the flushing stream is air, a nitrogen-rich stream or a CO 2 -rich stream.
  • At least a portion of the hydrogen stream provided by the electrolysis section is arranged to be fed as a feed to the synthesis section, optionally in admixture with syngas stream.
  • At least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream are arranged to be combusted in said at least one burner so as to provide a combusted gas stream.
  • at least one burner is a duct burner arranged in the enriched air duct of said electrolysis section.
  • Off-gases with a high heating value can be combusted alone. Off-gases with a low heating value might need additional support fuel, which could be H 2 and/or syngas Therefore, if required, an additional fuel stream, preferably being a portion of said hydrogen stream or a portion of said syngas stream, may be arranged to be provided to the at least one burner.
  • the at least one burner is arranged to receive an additional oxygencontaining stream.
  • a first heat exchanger is arranged to receive at least a portion of said combusted gas stream, and said water stream.
  • the first heat exchanger is arranged to transfer heat from the at least a portion of said combusted gas stream to said water stream so as to provide a cooled combusted gas stream and a steam stream.
  • At least a portion of said steam stream is fed to the electrolysis section as at least a portion of said first steam feed to the electrolysis section.
  • the plant comprises a steam drum, said stream drum being arranged to receive at least a portion of said steam stream from the first heat exchanger and provide a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
  • said plant further comprises a second heat exchanger, said second heat exchanger being arranged to heat a second water stream to produce a second steam stream and to feed said second steam stream to said steam drum. In this way, the second heat exchanger provides the remaining necessary heat to produce the steam stream.
  • said stream drum is arranged to receive a first water stream and said stream drum is arranged to provide said water stream to at least the first heat exchanger and/or provide said second water stream to the second heat exchanger.
  • the second heat exchanger comprises multiple heat exchanger units. Typically, the multiple heat exchangers are arranged in parallel. In one aspect, the second heat exchanger is heated by means of an electrical heater, a steam fired heater, by heat recovery from hot streams and/or by heat recovery using one or more heat pumps. Each heat exchanger unit may have different, multiple heat sources, either in sequence or in combination.
  • a steam drum is a standard feature of a water-tube boiler. It is a reservoir of water/steam at the top end of the water tubes. The drum stores the steam generated in the water tubes and acts as a phase-separator for the steam/water mixture.
  • a process for production of a steam stream using a combustible off-gas stream in a chemical plant comprises the steps of: providing a plant as described herein; feeding at least a first portion of said first steam feed to said electrolysis section and electrolyzing said first portion to provide a hydrogen stream and an oxygen- enriched stream; feeding at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream to at least one burner to provide a combusted gas stream; supplying at least a portion of said combusted gas stream and said water stream to said first heat exchanger and allowing heat transfer from the at least a portion of said combusted gas stream to said water stream to take place, so as to provide a cooled combusted gas stream and a steam stream and said process further comprises feeding at least a portion of said steam stream from the first heat exchanger to said steam drum and providing a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
  • the process further comprises the step, wherein at least a portion of said steam stream from said first heat exchanger is fed to the electrolysis section as at least a portion of said first steam feed to the electrolysis section.
  • said process further comprises feeding a first water stream to said steam drum so as to provide said water stream for at least the first heat exchanger.
  • said plant further comprises a second heat exchanger, and wherein said process comprises allowing heat transfer from said second heat exchanger to a second water stream provided from said steam drum to produce a second steam stream and feeding said second steam stream to said steam drum.
  • said process further comprises supplying a flushing stream such as an air or CO 2 -rich stream to the anode of said electrolysis section and flushing the oxygen with said flushing stream to provide an oxygen-enriched stream.
  • a flushing stream such as an air or CO 2 -rich stream
  • said flushing stream is oxygen poor and said process further comprises feeding a separate oxygen-containing stream to the at least one burner.
  • said chemical plant further comprises said syngas stream and said synthesis section, and wherein said process further comprises feeding a syngas to said synthesis section to provide a product stream and off-gas stream, and wherein at least a portion of said off-gas stream is fed as a feed to said burner.
  • said chemical plant further comprises the syngas stream, the synthesis section and the purification section, and said process further comprises feeding said syngas to said synthesis section to provide a product stream and off-gas stream and comprises feeding said product stream to said purification section to provide a purified product stream and an offgas stream, wherein at least a portion of said off-gas stream provided from said purification section is fed as a feed to said burner.
  • said process further comprises feeding at least a portion of the hydrogen stream from the electrolysis section to the synthesis section, optionally in admixture with a syngas stream. In another aspect, said process further comprises feeding an additional fuel stream, preferably being a portion of said hydrogen stream or a portion of said syngas stream, to the at least one burner.
  • said plant further comprises a synthesis section, and said process further comprises feeding least a portion of said steam stream to said synthesis section for use in a distillation process.
  • the synthesis section may be a methanol synthesis section, or other general synthesis section.
  • said plant comprises said purification section comprising a CO 2 recovery unit, and wherein said process comprises feeding least a portion of said steam stream to said purification section for regeneration of said CO 2 recovery unit.
  • an electrolysis section (20) receives at least a portion of a first steam feed (5) and electrolyze it to provide a hydrogen stream (22) and an oxygen-enriched stream (21). Additionally, said chemical plant (100) provides a combustible off-gas stream (12). At least one burner (30) receives at least a portion of said oxygen-enriched stream (21) and at least a portion of a combustible off-gas stream (12), such that said streams may be combusted within the at least one burner (30) so as to provide a combusted gas stream (31).
