GB2585643A - Methods and systems for gasification of hydrocarbonaceous feedstocks - Google Patents

Methods and systems for gasification of hydrocarbonaceous feedstocks Download PDF

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Publication number
GB2585643A
GB2585643A GB1909779.9A GB201909779A GB2585643A GB 2585643 A GB2585643 A GB 2585643A GB 201909779 A GB201909779 A GB 201909779A GB 2585643 A GB2585643 A GB 2585643A
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Prior art keywords
syngas
carbon dioxide
gas mixture
oxygen
gas
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GB201909779D0 (en
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Hurudza Munyaradzi Mkushi George
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Lfeog Ltd
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Lfeog Ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • 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
    • C01B3/36—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 oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/005—Carbon dioxide
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • 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
    • C01B2203/86—Carbon dioxide sequestration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0969—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C10J2300/1815—Recycle loops, e.g. gas, solids, heating medium, water for carbon dioxide
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)

Abstract

A system for producing a syngas, the system comprising: a gas mixer for receiving a gas mixture comprising oxygen, recovered carbon dioxide and other gases; a gasifier, for gasification, using the gas mixture, of input fuel comprising feedstock, to produce syngas; a scrubber for scrubbing the producer gas to remove carbon dioxide from the syngas; means for capturing carbon dioxide from the removed carbon dioxide; and means for circulating the captured carbon dioxide to the gas mixer, wherein said gas mixture comprises at least some of the captured carbon dioxide. The fuel may be hydrocarbons.

