WO2016016253A1 - Procédé intégré de reformage par oxydation catalytique partielle/chauffé au gaz à temps de contact court pour la production de gaz de synthèse - Google Patents

Procédé intégré de reformage par oxydation catalytique partielle/chauffé au gaz à temps de contact court pour la production de gaz de synthèse Download PDF

Info

Publication number
WO2016016253A1
WO2016016253A1 PCT/EP2015/067292 EP2015067292W WO2016016253A1 WO 2016016253 A1 WO2016016253 A1 WO 2016016253A1 EP 2015067292 W EP2015067292 W EP 2015067292W WO 2016016253 A1 WO2016016253 A1 WO 2016016253A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
compounds
process according
synthesis
partial oxidation
Prior art date
Application number
PCT/EP2015/067292
Other languages
English (en)
Inventor
Luca Eugenio Basini
Original Assignee
Eni S.P.A.
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 Eni S.P.A. filed Critical Eni S.P.A.
Publication of WO2016016253A1 publication Critical patent/WO2016016253A1/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
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • 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
    • C01B2203/061—Methanol production
    • 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
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • 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
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • 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
    • C01B2203/1258—Pre-treatment of the feed
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • C01B2203/1264—Catalytic pre-treatment of the feed
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/141—At least two reforming, decomposition or partial oxidation steps in parallel
    • 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
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • 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