  • a first heat exchanger (40) receives at least a portion of said combusted gas stream (31), and a water stream (51) such that the first heat exchanger (40) allows for heat transfer from at least a portion of said combusted gas stream (31) to said water stream (51).
  • the first heat exchanger (40) provides a cooled combusted gas stream (42) and a steam stream (52).
  • the electrolysis section (20) receives a portion (52a) of said steam stream (52) such as in admixture with the said first steam feed (5).
  • the chemical plant (100) is further developed.
  • a first addition to what is described in the first specific embodiment comprises that said electrolysis section (20) receives a flushing stream (6) such that the anode of said electrolysis section (20) receives the flushing stream (6) for flushing of oxygen and said electrolysis section (20) thereby provides an oxygen-enriched stream (21).
  • a second addition to what is described in the first specific embodiment comprises that said combustible off-gas stream (12) is provided from a synthesis section (10), where said synthesis section (10) receives a syngas stream (1) and provides a product gas stream (11) and a combustible offgas stream (12).
  • a third addition to what is described in the first specific embodiment comprises that said chemical plant (100) further comprises a steam drum (50) and a second heat exchanger (60).
  • the second heat exchanger (60) receives and heat a first water stream (51b) to produce a second steam stream (52c).
  • Said the steam drum (50) receives at least a portion (52b) of said steam stream (52) and at least a portion of the second steam stream (52c) and produces the steam stream (52).
  • the electrolysis section (20) receives a portion (52a) of said steam stream (52) such as in admixture with the said first steam feed (5).
  • the chemical plant (100) is arranged such that the steam drum (50) receives the first water stream (51b) and provides the water stream (51) to at least the first heat exchanger (40) and provides said second water stream (51c) to the second heat exchanger (60).
  • the chemical plant (100) is further developed.
  • a first addition to what is described in the proceeding specific embodiments, comprises that said chemical plant (100) further comprises a purification section (15).
  • Said purification section (15) receives the product stream (11) from the synthesis section (10) and converts it into a purified product stream (16) and an off-gas stream (12b).
  • the at least one burner (30) may receive the combustible off-gas (12, 12b) from the synthesis section (10), from the purification section (15) or from both the synthesis section (10) and the purification section (15), the latter optionally as admixed streams.
  • a second addition to what is described in the proceeding specific embodiments comprises that at least a portion (22a) of the hydrogen stream (22) from the electrolysis section (20) may be provided to the synthesis section (10) as an additional syngas, optionally in admixture with the syngas stream (1).
  • a third addition to what is described in the proceeding specific embodiments comprises that the at least one burner (30) receives a separate oxygen-containing stream (7). In may be preferred if said flushing stream (6) is oxygen poor. In one embodiment, illustrated in figure 5, the at least one burner (30) receives an additional fuel stream (8), preferably being a portion of said hydrogen stream (22b) from the electrolysis section (20) or a portion of said syngas stream (la).
  • the chemical plant (100) comprises the synthesis section (10), and said synthesis section (10) receives at least a portion (52d) of said steam stream (52) for use in a distillation process. Also illustrated in figure 6, is one embodiment of said chemical plant (100), comprises the purification section (15) wherein the purification section (15) comprises a CO 2 recovery unit (15a), such that said purification section (15) receives least a portion (52d) of said steam stream (52) for regeneration of said CO 2 recovery unit (15a).
  • First example as illustrated in fig 3, comprises process simulation performed in relation to ammonia synthesis.
  • Duty (energy transfer) in heat exchanger (40) in the oxygen-enriched stream (31) increases from 3.46 to 4.32 MW (25%) when the burner 30 is added to the system and stream 12 is fed to the burner 30.
  • the electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 3.3 MW to 2.4 MW (Part of 60). This corresponds to (26.5 %). Ranges used :
  • Second example as illustrated in fig. 3 comprises process simulation preformed in relation to methanol synthesis.
  • Duty (energy transfer) in heat exchanger (40) in the oxygen-enriched stream (31) increases from 1.8 MW to 2.3 MW (27.7 %).
  • Electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 7.0 MW to 6.5 MW (Part of 60). This corresponds to (7.3%)
  • Third example as illustrated in fig. 3 comprises process simulation preformed in relation to Fischer-Tropsch synthesis.
  • Duty (energy transfer) in heat exchanger (40) in the oxygen- enriched stream (31) increases from 1.96 MW to 2.62 MW (33.2 %).
  • Electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 7.0 MW to 6.35 MW (Part of 60). This corresponds to (9.3%)

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Abstract

A chemical plant is provided, in which an electrolysis section is arranged to receive at least a portion of a first steam feed and electrolyze it to provide a hydrogen stream and an oxygen- enriched stream. At least a portion of the oxygen-enriched stream and at least a portion of an off-gas stream are arranged to be combusted in at least one burner so as to provide a combusted gas stream. The first heat exchanger is arranged to receive at least a portion of said combusted gas stream and said water stream. The first heat exchanger is arranged to transfer heat from the at least a portion of the combusted gas stream to the water stream so as to provide a cooled combusted gas stream and a steam stream. A process for production of a steam stream using a combustible off-gas stream in the chemical plant is also provided.

Description

COMBUSTION OF OFF-GASSES USING ENRICHED AIR FROM AN ELECTROLYTIC PROCESS
TECHNICAL FIELD
The present invention relates to a chemical plant and a process for production of a steam stream using a combustible off-gas stream.
