WO2023281426A1 - Méthode et installation pour le traitement de déchets à base de carbone - Google Patents

Méthode et installation pour le traitement de déchets à base de carbone Download PDF

Info

Publication number
WO2023281426A1
WO2023281426A1 PCT/IB2022/056268 IB2022056268W WO2023281426A1 WO 2023281426 A1 WO2023281426 A1 WO 2023281426A1 IB 2022056268 W IB2022056268 W IB 2022056268W WO 2023281426 A1 WO2023281426 A1 WO 2023281426A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
hydrogasification
hydrogen
reforming
methane
Prior art date
Application number
PCT/IB2022/056268
Other languages
English (en)
Inventor
Alberto GIACONIA
Silvano Tosti
Giampaolo Caputo
Alfonso Pozio
Original Assignee
Agenzia Nazionale Per Le Nuove Tecnologie, L'energia E Lo Sviluppo Economico Sostenibile (Enea)
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 Agenzia Nazionale Per Le Nuove Tecnologie, L'energia E Lo Sviluppo Economico Sostenibile (Enea) filed Critical Agenzia Nazionale Per Le Nuove Tecnologie, L'energia E Lo Sviluppo Economico Sostenibile (Enea)
Priority to EP22747757.7A priority Critical patent/EP4367057A1/fr
Publication of WO2023281426A1 publication Critical patent/WO2023281426A1/fr

Links

Classifications

    • 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
    • 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
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift 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
    • C01B2203/0465—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
    • C01B2203/06—Integration with other chemical processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas

Definitions

  • the present invention relates to a process for the treatment of waste in which the hydrogasification step is integrated with the reforming step.
  • the present invention makes it possible to recover energy from waste and produce, at discretion, hydrogen (3 ⁇ 4 ) and/or methane (CPU).
  • the process of the present invention has the further advantage of being set up to produce PU and CPU as fuels with "green” energy content, as they are obtained with the use of a renewable energy source (e.g. solar energy) and without resulting in the emission of pollutants into the environment.
  • a renewable energy source e.g. solar energy
  • the fed methane is first purified of contaminants (possible deactivators for the catalysts used) and mixed with water steam before entering the catalytic reactor.
  • the reaction (1) is very endothermic and is commonly carried out in large industrial furnaces where high process temperatures are reached by combustion of gaseous fuels.
  • the mixture produced, consisting of CO and H 2 (synthesis gas) is cooled and sent to Water-Gas Shift (WGS) reactors where the reaction (2) is carried out that allows CO to be converted into C0 2 and thus increase the production of hydrogen.
  • GSS Water-Gas Shift
  • steam reforming represents the most widely used industrial process for converting methane into hydrogen with the highest conversion yields, it suffers from the limitation due to high endothermicity.
  • the possibility of feeding the steam reforming process with "zero emissions" heat for example through heat derived from solar systems or from electricity produced from other sources with low environmental impact, has been under consideration for several years.
  • the problem relative to waste disposal is becoming more and more pressing year after year.
  • technologies for the processing and the valorisation of waste have been developed for years, it is still extremely difficult to date to effectively use these technologies.
  • the methods for the treatment of waste implemented to date suffer from the problem that they can lead to the emission of harmful substances into the environment and, for this reason, they meet with the hostility from the population living near the sites where the relevant plants should be built.
  • many of the waste treatments available to date requiring a constant supply of energy and reacting substances, do not result in a cost-effective energy gain.
  • the inventors of the present invention have developed a process and a relative plant capable of integrating the hydrogasification of carbon-based waste with methane reforming, to produce at the complete discretion of the process operator 3 ⁇ 4 and/orCIU depending on the convenience.
  • the process object of the present invention thanks to the integration of the reforming with the hydrogasification, can be self-sufficient in terms of reacting substances to be used.
  • Aim of the present invention is a process for the treatment of waste, the main characteristics of which are set forth in independent Claim 1, and the secondary and auxiliary characteristics of which are set forth in dependent Claims 2 - 7.
  • a further aim of the present invention is a plant for the treatment of waste, the main features of which are set forth in independent Claim 8, and the secondary and auxiliary features of which are set forth in dependent Claims 9 - 15.
  • the plant 1 substantially comprises a hydrogasification reactor 2 (C + 23 ⁇ 4 CPU), a reforming reactor 3 (CPU + H2O CO + 3H2) and a carbon monoxide conversion reactor 4 (CO + H2O C0 2 + H 2) .
  • the typical composition of the RDS can vary greatly from case to case: in the following analysis the composition of a RDS reported in % by weight in Table I was used.
  • Table I Elemental composition of ash-free dried RDS.
  • Such a composition could, for example, derive from a heterogeneous mass in which an organic fraction with polymeric compounds such as polyethylene, polypropylene, polyethylene terephthalate (PET), PVC, nitrogenous (mainly derived from textiles, such as nylon) and sulfurized (e.g. from rubbers) polymers, as well as aromatic substances, prevails.
  • polymeric compounds such as polyethylene, polypropylene, polyethylene terephthalate (PET), PVC, nitrogenous (mainly derived from textiles, such as nylon) and sulfurized (e.g. from rubbers) polymers, as well as aromatic substances, prevails.
  • RDF enter the plant according to the composition in Table I, and that the hydrogasification reactor 2 is fed with stoichiometric hydrogen (3 ⁇ 4) to allow a quantitative conversion of the RDF components in the Gibbs reactor.
  • stoichiometric hydrogen 3 ⁇ 4
  • a stream of 29 kmol/h (650 Nm 3 /h) of H2 was assumed.
  • the hydrogasification reactor 2 was modelled as a Gibbs reactor, whose products, in addition to those present in the starting RDF and to 3 ⁇ 4, may be CtU, H2O, CO, C0 2 , HC1, NH 3 , H 2 S.
  • Table II shows the material balance (kmol/h) and the specifications of the streams of the reagents (RDF and 3 ⁇ 4) and of the products.
  • the RDS stream will be referred to as the RDS leading line
  • the 3 ⁇ 4 stream will be referred to as the "a-fh" leading line (3 ⁇ 4 supply) while the stream of the products exiting the hydrogasification reactor 2 is referred to as the leading line 5.
  • the CtU-rich stream exiting the hydrogasification reactor 2 is sent via the leading line 5 to a mixer 6 where it is mixed with water steam superheated to 250°C and 10 bar and produced in a steam generator 7.
  • a gaseous stream containing any unrecovered 3 ⁇ 4 residues, as well as unconverted CtU and CO in the reforming 3 and carbon monoxide conversion 4 reactors, respectively, is also sent to the mixer 6.