Definitions

  • This invention relates to a process for the production of synthesis gas through a process integrating short contact time Catalytic Partial Oxidation (CPO) technology with Gas Heated Reforming (GHR) technology.
  • CPO Catalytic Partial Oxidation
  • GHR Gas Heated Reforming
  • intervals always include the end members unless specified otherwise.
  • Synthesis gas is produced by Steam Reforming (SR) technology and by Non-catalytic Partial Oxidation (POx) and Autothermal Reforming (ATR) technologies.
  • SR Steam Reforming
  • POx Non-catalytic Partial Oxidation
  • ATR Autothermal Reforming
  • a relatively recent variant of the SR process is Gas Heated Reforming (GHR) which at least partly replaces the radiant heat required for the endothermic reactions with a convective source: typically the hot gas produced by combustion reactions and/or the synthesis gas itself produced by an ATR at high temperature.
  • GHR Gas Heated Reforming
  • the ATR and SR or GHR technologies are integrated into schemes known as Combined Reforming (CR).
  • SCT-CPO Short Contact Time - Catalytic Partial Oxidation
  • Synthesis gas is used in many industrial processes, among which we would mention the synthesis of ammonia and urea, the production of H 2 for refining and fuels production, the synthesis of methanol and its derivatives, and the synthesis of liquid hydrocarbons by the Fischer-Tropsch (F-T) process. Synthesis gas is also used in fine chemical processes, and in the electronics, metal refining, glass and food industries. These many industrial uses require the synthesis gas is produced with very different compositions in order to minimize recycling and improve overall yields.
  • Table 1 describes the main reactions involved in the processes for the production of synthesis gas and Table 2 shows the compositional characteristics of the synthesis gas required by their main uses.
  • CPO Catalytic Partial Oxidation
  • EP 2142467 describes a combined process in which a gaseous hydrocarbon mixture reacts with steam in an endothermal adiabatic pre-reformer and the product, the pre- reformate, is divided into three streams fed to a Steam Methane Reformer (SMR), a Gas Heated Reformer (GHR) and an Autothermal Reformer (ATR) operating in parallel.
  • SMR Steam Methane Reformer
  • GHR Gas Heated Reformer
  • ATR Autothermal Reformer
  • EP 1622827 describes a process for the production of synthesis gas from carbon- containing material, preferably comprising natural gas or gaseous hydrocarbon feedstock, refinery gas and more generally gas streams containing compounds having up to 4 carbon atoms, which provides for: (a) a stage of partial oxidation of the carbon-containing material performed in a reactor in which a burner is present in the upper part (therefore an ATR or POx reactor) thus obtaining a first mixture of hydrogen and carbon monoxide;
  • EP 1403216 describes a process for the production of synthesis gas in which a series of catalytic steam reforming units are in parallel with an AutoThermal Reforming unit.
  • the heat required by the SR passages is again in this case provided by combustion of the outflows from the various SR and ATR.
  • the final mixture of outflows obtained by adding the synthesis gas produced by the convectively heated SR processes and ATR processes has an H 2 /CO ratio of between 1 .8 and 2.3 v/v.
  • WO 2008017741 describes a process for the production of liquid hydrocarbons from biomass, coal, lignite and petroleum residues boiling at a temperature over 340°C, the said process comprising at least:
  • FT Fischer-Tropsch
  • Adiabatic endothermic "pre-reforming" reactors are often inserted upstream of the SR and ATR reactors. These reactors are described in various documents in the literature, including "T.S. Christensen, Appl. Catal. A: 138(1996)285" e “I. Dybkjaer, Fuel Process. Techn. 42(1995)85”.
  • the "pre-reformers” make it possible to convert the C2+ carbons present in the gaseous hydrocarbon streams into CO, H 2 and CH 4 at relatively low temperatures (approximately 550°C), reducing the possibility of the occurrence of other parasitic formation reactions [7-9] in the subsequent passes through SR or ATR. In particular reactions [10-1 1] which accompany the Water Gas Shift (WGS) reaction [5] take place in the endothermic "pre-reforming" reactors.
  • WGS Water Gas Shift
  • the adiabatic endothermic "pre-reforming" reactors are typically fed with a mixture of gaseous reagents and steam preheated in a furnace at approximately 550°C.
  • a catalyst based on Ni is (in most cases) used to complete reactions [10-11 ] in the adiabatic endothermic "pre-reforming” reactor.
  • the mixture of pre-reformed gas is then passed to the reforming reactor and has lesser thermodynamic affinity towards the reactions forming carbon-containing residues through reactions [7-9]. This makes it possible to reduce the steam/carbon (Steam/C v/v) and/or Oxygen/Carbon (O2/C) ratios in the feeds to the SR or ATR reactors, increasing their energy efficiency (W.D. Verduijin Ammonia Plant Saf.
  • pre-reforming units also makes it possible to increase the flexibilities of SR and ATR technologies in relation to the composition of the feedstock; for example it makes it possible to use feedstocks from refinery gases to naphthas.
  • feedstocks from refinery gases to naphthas.
  • adiabatic endothermic "pre-reforming” technology can increase the production capacity of plants without requiring significant changes in the characteristics of the reforming unit.