BACKGROUND
When producing e.g. ammonia or methanol, in a chemical plant, a purge of combustible gases is emitted from the synthesis loop (a "purge stream" or "off-gas stream"). In conventional natural gas plants these purge streams are normally used as fuel in the reformer or fired heater.
In chemical plants based on electrolysis, which may not comprise fired heaters, such purge streams are currently a waste/export stream. There is a desire to make effective use of purge streams in chemical plants. This would improve the efficiency of the plant and make use of what might otherwise be a waste stream.
SUMMARY
This invention utilizes the heating value of the purge stream by combusting the stream in a duct burner with the enriched air from the electrolysis process. This improves the efficiency of the plant and make use of a stream, which is otherwise treated as a waste stream.
So, in a first aspect the present invention relates to a chemical plant, said plant comprising : a combustible off-gas stream, an electrolysis section, a first steam feed, at least one burner, a first heat exchanger, a water stream, wherein said electrolysis section is arranged to receive at least a portion of said first steam feed and electrolyze it to provide a hydrogen stream and an oxygen- enriched stream; wherein at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream are arranged to be combusted in said at least one burner so as to provide a combusted gas stream; wherein said first heat exchanger is arranged to receive at least a portion of said combusted gas stream, and said water stream, where said first heat exchanger is arranged to transfer heat from the at least a portion of said combusted gas stream to said water stream so as to provide a cooled combusted gas stream and a steam stream, and wherein said plant comprises a steam drum, said stream drum being arranged to receive at least a portion of said steam stream from the first heat exchanger and provide a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
In another aspect, a process for production of a steam stream is provided using a combustible off-gas stream in a chemical plant as described herein, said process comprising the steps of: providing a plant as described herein; feeding at least a first portion of said first steam feed to said electrolysis section and electrolyzing said first portion to provide a hydrogen stream and an oxygen- enriched stream; feeding at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream to at least one burner to provide a combusted gas stream; supplying at least a portion of said combusted gas stream and said water stream to said first heat exchanger and allowing heat transfer from the at least a portion of said combusted gas stream to said water stream to take place, so as to provide a cooled combusted gas stream and a steam stream, and feeding at least a portion of said steam stream from the first heat exchanger to said steam drum and providing a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
Further aspects of the present invention are set out in the following description text, figures and the appended claims.
LEGENDS
The technology is illustrated by means of the following schematic illustrations, in which: Figure 1 shows a simple layout of one aspect of the system of the invention.
Figure 2 shows a more developed layout of the system of the invention.
Figure 3 shows a further developed layout of the system of the invention.
Figure 4 shows a further developed layout of the system of the invention.
Figure 5 shows a further developed layout of the system of the invention.
Figure 6 shows a further developed layout of the system of the invention.
DETAILED DISCLOSURE
Unless otherwise specified, any given percentages for gas content are % by volume. All feeds are preheated as required.
A "stage" comprises one or more "units" which perform a change in the chemical composition of a feed, and may additionally comprise elements such as e.g. heat exchanger, mixer or compressor, which do not change the chemical composition of a feed or stream.
The term "synthesis gas" (abbreviated to "syngas") is meant to denote a gas comprising hydrogen, carbon monoxide, carbon dioxide and small amounts of other gasses, such as argon, nitrogen, methane, steam, etc.
In a first aspect, a chemical plant is provided, said plant comprises: a combustible off-gas stream, an electrolysis section, a first steam feed, at least one burner, a first heat exchanger, a water stream, and a steam drum.
Combustible off-gas stream A combustible off-gas stream refers to an off-gas stream comprising at least one combustible component, wherein said off-gas stream is produced within said chemical plant e.g. a purge gas stream or a waste gas stream from a purification section. A typical combustible off-gas stream composition may e.g comprise CO, CO2, H2, CH4 and inert gases (N2, Ar etc.). Optionally, the off-gas stream may further comprise unsaturated hydrocarbons, such as olefins or alkenes (CnH2n; n>2). The specific composition of the combustible off-gas stream may vary, depending on the production purpose of the chemical plant.
The combustible off-gas stream may in an embodiment comprise 15-70 mole % H2, such as 20-70 mole %. The combustible off-gas stream may in an embodiment comprise less than 25 mole % CO. The combustible off-gas stream may in an embodiment comprise 0-25 mole % CO, such as 0.1-5 mole % or 10-25 mole %. The combustible off-gas stream may in an embodiment comprise less than 35 mole % CH4. The combustible off-gas stream may in an embodiment comprise 0-35 mole % CH4, such as 0.1-5 mole % or 10-25 mole %. The combustible off-gas stream may in an embodiment comprise less than 20 mole % NH3. The combustible off-gas stream may in an embodiment comprise 0-20 mole % NH3, such as 0.1- 10 mole %. The combustible off-gas stream may comprise one or more of these combustible components in any combination with the proviso that the total amount of these combustible components amounts to 100% or less of the total combustible off-gas stream. The total amount of these combustible components may thus amount to 40 - 100 mole % of the total combustible off-gas stream, such as 50 - 90 mole % or 50-80 mole % of the total combustible off-gas stream. Other components may be present such as CO2, Argon and/or N2.