Description

Methods and Systems for Gasification of Hydrocarbonaceous Feedstocks
Technical Field
Aspects of the present invention generally relate to methods and systems to gasify hydrocarbonaceous feedstocks to produce a syngas whose bulk volumetric components are hydrogen and carbon monoxide. The methods may include heating and modifying the oxidation in biomass and waste gasification by feedstocks.
Background
Current practice in the waste management sector involves recovering the energy value in refuse derived fuel (RDF) as required by the waste framework directive (WED) and the renewable energy directive (RED). RDF is the result of solid waste produced by the public and commercial / industrial organisations once the valuable components of the waste have been recycled. In this situation, waste is collected by a waste management company who seek to recover and recycle all of the materials from waste that can be economically justified (recyclables).
Typically, RDF undergoes gasification and or combustion at close coupled gasification or "energy from waste" / "waste to energy" plants. The resultant hot combustion gases are passed through a boiler to raise steam and subsequently generate power via a steam Rankine cycle.
In the situation where the fuel has a CV which is too high, these plants are unabie to provide sufficient air to fully combust the fuel due to the limitations of large blower design, and the resultant high temperatures of the flue gases result in mechanical and corrosion failures on the steam boiler and superheater tubes.
Typicaliy, energy from waste plants are unable to heat the superheated steam they generate to more than 523 degrees centigrade for this reason, limiting the efficiency they can achieve when compared to coal fired ultra-super critical steam power stations for example.
In cases where the fuel has a CV which is too Low, they suffer an efficiency loss because the efficiency of steam (Rankine Cycle) plants improves with increasing difference between the maximum temperature of the heat source (flue gases) and the heat sink (cooling) in accordance with the Carnot principle, and a low CV fuel will not achieve the heat source temperatures which will maximise the efficiency of these plants.
It is to these problems, amongst others, that aspects according to the invention attempt to offer a solution.
zo Summary
Aspects of the present invention relate to multifuel processes for syngas generation from heterogenous feedstocks. In particular, they relate to processes for the generation of a syngas from any carbonaceous feedstock (containing carbon), including hydrocarbonaceous feedstock (containing carbon).
According to a first independent aspect, there is provided a method of producing syngas, the method comprising the steps of: a) providing a gas mixture comprising oxygen and carbon dioxide recovered from step c); b) providing the gas mixture to a gasifier for gasification of input fuel comprising feedstock, to produce syngas; c) scrubbing the syngas to remove and recover carbon dioxide from the syngas; and repeating steps a) to c), wherein, in step a), the gas mixture comprises carbon dioxide as captured at step c).
It will be appreciated that the gas mixture may contain other gases. In an example, the gas mixture at step a) is oxygen enriched air.
The removal and recovery of CO2 from a syngas is therefore used for the purpose of increasing the concentration of carbon monoxide and hydrogen in the resultant syngas. Advantageously, feedstock flexibility is increased because the resultant syngas has higher concentrations of CO and H2 than is possible with the prior art for biomass and waste derived feedstocks regardless of the carbonaceous feedstocks' proximate or ultimate composition.
The resultant syngas can have a CV which varies less than 5%. This permits the use of prime movers which are smaller than would otherwise be possible reducing capital costs.
In a dependent aspect, before scrubbing, the syngas produced at step b) is cooled using carbon dioxide as captured at step c), resulting in heated carbon dioxide.
zo In a dependent aspect, the gas mixture comprises air and the said heated carbon dioxide.
Using the captured (i.e. recovered) CO2 as a coolant to cool the producer gas (i.e. syngas) serves a dual purpose of cooling syngas and preheating the CO2 before scrubbing. This allows for a safer method than preheating oxidisers such as air or oxygen, because there is no consequence to a failure of the heat exchanger tubes between the syngas and the oxidiser.
Advantageously, the method is also safer than a heat recovery boiler because it can operate at lower pressures than an equivalent steam system and has lower capex than a steam system.
According to a second independent aspect, there is provided a system for producing a syngas, the system comprising: a gas mixer for receiving a gas mixture comprising oxygen; a gasifier, for gasification, using the gas mixture, of input fuel comprising feedstock, to produce syngas; a scrubber for scrubbing the syngas to remove carbon dioxide from the syngas; means for capturing carbon dioxide from the removed carbon dioxide; and means for circulating the captured carbon dioxide to the gas mixer, wherein said gas mixture comprises at least some of the captured carbon dioxide.
In dependent aspects, the gas mixture is provided using oxygen enriched air, preferably with an 02 concentration greater than 22% in molar percentage. This results in improved performance of the oxidant stream enabling a smaller gasification reaction vessel.
Further preferred features of each one of the independent claims are provided in the dependent claims.
Brief Description of the Figures
Embodiments of the invention will be described with reference to the accompanying Figures, in which: Figure 1, which is a schematic diagram of a system according to the present invention; Figure 2 is a schematic partial diagram of the system, showing the use of hot syngas to heat captured carbon dioxide, thereby cooling the hot syngas.
Detailed Description
With reference to Figures 1 and 2, embodiments of the present invention involve the utilisation of a number of process steps. It will be appreciated that some of these steps are optional, being described in the Summary section above as dependent aspects.
Step 1 Air is oxygen enriched, being provided to an oxygen enricher before being passed to a gas mixer. In this example, the oxygen fraction is increased to an oxygen concentration greater than 22%, at temperatures less than 150 degrees centigrade. Optionally, the target oxygen fraction is determined by a control system, improving process control. Modification of thermal oxidant stream may be achieved through removal of N2.
Step 2 The enriched oxygen stream is transferred to a gas mixer. It will be appreciated that the gas mixer can be any suitable container such as a vessel, pipe, reactor element etc. The enriched oxidant stream is mixed with captured carbon dioxide from Step 6 (described below) and may also be mixed with heated carbon dioxide from Step 4 (described below). A target mixture composition may be determined by the control system.
Step 3 The resultant gas mixture from Step 2 is transferred to a gasifier (i.e. gasification reactor) where it reacts with the input fuel, in this example hydrocarbonaceous feedstock. The resultant gas is referred to as syngas or producer gas.
The producer gas is optionally filtered to remove particulate. Optionally, it is possible to use thermal hydrocarbon cracking and soot auto consumption.
The syngas may be optionally conditioned (e.g. using lysis of volatile organic compounds (VOCs) polyaromatic hydrocarbons (PAHs) and polychlorinated bisphenol (PCBs)) through the separate or combined addition recovered carbon dioxide from Step 6, the gas mixture from Step 2, the undiluted oxidant gas from Step 1 or steam to achieve the target setpoint as determined by the control system. Advantageously, the performance of the oxidant stream (oxidant fraction of oxidant stream) is improved by the presence of 02 and CO2 as oxidants.
Step 4 Heat may be recovered from the syngas produced in Step 3. Advantageously, this may be achieved by heating all or a fraction of the carbon dioxide recovered in Step 6. The fraction to be heated may be determined by the control system. At the same time, this represents a means of cooling the syngas produced in Step 3.
The syngas may be cooled to a temperature preferably less than the boiling point of water at the operating temperature.
Step 5 The syngas is scrubbed in a scrubber such as a gas / liquid contactor or series of contactors removing condensable water-soluble gases, ash particulate and condensable hydrocarbons.
This may include the removal of condensable water, water soluble acid and alkaline gases, ash and light hydrocarbons for example. Advantageously, lower carbon levels are found in the gasifier ash/slag.
Step 6 A fraction of carbon dioxide present in the syngas from Step 5 is recovered from the syngas. For example, more than 10% of the carbon dioxide present in the resultant gas from Step 5 is removed. Subsequently, all or a fraction of the removed carbon dioxide is recovered (captured) for use as the coolant in Step 4. Some of the removed carbon dioxide may be mixed in the gas mixture at Step 2.
It will be appreciated that the above steps may be repeated forming a cycle.
The methods and systems described above minimise the presence of carbon dioxide, nitrogen, condensable water and hydrocarbons (tars) in the resultant syngas. The following main advantages are noted: * Improved performance of the oxidant stream through the presence of 02 and CO2 as oxidants, enabling a smaller gasification reaction vessel; * Smaller equipment and reduced capital costs at the heat recovery stage; * Equipment downstream of the system is smaller due to the lower concentration contaminant and dilutant gases reducing capital costs for subsequent plant equipment.
* Heat recovery from the syngas is safer because of the use of the captured carbon dioxide; * The gasification process has a lowered equivalence ratio and a higher thermal efficiency due to the use of preheated carbon dioxide as part of the oxidant mixture produced in Step 2; * The control system is better able to respond to changes in the feedstock meaning the process will be able to accept a broader range of hydrocarbonaceous feedstock without the requirement for pre-treatment or blending because the greater control over the oxidant mixture(s) being injected at Step 3; * The resulting syngas can have a calorific value which is greater than 10 Mj/Nm3; * Lower carbon levels in the gasifier ash / slag generated at Step 3; The methods and systems claimed are undertaken for the purpose of thermally converting the biomass and waste derived feedstocks into hydrogen and carbon monoxide. This is of value to, but not limited to, the waste management industry where feedstock sent to energy from waste plants is highly variable, and a significant tonnage is rejected because it is outside the fuel specification for state-of-the-art plants.
Interpretation It will be appreciated that the order of performance of the steps in any of the embodiments in the present description is not essential, unless required by context or otherwise specified.
Thus some steps may be performed in any order. In addition, any of the embodiments may include more or fewer steps than those disclosed.
Additionally, it will be appreciated that the term "comprising" and its grammatical variants must be interpreted inclusively, unless the context requires otherwise. That is, "comprising" should be interpreted as meaning "including but not limited to".
Moreover, the invention has been described in terms of various specific embodiments. However, it will be appreciated that these are only examples which are used to illustrate the invention without limitation to those specific embodiments. Consequently, modifications can be made to the described embodiments without departing from the scope of the invention.