  • the technologies for the production of synthesis gas are used in many industrial processes to produce different products. It is therefore desirable to be able to have a process for the production of synthesis gas which is flexible with regard to both the composition of the reagent feedstock, production capacity, and the quality of the synthesis gas produced. At the same time it is very important to use processes having high energy efficiency with low carbon dioxide emissions, which require smaller capital costs than conventionally used technologies.
  • this patent application provides an integrated process for the production of synthesis gas which combines Short Contact Time Partial Catalytic Oxidation (SCT- CPO) technology with Gas Heated Reforming (GHR) technology.
  • SCT- CPO Short Contact Time Partial Catalytic Oxidation
  • GHR Gas Heated Reforming
  • the object of this invention therefore comprises an integrated process for the production of synthesis gas comprising the following stages:
  • This configuration therefore makes use of the possibility offered by SCT-CPO technology to use different types of feedstocks, both liquid and gaseous, which cannot be used in GHR technologies, maintaining the high energy efficiency characteristics of catalytic conversions and thus using them in the production of synthesis gas.
  • This process configuration therefore consider a scheme in which the SCT-CPO stage and a GHR stage operate in a parallel in such a way as to allow the use of compounds which GHR technology is incapable of converting for the production of synthesis gas, in particular liquid and gaseous hydrocarbons, and compounds deriving from biomass which are also mixed together which cannot be used in either SR processes or ATR processes.
  • This patent application relates to an integrated process for the production of synthesis gas comprising the following stages:
  • the stream containing oxygen may be oxygen, air or enriched air.
  • this process provides for a further pre-reforming stage upstream of either the SCT-CPO section, or the GHR section, or both.
  • the said pre-reforming stage may be either exothermic adiabatic or endothermic adiabatic, and in particular the following combinations are described here: adiabatic exothermic pre-reformer upstream of the GHR and upstream of the SCT- CPO, or
  • the first and second hydrocarbon gas streams may be fed to either an adiabatic exothermic pre-reformer or an adiabatic endothermic pre-reformer. This is regardless of the fact whether these pre- reformers are upstream of either the GHR or the SCT-CPO.
  • the third stream containing gaseous compounds in which the said gaseous compounds are selected from hydrocarbons other than natural gas and/or refinery gas or from gaseous compounds which can also be obtained from biomass, can be fed to either an adiabatic exothermic pre-reformer or an adiabatic endothermic pre-reformer located upstream of a SCT-CPO.
  • the third stream containing liquid compounds in which the said liquid compounds are selected from hydrocarbons or compounds of various nature deriving from biomass, or mixtures thereof, may be fed to only one adiabatic exothermic pre-reformer located upstream of a SCT-CPO.
  • the third stream contains both liquid compounds and gaseous compounds these can be fed to only one adiabatic exothermic pre-reformer located upstream of a SCT- CPO.
  • the pre-reforming stage gives rise to a flow of reformate which is subsequently fed to the SCT-CPO and/or GHR sections.
  • An adiabatic exothermic pre-reforming reactor benefits from the same principles as the SCT-CPO process as described for example in ITMI20120418.
  • the pre-reforming sections may be separate and each located upstream of the GHR and SCT-CPO sections.
  • the first and second synthesis gases are cooled through a heat exchanger device generating steam.
  • the steam generated is used as a reagent in either the Gas Heated Reforming section or the short contact time Partial Catalytic Oxidation section.
  • the excess steam is instead used for external purposes (export steam).
  • the first gaseous stream selected from natural gas and/or refinery gas contains sulfur compounds, then this may undergo a hydrodesulfurisation treatment before being passed to the pre-reformer sections or to the GHR and SCT-CPO sections.
  • the product containing H 2 and CO obtained after reaction in the GHR and SCT-CPO sections may be used for the synthesis of liquid hydrocarbons by the Fischer-Tropsch process, or for the synthesis of methanol, or for the synthesis of ammonia.
  • the integrated process described and claimed may also provide for a stage in which the first and second synthesis gases are reacted, after cooling, according to a water gas shift (WGS) reaction, followed by a stage of separation or purification for the production of H 2 .
  • WGS water gas shift
  • Industrial solutions incorporating SCT-CPO processes, GHR processes and methanol synthesis benefit from the advantage deriving from the integration between GHR and SCT-CPO technology, which makes it possible to avoid the excess hydrogen production that occurs when only GHR technology is used.
  • the produced mixture of hydrogen and carbon monoxide would have an H 2 /CO ratio greater than 3 v/v, preferably over 3.5 v/v, and in addition to this it would be difficult to reduce the values for methane residue in the "dry" synthesis gas (that is without steam) produced by GHR technology alone below 3% v/v. If therefore a single GHR reactor is used to produce synthesis gas for the synthesis of methanol, it would be obtained a mixture having an H 2 content (approximately 30% of the hydrogen produced would be superfluous) and a CH 4 content which it would be desirable to reduce in order to improve the energy efficiency of the whole system