In one aspect, said chemical plant further comprises a syngas stream and a synthesis section wherein said synthesis section is arranged to receive said syngas stream and convert it into a product stream and an off-gas stream, and wherein said synthesis section is arranged to provide at least a portion of said off-gas stream to said burner.
In one embodiment, the synthesis section (also referred to as a synthesis loop) is arranged to provide at least a portion of the off-gas stream to said burner, wherein said off-gas stream is a purge gas stream. In said embodiment, the synthesis section partly converts the syngas stream to a product stream and a recycle stream, where the recycle stream receives a second syngas steam (referred to as make-up syngas stream) followed by the recycle stream being recycled such that it re-enters the synthesis section such as into a synthesis reactor. To control the content of by-products and inert gasses, which may accumulate due to said recycle stream, at least a portion of the recycle stream is provide as an off-gas stream to said burner, preferably before adding make-up syngas. In this way, the off-gas stream may comprise unconverted syngas, by-products produced within said synthesis section and inert gases.
In one aspect, the chemical plant comprises a syngas stream, a synthesis section, and a purification section, wherein said synthesis section is arranged to receive said syngas stream and convert it into a product stream and an off-gas stream and wherein said purification section is arranged to receive said product stream and convert it into a purified product stream and a further off-gas stream, and wherein said purification section is arranged to provide at least a portion of said further off-gas stream to said burner.
Within these aspects, at least a portion of said off-gas stream arranged to be combusted in said at least one burner may be provided i) solely from one or more synthesis section(s), ii) solely from one or more purification section(s) or iii) a combination of off-gas streams from said synthesis section(s) and purification section(s) or iv) any of i-iii) combined with one or more alternative streams. In this way, the specific composition depends on conditions comprising the following conditions: a) the composition of the provided feed(s) e.g. syngas stream; b) type and combinations of stage/section/reactor(s) specifically the specification of the synthesis section and hence optionally the applied catalysts; c) arrangement of optional purification sections comprising recovery and/or separation section or units such as CO2 recovery units and d) process conditions applied throughout the chemical plant such as temperature and pressure.
In aspects, the chemical plant comprises a syngas stream. Said syngas stream may be a gas stream comprising primarily hydrogen (H2) and nitrogen (N2). Alternatively, said syngas stream may be a gas stream comprising hydrogen, carbon monoxide, carbon dioxide and small amounts of other gasses, such as argon, nitrogen, methane, steam. Said syngas stream may be fed as a feed to said synthesis section.
In one aspect, the chemical plant comprises a synthesis section, wherein said synthesis section is an ammonia synthesis section, a methanol synthesis section, a methanol-to-olefins synthesis section, methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section.
In one embodiment, the chemical plant comprises an ammonia synthesis section. In said embodiment, the chemical plant comprises a syngas stream comprising primarily H2 and N2. An electrolysis section may provide the H2 or alternatively the H2 may be provided from a production plant, wherein H2 is produced from natural gas or fossil fuel. An air fractionation unit may provide the N2. The ammonia synthesis section may receive the syngas and provide an off-gas stream, which is fed to the burner. In other embodiments, the chemical plant comprises a methanol synthesis section, a methanol-to-olefins synthesis section, a methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section. In said embodiments the syngas stream fed to the synthesis may comprise H2 and CO2. An electrolysis section may provide the H2 or alternatively the H2 may be provided from said chemical plant such that H2 is produced from natural gas or fossil fuel. Typically, the provided CO2 is recovered from a flue gas from combustion of a fossil fuel or a non-fossil biomass. The synthesis section receives the syngas and provide an off-gas stream, which is fed to the burner.
In embodiments wherein the chemical plant comprises a purification section, said purification section may comprise a CO2 recovery unit.
The electrolysis section
The electrolysis section is arranged to receive at least a portion of said first steam feed and electrolyze it to provide a hydrogen stream and an oxygen-enriched stream.
A first steam feed is required as a feed for the electrolysis section. Preferably, the first steam feed is a dry steam feed of high purity. To obtain a steam feed of high purity, it is generally known to expose a water stream to some kind of water treatment prior to using it in industrial systems (may be referred to as a process steam). Untreated water may contain impurities causing damage or wear to the system. Such impurities may cause formation of scales, corrosion, deposits etc. Also, oxygen may be unwanted in the process steam since it may cause corrosion, e.g. in piping and heat exchangers. Furthermore droplets/entrainment are unwanted due to high concentration of impurities in the boiler water.
One way of obtaining a steam feed of high purity, is to first treat raw water in an ionexchanger to remove minerals. Demineralized water is then passed through a deaerator to produce deaerated water which is then passed to a boiler with a steam drum where dry steam is produced, which is then ready for use as a process steam. In the deaerator oxygen is stripped from the water and the stripped water is collected in a surge vessel. In the boiler, the deaerated water is heated in a heat exchanger and the heated mixture of water and steam is then separated in a steam drum to produce the dry steam for use as feed.
The electrolysis section may comprise solid oxide electrolysis cell (SOEC) electrodes such that the splitting of H2O occurs within a SOEC. Multiple cells may be combined into SOEC stacks, and multiple stacks may in turn be combined into an SOEC plant. A solid oxide cell (SOC) is an electrochemical conversion device having two compartments (an anode side and a cathode side) divided by an electrolyte material made of a solid oxide or a ceramic electrolyte. Such a cell is fully reversible e.g. for the components H2O<->H2.