Claims (20)

  1. BCLAIMS1. A method of producing syngas, the method comprising the steps of: a) providing a gas mixture including oxygen and carbon dioxide recovered from step c); b) providing the gas mixture to a gasifier for gasification of input fuel comprising feedstock, to produce syngas; c) scrubbing the syngas to remove and recover carbon dioxide from the syngas; and repeating steps a) to c), wherein, in step a), the gas mixture includes carbon dioxide as captured at step c) and oxygen.
  2. 2. A method according to claim 1, wherein, before scrubbing, the syngas produced at step b) is cooled using carbon dioxide as captured at step c), resulting in heated carbon dioxide.
  3. 3. A method according to claim 2, wherein the gas mixture comprises air and the said heated carbon dioxide.
  4. 4. A method according to any preceding claim, wherein, at step a), the gas mixture is provided using oxygen enriched air.
  5. 5. A method according to claim 4, wherein oxygen is present in the gas mixture in a concentration greater than 22% on a molar basis.
  6. 6. A method according to any preceding claim, wherein, at step a), the gas mixture is at a temperature less than 150 degrees centigrade.
  7. 7. A method according to any preceding daim, wherein, the gas mixture has a target gas mixture composition determined by a control system.
  8. 8. A method according to any preceding claim, wherein said feedstock is hydrocarbonaceous feedstock.
  9. 9. A method according to any preceding claim, wherein, in step b), the syngas is filtered to remove particulate.
  10. 10. A method according to any preceding claim, wherein, in step b), the syngas is conditioned to achieve a target syngas composition.
  11. 11. A method according to claim 10, wherein said conditioning comprises one or more of: adding carbon dioxide as captured at step c), adding gas mixture from step a), adding oxidant gas and adding steam.
  12. 12. A method according to any preceding claims, wherein prior to scrubbing the syngas is cooled to a temperature less than a boiling point of water in the prevailing operating conditions.
  13. 13. A method according to any preceding claim, wherein, in step c), scrubbing is in at Least one gas/liquid contactor for removing condensable water-soluble gases, ash particulate and condensable hydrocarbons.
  14. 14. A method according to preceding claim, wherein, in step c), at least 10% of carbon dioxide present in the syngas is removed.
  15. 15. A system for producing a syngas, the system comprising: a gas mixer for receiving a gas mixture comprising oxygen; a gasifier, for gasification, using the gas mixture, of input fuel comprising feedstock, to produce syngas; a scrubber for scrubbing the syngas to remove carbon dioxide from the syngas; means for capturing carbon dioxide from the removed carbon dioxide; and means for circulating the captured carbon dioxide to the gas mixer, wherein said gas mixture comprises at least some of the captured carbon dioxide.
  16. 16. A system according to claim 15, further comprising means for cooling the syngas before scrubbing.
  17. 17. A system according to claim 15 or claim 16, further comprising a control system for setting a target gas mixture composition for the gas mixture.
  18. 18. A system according to any of claims 15 to 17, further comprising an oxygen enriching element for increasing oxygen concentration in air comprised in the gas mixture.
  19. 19. A system according to any of claims 15 to 19, further comprising a filtering element for filtering the syngas.
  20. 20. A system according to any of claims 15 to 19, further comprising a conditioner for conditioning the syngas.
GB1909779.9A 2019-07-08 2019-07-08 Methods and systems for gasification of hydrocarbonaceous feedstocks Withdrawn GB2585643A (en)