  • the reforming reactor 3 is fed with a gaseous stream characterized by a H 2 O/CH 4 molar ratio equal to about 3.
  • the presence of a purification unit (not shown in the figure) will be required to rectify the content of potential contaminants (e.g. nitrogenous, chlorinated, sulfurized compounds, etc.). It is preferred that the purification unit operates at high temperatures (> 200°C) in order to avoid condensation and re-evaporation of the residual water steam with the obvious advantages in terms of productivity and energy efficiency that this entails.
  • potential contaminants e.g. nitrogenous, chlorinated, sulfurized compounds, etc.
  • a gaseous stream at a temperature of 850°C flows out of the reforming reactor 3 which, through a leading line 9, feeds the carbon monoxide conversion reactor 4.
  • the leading lines 8 and 9 engage a heat exchanger 10 to allow a recovery of the heat of the gaseous stream exiting the reforming reactor 3.
  • the presence of the heat exchanger 10 divides each of the leading lines 8 and 9 into a respective upstream branch (8a and 9a) and into a respective downstream branch (8b and 9b) of the heat exchanger 10.
  • Table III reports the specifications of the streams of the leading lines 8 and 9 and of the stream exiting the carbon monoxide conversion reactor 4 through a leading line 11.
  • the stream exiting the carbon monoxide conversion reactor 4 is sent to a carbon dioxide separation unit (C0 2) 12, from which a CO2 stream is produced which through the leading line 13 is transported outside the plant 1.
  • the gaseous mixture separated from CO2 in the carbon dioxide separation unit 12 is sent via a leading line 14 to a hydrogen separation unit 15.
  • the hydrogen exiting the separation unit 15 is conveyed in a leading line 16.
  • a mixture is also obtained composed of any residues of unrecovered hydrogen, water, as well as unreacted methane and carbon monoxide respectively in the reforming 3 and carbon monoxide conversion 4 reactors. This mixture is sent to the mixer 6 through a leading line 17.
  • the separation unit 15 can operate both at low temperature and at high temperatures (> 200°C).
  • the high temperatures have the advantage of avoiding the condensation and re-evaporation of the water steam sent in excess and, therefore, not converted in the reforming reactor 3 and in the CO conversion reactor 4, with the obvious advantages in terms of productivity and energy efficiency that this entails.
  • the leading line 16 branches into a hydrogen leading line 18 towards the outside of the plant 1 and into the a-H 2 leading line previously described and characterized in Table II.
  • the leading line 18 represents the net production of hydrogen by the process according to the present invention.
  • Table IV reports the specifications of the streams of the leading lines 13, 14, 16, 17 and 18
  • the system has two energy-consuming units: steam generator 7, with a gross load equal to 924 kW of heat to be supplied at 250°C reforming reactor 3 with a demand equal to 1151 kW of heat to be supplied at 850°C
  • the process also has two exothermic units operating at temperatures 3300°C, whose heat can then be recovered to (partially) feed the steam generator 7: the hydrogasification reactor releases 484 thermal kW at 300°C the CO conversion reactor releases 317 thermal kW at 350°C
  • the proposed process requires 1274 kW of heat from renewable heat source to produce 3890 kW of "clean" fuel, in the form of heating power of 3 ⁇ 4 .
  • the process therefore results in a "net gain” in terms of "thermal power” equal to 2616 kW, corresponding, therefore, to more than 200% valorisation of the renewable energy (in the case of an electrolysis process the net energy gain is about 60-70%).
  • the process has a high efficiency: a RDS can have a heating power of the order of 23-31 MJ/kg. Therefore, 10 tons/day correspond to a thermal power input of around 2600-3600 kW and an energy efficiency of renewable energy conversion + RDS into hydrogen ranging between 80% and 99% is obtained.
  • hydrogasification reaction is exothermic, while the pyrolysis reaction is endothermic, which benefits the energy balance of the process as a whole.
  • 33% of 3 ⁇ 4 produced is recycled to feed the hydrogasification reactor 2, while the remaining represents a net production of hydrogen.
  • the possibility of removing CO2 in the unit 12 and 3 ⁇ 4 in the unit 15 under conditions of high temperature, at least higher than the dew temperature of the gaseous mixture in the leading line 11, would allow to avoid condensation and re-evaporation of residual H2O in this stream, resulting in a reduction of the thermal load on the steam generator 7 and, therefore, a further increase in the efficiency of the process as a whole.
  • the process of the present invention also has the great advantage that it can also treat waste in wet form. Such a possibility would allow the hydrogasification reactor 2 to be operated in an almost autothermal way (zeroing the heat to be removed) with an easier control of the temperature and reduction of plant costs.
  • the H2O present in the starting RDF could absorb the reaction heat of the hydrogasification reactor 2, be vaporized and, therefore, reduce the thermal load at the steam generator 7 in addition to the plant costs for the thermal recovery from the hydrogasification reactor 2 which could be operated in an almost autothermal manner.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Processing Of Solid Wastes (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