The first steam feed may enter the process side of the SOEC where it is (partly) converted into the hydrogen stream which is the fuel stream and an oxygen-enriched stream. The oxygen produced in the conversion on the fuel side is transferred through the electrochemical cell to the oxy side of the SOEC, where it is recombined as gaseous oxygen. It is typically transported away from the SOEC with a flushing stream.
In one aspect, said plant comprises a flushing stream where the flushing stream is arranged to be supplied to the anode of said electrolysis section as flushing stream for flushing of oxygen, and thereby provide an oxygen-enriched stream. In one aspect, the flushing stream is air, a nitrogen-rich stream or a CO2-rich stream.
In one aspect, at least a portion of the hydrogen stream provided by the electrolysis section is arranged to be fed as a feed to the synthesis section, optionally in admixture with syngas stream.
Burner
At least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream are arranged to be combusted in said at least one burner so as to provide a combusted gas stream. In one aspect, at least one burner is a duct burner arranged in the enriched air duct of said electrolysis section.
Off-gases with a high heating value can be combusted alone. Off-gases with a low heating value might need additional support fuel, which could be H2 and/or syngas Therefore, if required, an additional fuel stream, preferably being a portion of said hydrogen stream or a portion of said syngas stream, may be arranged to be provided to the at least one burner.
When the flushing stream is air or where no stream is used, then no additional air is needed. If flushing stream does not contain oxygen, then additional oxygen might be needed. In one aspect, therefore the at least one burner is arranged to receive an additional oxygencontaining stream.
Heat exchanger A first heat exchanger is arranged to receive at least a portion of said combusted gas stream, and said water stream. The first heat exchanger is arranged to transfer heat from the at least a portion of said combusted gas stream to said water stream so as to provide a cooled combusted gas stream and a steam stream.
In one aspect, at least a portion of said steam stream is fed to the electrolysis section as at least a portion of said first steam feed to the electrolysis section.
Steam drum and additional heat exchangers
The plant comprises a steam drum, said stream drum being arranged to receive at least a portion of said steam stream from the first heat exchanger and provide a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section.
In one aspect, said plant further comprises a second heat exchanger, said second heat exchanger being arranged to heat a second water stream to produce a second steam stream and to feed said second steam stream to said steam drum. In this way, the second heat exchanger provides the remaining necessary heat to produce the steam stream.
In one aspect, said stream drum is arranged to receive a first water stream and said stream drum is arranged to provide said water stream to at least the first heat exchanger and/or provide said second water stream to the second heat exchanger.
In one aspect, the second heat exchanger comprises multiple heat exchanger units. Typically, the multiple heat exchangers are arranged in parallel. In one aspect, the second heat exchanger is heated by means of an electrical heater, a steam fired heater, by heat recovery from hot streams and/or by heat recovery using one or more heat pumps. Each heat exchanger unit may have different, multiple heat sources, either in sequence or in combination.
A steam drum is a standard feature of a water-tube boiler. It is a reservoir of water/steam at the top end of the water tubes. The drum stores the steam generated in the water tubes and acts as a phase-separator for the steam/water mixture.
Process for production of a steam stream
In a second aspect, a process for production of a steam stream using a combustible off-gas stream in a chemical plant is also provided. Said process comprises the steps of: providing a plant as described herein; feeding at least a first portion of said first steam feed to said electrolysis section and electrolyzing said first portion to provide a hydrogen stream and an oxygen- enriched stream; feeding at least a portion of said oxygen-enriched stream and at least a portion of said off-gas stream to at least one burner to provide a combusted gas stream; supplying at least a portion of said combusted gas stream and said water stream to said first heat exchanger and allowing heat transfer from the at least a portion of said combusted gas stream to said water stream to take place, so as to provide a cooled combusted gas stream and a steam stream and said process further comprises feeding at least a portion of said steam stream from the first heat exchanger to said steam drum and providing a portion of said steam stream as at least a portion of said first steam feed to the electrolysis section..
In one aspect, the process further comprises the step, wherein at least a portion of said steam stream from said first heat exchanger is fed to the electrolysis section as at least a portion of said first steam feed to the electrolysis section.
In one aspect, said process further comprises feeding a first water stream to said steam drum so as to provide said water stream for at least the first heat exchanger.
In one aspect, said plant further comprises a second heat exchanger, and wherein said process comprises allowing heat transfer from said second heat exchanger to a second water stream provided from said steam drum to produce a second steam stream and feeding said second steam stream to said steam drum.
In one aspect, said process further comprises supplying a flushing stream such as an air or CO2-rich stream to the anode of said electrolysis section and flushing the oxygen with said flushing stream to provide an oxygen-enriched stream. In a more specific aspect, said flushing stream is oxygen poor and said process further comprises feeding a separate oxygen-containing stream to the at least one burner.
In one aspect, said chemical plant further comprises said syngas stream and said synthesis section, and wherein said process further comprises feeding a syngas to said synthesis section to provide a product stream and off-gas stream, and wherein at least a portion of said off-gas stream is fed as a feed to said burner. In one aspect, said chemical plant further comprises the syngas stream, the synthesis section and the purification section, and said process further comprises feeding said syngas to said synthesis section to provide a product stream and off-gas stream and comprises feeding said product stream to said purification section to provide a purified product stream and an offgas stream, wherein at least a portion of said off-gas stream provided from said purification section is fed as a feed to said burner.