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB711912A (en) * 1950-11-06 1954-07-14 Ruhrchemie Ag A process for the production of hydrocarbons by the conversion of solid carbonaceousfuels
US4017271A (en) * 1975-06-19 1977-04-12 Rockwell International Corporation Process for production of synthesis gas
JPS5538846A (en) * 1978-09-14 1980-03-18 Agency Of Ind Science & Technol Gasification of coal
DE2843976A1 (en) * 1978-10-09 1980-04-10 Steag Ag Pressure gasification of solid fuels for power generation - with washing of acid gases from the prod. and recycling of carbon di:oxide
US20090282739A1 (en) * 2008-05-16 2009-11-19 Poul Erik Hojlund Nielsen Process for the preparation of synthesis gas from black liquor
US20100324156A1 (en) * 2009-06-17 2010-12-23 John Duckett Winter Methods of recycling carbon dioxide to the gasification system
US20120301949A1 (en) * 2010-02-01 2012-11-29 See - Soluções, Energia E Meio Ambiente Ltda. Method and system for producing hydrogen from carbon-containing raw materials
US20140151603A1 (en) * 2011-05-09 2014-06-05 Hrl Treasury (Idgcc) Pty Ltd Integrated drying gasification
CN208151308U (en) * 2018-04-08 2018-11-27 新能能源有限公司 Fluidized-bed gasification furnace gasifying agent system

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB711912A (en) * 1950-11-06 1954-07-14 Ruhrchemie Ag A process for the production of hydrocarbons by the conversion of solid carbonaceousfuels
US4017271A (en) * 1975-06-19 1977-04-12 Rockwell International Corporation Process for production of synthesis gas
JPS5538846A (en) * 1978-09-14 1980-03-18 Agency Of Ind Science & Technol Gasification of coal
DE2843976A1 (en) * 1978-10-09 1980-04-10 Steag Ag Pressure gasification of solid fuels for power generation - with washing of acid gases from the prod. and recycling of carbon di:oxide
US20090282739A1 (en) * 2008-05-16 2009-11-19 Poul Erik Hojlund Nielsen Process for the preparation of synthesis gas from black liquor
US20100324156A1 (en) * 2009-06-17 2010-12-23 John Duckett Winter Methods of recycling carbon dioxide to the gasification system
US20120301949A1 (en) * 2010-02-01 2012-11-29 See - Soluções, Energia E Meio Ambiente Ltda. Method and system for producing hydrogen from carbon-containing raw materials
US20140151603A1 (en) * 2011-05-09 2014-06-05 Hrl Treasury (Idgcc) Pty Ltd Integrated drying gasification
CN208151308U (en) * 2018-04-08 2018-11-27 新能能源有限公司 Fluidized-bed gasification furnace gasifying agent system

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