L'invention concerne un procédé de traitement de déchets, comprenant une étape d'hydrogazéification, pendant laquelle une masse de déchets à base de carbone est amenée à réagir avec de l'hydrogène à une température allant de 250 à 500°C et à une pression allant de 1 à 50 bars pour la production de méthane par réaction exothermique ; une étape de reformage, au cours de laquelle au moins une partie du méthane produit par l'étape d'hydrogazéification est amenée à réagir avec de l'eau à une température allant de 400 à 1000°C et à une pression allant de 1 à 40 bars pour la production d'hydrogène et de monoxyde de carbone ; au moins une partie de l'hydrogène produit par l'étape de reformage étant introduite dans l'étape d'hydrogazéification.
PCT/IB2022/056268 2021-07-09 2022-07-07 Méthode et installation pour le traitement de déchets à base de carbone WO2023281426A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP22747757.7A EP4367057A1 (fr) 2021-07-09 2022-07-07 Méthode et installation pour le traitement de déchets à base de carbone

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT102021000018125 2021-07-09
IT102021000018125A IT202100018125A1 (it) 2021-07-09 2021-07-09 Processo e impianto di trattamento dei rifiuti a matrice carboniosa

Publications (1)

Publication Number Publication Date
WO2023281426A1 true WO2023281426A1 (fr) 2023-01-12

Family

ID=77802193

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2022/056268 WO2023281426A1 (fr) 2021-07-09 2022-07-07 Méthode et installation pour le traitement de déchets à base de carbone

Country Status (3)

Country Link
EP (1) EP4367057A1 (fr)
IT (1) IT202100018125A1 (fr)
WO (1) WO2023281426A1 (fr)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4822935A (en) * 1986-08-26 1989-04-18 Scott Donald S Hydrogasification of biomass to produce high yields of methane
WO2006022687A2 (fr) * 2004-08-03 2006-03-02 The Regents Of The Universtiy Of California Procede de pyrolyse de vapeur ameliorant l'hydro-gazeification de matieres carbonees
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US20160304799A1 (en) * 2009-11-18 2016-10-20 G4 Insights Inc. Method and system for biomass hydrogasification

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4822935A (en) * 1986-08-26 1989-04-18 Scott Donald S Hydrogasification of biomass to produce high yields of methane
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
WO2006022687A2 (fr) * 2004-08-03 2006-03-02 The Regents Of The Universtiy Of California Procede de pyrolyse de vapeur ameliorant l'hydro-gazeification de matieres carbonees
US20160304799A1 (en) * 2009-11-18 2016-10-20 G4 Insights Inc. Method and system for biomass hydrogasification

Also Published As

Publication number Publication date
EP4367057A1 (fr) 2024-05-15
IT202100018125A1 (it) 2023-01-09

Similar Documents

Publication Publication Date Title
Frattini et al. A system approach in energy evaluation of different renewable energies sources integration in ammonia production plants
US20120232173A1 (en) High Energy Power Plant Fuel, and CO or CO2 Sequestering Process
GB2545474A (en) Integrated system and method for producing methanol product
US9856426B2 (en) Combined processes for utilizing synthesis gas with low CO2 emission and high energy output
US20080132588A1 (en) Apparatus and methods for the production of ammonia and fischer-tropsch liquids
US20130331469A1 (en) Method and Apparatus for Reducing CO2 in a Stream by Conversion to a Syngas for Production of Energy
RU2127720C1 (ru) Синергетический способ производства метанола (варианты)
WO2008067221A1 (fr) Procédés et appareils améliorés de production de combustible synthétique
US20220348461A1 (en) Process for the conversion of carbon dioxide
WO1999055618A1 (fr) Procede et appareil de production de gaz de synthese
WO2011021944A1 (fr) Procédés combinés permettant d'utiliser un gaz de synthèse à faible émission de co2 et à rendement énergétique élevé
US9850185B2 (en) Method and system for acetylene (C2H2) or ethylene (C2H4) production
EA018619B1 (ru) Способ получения синтез-газа и метанола из органических отходов
CN113402362B (zh) 化学制氢的co2零排放煤制甲醇***和方法及应用
AU2021281029A1 (en) Circular carbon process
WO2023281426A1 (fr) Méthode et installation pour le traitement de déchets à base de carbone
EP3434753B1 (fr) Procédé de production de méthane à partir de combustible dérivé
WO2020234709A1 (fr) Four et procédé de production de gaz de synthèse
EP3992267B1 (fr) Unité de conversion de co pour convertir des déchets solides en gaz de synthèse
CN113272410B (zh) 由废弃物生产生物甲烷的方法和设备
Mastellone et al. Waste Recovery and Decarbonization: a Sustainable Synergy
Iaquaniello et al. An Overview of Today’s Industrial Processes to Make Hydrogen and Future Developments’ Trend
WO2024002442A1 (fr) Production de gaz de synthèse à partir de déchets

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 22747757

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2022747757

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2022747757

Country of ref document: EP

Effective date: 20240209