In one aspect, said process further comprises feeding at least a portion of the hydrogen stream from the electrolysis section to the synthesis section, optionally in admixture with a syngas stream. In another aspect, said process further comprises feeding an additional fuel stream, preferably being a portion of said hydrogen stream or a portion of said syngas stream, to the at least one burner.
In one aspect, said plant further comprises a synthesis section, and said process further comprises feeding least a portion of said steam stream to said synthesis section for use in a distillation process. The synthesis section may be a methanol synthesis section, or other general synthesis section.
In a further aspect, said plant comprises said purification section comprising a CO2 recovery unit, and wherein said process comprises feeding least a portion of said steam stream to said purification section for regeneration of said CO2 recovery unit.
Specific embodiments
In a chemical plant (100), illustrated in figure 1, an electrolysis section (20) receives at least a portion of a first steam feed (5) and electrolyze it to provide a hydrogen stream (22) and an oxygen-enriched stream (21). Additionally, said chemical plant (100) provides a combustible off-gas stream (12). At least one burner (30) receives at least a portion of said oxygen-enriched stream (21) and at least a portion of a combustible off-gas stream (12), such that said streams may be combusted within the at least one burner (30) so as to provide a combusted gas stream (31). A first heat exchanger (40) receives at least a portion of said combusted gas stream (31), and a water stream (51) such that the first heat exchanger (40) allows for heat transfer from at least a portion of said combusted gas stream (31) to said water stream (51). In this way, the first heat exchanger (40) provides a cooled combusted gas stream (42) and a steam stream (52). Optionally, the electrolysis section (20) receives a portion (52a) of said steam stream (52) such as in admixture with the said first steam feed (5). In one embodiment, illustrated in figure 2, the chemical plant (100) is further developed. A first addition to what is described in the first specific embodiment, comprises that said electrolysis section (20) receives a flushing stream (6) such that the anode of said electrolysis section (20) receives the flushing stream (6) for flushing of oxygen and said electrolysis section (20) thereby provides an oxygen-enriched stream (21). A second addition to what is described in the first specific embodiment, comprises that said combustible off-gas stream (12) is provided from a synthesis section (10), where said synthesis section (10) receives a syngas stream (1) and provides a product gas stream (11) and a combustible offgas stream (12). A third addition to what is described in the first specific embodiment, comprises that said chemical plant (100) further comprises a steam drum (50) and a second heat exchanger (60). In this embodiment, the second heat exchanger (60) receives and heat a first water stream (51b) to produce a second steam stream (52c). Said the steam drum (50) receives at least a portion (52b) of said steam stream (52) and at least a portion of the second steam stream (52c) and produces the steam stream (52). Optionally, the electrolysis section (20) receives a portion (52a) of said steam stream (52) such as in admixture with the said first steam feed (5).
In one embodiment, illustrated in figure 3, the chemical plant (100) is arranged such that the steam drum (50) receives the first water stream (51b) and provides the water stream (51) to at least the first heat exchanger (40) and provides said second water stream (51c) to the second heat exchanger (60).
In one embodiment, illustrated in figure 4, the chemical plant (100) is further developed. A first addition to what is described in the proceeding specific embodiments, comprises that said chemical plant (100) further comprises a purification section (15). Said purification section (15) receives the product stream (11) from the synthesis section (10) and converts it into a purified product stream (16) and an off-gas stream (12b). In this way, the at least one burner (30) may receive the combustible off-gas (12, 12b) from the synthesis section (10), from the purification section (15) or from both the synthesis section (10) and the purification section (15), the latter optionally as admixed streams. A second addition to what is described in the proceeding specific embodiments, comprises that at least a portion (22a) of the hydrogen stream (22) from the electrolysis section (20) may be provided to the synthesis section (10) as an additional syngas, optionally in admixture with the syngas stream (1). A third addition to what is described in the proceeding specific embodiments, comprises that the at least one burner (30) receives a separate oxygen-containing stream (7). In may be preferred if said flushing stream (6) is oxygen poor. In one embodiment, illustrated in figure 5, the at least one burner (30) receives an additional fuel stream (8), preferably being a portion of said hydrogen stream (22b) from the electrolysis section (20) or a portion of said syngas stream (la).
In one embodiment, illustrated in figure 6, the chemical plant (100) comprises the synthesis section (10), and said synthesis section (10) receives at least a portion (52d) of said steam stream (52) for use in a distillation process. Also illustrated in figure 6, is one embodiment of said chemical plant (100), comprises the purification section (15) wherein the purification section (15) comprises a CO2 recovery unit (15a), such that said purification section (15) receives least a portion (52d) of said steam stream (52) for regeneration of said CO2 recovery unit (15a).
EXAMPLES
First example as illustrated in fig 3, comprises process simulation performed in relation to ammonia synthesis. Duty (energy transfer) in heat exchanger (40) in the oxygen-enriched stream (31) increases from 3.46 to 4.32 MW (25%) when the burner 30 is added to the system and stream 12 is fed to the burner 30. The electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 3.3 MW to 2.4 MW (Part of 60). This corresponds to (26.5 %). Ranges used :
Off-gas [NH3] [Mole %]
Range: Typical
N2: 15-60 23
H2: 20-70 66
CH4: 0-25 0
Ar: 5-15 10
NH3: 0-2 1
Other: < 1 < 1
Second example as illustrated in fig. 3 comprises process simulation preformed in relation to methanol synthesis. Duty (energy transfer) in heat exchanger (40) in the oxygen-enriched stream (31) increases from 1.8 MW to 2.3 MW (27.7 %). Electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 7.0 MW to 6.5 MW (Part of 60). This corresponds to (7.3%)
Off-gas (MeOH) [Mole %] Range: Typical
H2: 40-60 50
CO2: 35-55 45
CO: 0-2 1
CH4: 0-5 2
MeOH: 0-6 3
Others: 0-5 < 1
Conclusion: Use of waste stream reduces power consumption in the chemical plant.
Third example as illustrated in fig. 3 comprises process simulation preformed in relation to Fischer-Tropsch synthesis. Duty (energy transfer) in heat exchanger (40) in the oxygen- enriched stream (31) increases from 1.96 MW to 2.62 MW (33.2 %). Electrical power for producing the steam required for the process (52a) in the electrolysis section (20) is reduced from 7.0 MW to 6.35 MW (Part of 60). This corresponds to (9.3%)
Off-gas (F-T) [Mole %]
Range: Typical
H2 15-25 17
CO2 20-50 33
CO 10-25 15
CH4 10-35 32
N2 0-5
C2+ XX-XX 0-5 2
Conclusion: Use of waste stream reduces power consumption in the chemical plant.
While the invention has been described with reference to a number of embodiments and aspects, the overall scope of the invention is defined in the appended claims. The skilled person may combine embodiments and aspects as required, within the scope of the invention. All documents mentioned herein are incorporated by reference.

Claims

1. A chemical plant (100), said plant (100) comprising: a combustible off-gas stream (12) an electrolysis section (20) a first steam feed (5) at least one burner (30) a first heat exchanger (40) a water stream (51) wherein said electrolysis section (20) is arranged to receive at least a portion of said first steam feed (5) and electrolyze it to provide a hydrogen stream (22) and an oxygen-enriched stream (21); wherein at least a portion of said oxygen-enriched stream (21) and at least a portion of said off-gas stream (12) are arranged to be combusted in said at least one burner (30) so as to provide a combusted gas stream (31); wherein said first heat exchanger (40) is arranged to receive at least a portion of said combusted gas stream (31), and said water stream (51), where said first heat exchanger (40) is arranged to transfer heat from the at least a portion of said combusted gas stream (31) to said water stream (51) so as to provide a cooled combusted gas stream (42) and a steam stream (52),
, wherein said plant comprises a steam drum (50), said stream drum (50) being arranged to receive at least a portion of said steam stream (52b) from the first heat exchanger (40) and provide a portion of said steam stream (52a) as at least a portion of said first steam feed (5) to the electrolysis section (20).
2. The chemical plant according to claim 1, wherein said plant comprises a second heat exchanger (60), said second heat exchanger (60) being arranged to heat a second water stream (51c) to produce a second steam stream (52c) and to feed said second steam stream (52c) to said steam drum (50).
3. The chemical plant according to any one of claim 1 or 2, wherein said stream drum (50) is arranged to receive a first water stream (51b) and said stream drum (50) is arranged to provide said water stream (51) to at least the first heat exchanger (40) and/or provide said second water stream (51c) to the second heat exchanger (60).
4. The chemical plant according to claim 3, wherein the second heat exchanger (60) comprises multiple heat exchanger units.
5. The chemical plant according to claim 3 or 4, wherein the second heat exchanger (60) is heated by means of an electrical heater, a steam fired heater, by heat recovery from hot streams and/or by heat recovery using one or more heat pumps.
6. The chemical plant according to any one of the proceeding claims, wherein said plant comprises a flushing stream (6) where the flushing stream is arranged to be supplied to the anode of said electrolysis section (20) as flushing stream for flushing of oxygen, and thereby provide an oxygen-enriched stream (21).
7. The chemical plant according to claim 6, wherein the flushing stream (6) is air, a nitrogen-rich stream or a CC>2-rich stream.
8. The chemical plant according to any one of the preceding claims, where the at least one burner (30) is arranged to receive an additional oxygen-containing stream (7).
9. The chemical plant according to any one of the proceeding claims, wherein said chemical plant further comprises a syngas stream (1) and a synthesis section (10) wherein said synthesis section (10) is arranged to receive said syngas stream (1) and convert it into a product stream (11) and an off-gas stream (12), and wherein said synthesis section (10) is arranged to provide at least a portion of said off-gas stream (12) to said burner (30).
10. The chemical plant according to any one of the proceeding claims, wherein said chemical plant comprises a syngas stream (1), a synthesis section (10), and a purification section (15), wherein said synthesis section (10) is arranged to receive said syngas stream (1) and convert it into a product stream (11) and an off-gas stream (12) and wherein said purification section (15) is arranged to receive said product stream (11) and convert it into a purified product stream (16) and a further off-gas stream (12b), and wherein said purification section (15) is arranged to provide at least a portion of said further off-gas stream (12b) to said burner (30).
11. The chemical plant according to any one of claim 9 or 10, wherein said synthesis section is an ammonia synthesis section, a methanol synthesis section, a methanol- to-olefins synthesis section, a methanol-to-gasoline (TIGAS) synthesis section, a methanation section or a Fischer-Tropsch (FT) synthesis section.
12. The chemical plant according to any one of the preceding claims, wherein the at least one burner (30) is a duct burner arranged in the enriched air duct of said electrolysis section (20).
13. The chemical plant according to any one of claim 9-12, wherein at least a portion of the hydrogen stream (22a) provided by the electrolysis section (20) is arranged to be fed as a feed to the synthesis section (10), optionally in admixture with syngas stream (1).
14. The chemical plant according to any one of the proceeding claims, wherein an additional fuel stream (8), preferably being a portion of said hydrogen stream (22b) or a portion of said syngas stream (la), is arranged to be provided to the at least one burner (30).
15. A process for production of a steam stream (52) using a combustible off-gas stream (12) in a chemical plant (100) according to any one of the preceding claims, said process comprising the steps of: providing a plant according to any one of the preceding claims; feeding at least a first portion of said first steam feed (5) to said electrolysis section (20) and electrolyzing said first portion to provide a hydrogen stream (22) and an oxygen-enriched stream (21); feeding at least a portion of said oxygen-enriched stream (21) and at least a portion of said off-gas stream (12) to at least one burner (30) to provide a combusted gas stream (31); supplying at least a portion of said combusted gas stream (31) and said water stream (51) to said first heat exchanger (40) and allowing heat transfer from the at least a portion of said combusted gas stream (31) to said water stream (51) to take place, so as to provide a cooled combusted gas stream (42) and a steam stream (52), and feeding at least a portion of said steam stream (52b) from the first heat exchanger (40) to said steam drum (50) and providing a portion of said steam stream (52a) as at least a portion of said first steam feed (5) to the electrolysis section (20).
16. The process according to claim 15, wherein said process comprises feeding a first water stream (51b) to said steam drum (50) so as to provide said water stream (51) for at least the first heat exchanger (40).
17. The process according to any one of claim 15 or 16, wherein said plant comprises a second heat exchanger (60), and wherein said process comprises allowing heat transfer from said second heat exchanger (60) to a second water stream (51c) provided from said steam drum (50) to produce a second steam stream (52c) and feeding said second steam stream (52c) to said steam drum (50).
18. The process according to any one of claims 15-17, wherein said process comprises supplying a flushing stream (6) such as an air or CO2-rich stream to the anode of said electrolysis section (20) and flushing the oxygen with said flushing stream (6) to provide an oxygen-enriched stream (21).
19. The process according to claim 18, wherein said flushing stream (6) is oxygen poor and said process further comprises feeding a separate oxygen-containing stream (7) to the at least one burner (30).
20. The process according to any one of claims 15-19, wherein said chemical plant comprises said syngas stream (1) and said synthesis section (10), and wherein said process comprises feeding a syngas (1) to said synthesis section (10) to provide a product stream (11) and off-gas stream (12), and wherein at least a portion of said off-gas stream is fed as a feed to said burner (30).
21. The process according to any one of claims 15-20, wherein said chemical plant comprises the syngas stream (1), the synthesis section (10) and the purification section (15), and wherein said process comprises feeding said syngas (1) to said synthesis section (10) to provide a product stream (11) and off-gas stream (12) and comprises feeding said product stream (11) to said purification section (15) to provide a purified product stream (16) and an off-gas stream (12b), wherein at least a portion of said off-gas stream (12b) provided from said purification section (15) is fed as a feed to said burner (30).
22. The process according to any one of claims 15-21, wherein the off-gas stream comprises between 15-70 mole % hydrogen (H2), less than 25 mole % carbon monoxide (CO) and less than 35 mole % methane (CH4).
23. The process according to any one of claim 20-22, wherein said process comprises feeding at least a portion of the hydrogen stream (22a) from the electrolysis section (20) to the synthesis section (10), optionally in admixture with a syngas stream (1).
24. The process according to any one of claims 20-23, wherein said process comprises feeding an additional fuel stream (8), preferably being a portion of said hydrogen stream (22b) or a portion of said syngas stream (la), to the at least one burner (30).
25. The process according to any one of claims 20-24, wherein said plant comprises a synthesis section (10), and wherein said process comprises feeding at least a portion (52d) of said steam stream (52) to said synthesis section (10) for use in a distillation process.
26. The process according to any one of claims 20-25, wherein said plant comprises said purification section (15) comprising a CO2 recovery unit (15a), and wherein said process comprises feeding least a portion (52d) of said steam stream (52) to said purification section (15) for regeneration of said CO2 recovery unit (15a).
EP23833379.3A 2022-12-23 2023-12-15 Combustion of off-gasses using enriched air from an electrolytic process Pending EP4638917A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP22216438 2022-12-23
PCT/EP2023/086021 WO2024132913A1 (en) 2022-12-23 2023-12-15 Combustion of off-gasses using enriched air from an electrolytic process

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JP (1) JP2026501273A (en)
KR (1) KR20250127050A (en)
CN (1) CN120359345A (en)
AU (1) AU2023410825A1 (en)
CL (1) CL2025001561A1 (en)
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WO (1) WO2024132913A1 (en)

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US20080115500A1 (en) * 2006-11-15 2008-05-22 Scott Macadam Combustion of water borne fuels in an oxy-combustion gas generator
NO20150411A1 (en) * 2015-04-09 2016-10-10 Aker Solutions As Method and plant for oxygen generation
MX2021000400A (en) * 2018-07-12 2021-05-27 Haldor Topsoe As EXPANDER FOR SOEC APPLICATIONS.

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JP2026501273A (en) 2026-01-14
CL2025001561A1 (en) 2025-08-29
CN120359345A (en) 2025-07-22
TW202437580A (en) 2024-09-16
WO2024132913A1 (en) 2024-06-27
AU2023410825A1 (en) 2025-05-29

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