  • the integrated process according to the present invention it is instead possible to obtain a hydrogen and carbon monoxide mixture in which the H 2 /CO ratio lies between 1.8 and 3.5 v/v; this improves the efficiency of the methanol synthesis process because it reduces the volume of the recycling loop in the MeOH synthesis and the purge of H 2 and CH 4 .
  • the greater efficiency of the system for producing and using synthesis gas also makes it possible to reduce C0 2 emissions.
  • the methanol modulus is defined by the equation:
  • NH 3 is produced by feeding to a SR reactor desulfurised natural gas mixed with steam.
  • the synthesis gas so produced is passed to a "secondary reformer", typically an ATR which uses air as oxidant.
  • the synthesis gas obtained contains H 2 , CO, N 2 , C0 2 and a small CH 4 residue (typically less than 1% on a volumetric basis).
  • This mixture then undergoes WGS treatment in which CO is almost completely converted into C0 2 and H 2 .
  • the subsequent stage provides for cooling the synthesis gas after WGS and removing the C0 2 (typically by "chemical scrubbing" with amine).
  • the stream obtained in this way is passed to a "methanator” in which the C0 2 and the residual CO are converted into CH 4 .
  • the mixture so obtained which mainly contains H 2 and N 2 in a ratio of
  • Figures 1-6 describe some preferred embodiments of this invention.
  • Figure 1 describes a process arrangement in which a first stream of refinery gas and/or natural gas, and their mixtures, (2), is desulfurised in a hydrodesulfurisation unit (6).
  • This desulfurised stream is divided into two parts; one part is passed to a GHR after being mixed with steam (1 ) and the other part is mixed with a second mixture containing a second stream of gaseous reagents different from first stream (2) and/or liquid compounds and/or compounds deriving from biomass which cannot normally be processed in a GHR reactor but can be converted in a SCT-CPO reactor.
  • An oxidant stream (4) and steam (5) are fed to this mixture.
  • the first reaction product (30) leaving the SCT-CPO is passed at high temperature to the GHR reactor as a thermal vector, convectively heating it, and thus making it possible to produce synthesis gas (31 ).
  • Streams (30) and (31 ) are recombined and cooled in a syngas cooler (SGC) at temperatures below 400°C forming the final synthesis gas (13), generating steam which is delivered as a feed (1 , 5) or exported for other uses (1 1 , 12).
  • SGC syngas cooler
  • Figure 2 describes a process arrangement similar to that in Figure 1 but which includes exothermic adiabatic pre-reforming (14), for example having the characteristics as described in ITMI20120418 which make it possible to convert the heavier fraction of the feedstock fed to the SCT-CPO reactor.
  • Figure 3 describes a process arrangement similar to that in Figure 1 or 2 in which both the reagent mixtures are treated in pre-reforming sections, an adiabatic endothermic one (15) and an adiabatic exothermic one (14) respectively, before being passed to the GHR and SCT-CPO reactors.
  • Figure 4 describes integration of the process according to this invention with a Fischer- Tropsch section (18).
  • the synthesis gas is produced using the arrangement in Figure 3 and passed to a F-T reactor (18) to produce a mixture of liquid and gaseous hydrocarbons having a high middle distillates content (21 ).
  • the arrangement provides that part (20) of the "recycle loop" (19) of the FT reactor is recycled as a feed to the SCT- CPO reactor.
  • Figure 5 describes integration of the process according to this invention with a methanol synthesis section.
  • the synthesis gas produced following the arrangement in Figure 3 is subsequently compressed (16) and passed to a methanol synthesis reactor (17) and the methanol produced (24) is then obtained pure after distillation treatment (23).
  • Figure 6 describes integration of the process according to this invention with an ammonia synthesis section.
  • the synthesis gas produced by means of an arrangement described in Figure 3 undergoes Water Gas Shift treatment (25) to remove the CO 2 (26) and methanation treatment (27) before being compressed (16) and passed to the ammonia synthesis reactor (28).
  • the streams of the Iatter (29) and C0 2 (21 ) can be obtained with the best stoichiometry for use in urea synthesis processes.

Abstract

La présente invention concerne un procédé intégré pour la production de gaz de synthèse comportant les étapes suivantes : a) diviser un flux d'hydrocarbures gazeux, comprenant de préférence du gaz naturel et/ou un gaz de raffinerie, en un premier et un deuxième flux, b) mélanger ledit deuxième flux avec un flux contenant de l'oxygène, de la vapeur d'eau et éventuellement du CO2, et éventuellement un troisième flux contenant des composés liquides et/ou gazeux, lesdits composés gazeux étant choisis parmi des hydrocarbures autres que le gaz naturel et/ou un gaz de raffinerie, ou parmi ces composés qui sont dérivés également d'une biomasse, et lesdits composés liquides étant choisis parmi des hydrocarbures ou des composés de diverse nature étant dérivés d'une biomasse, ou des mélanges de ceux-ci, c) amener le mélange obtenu en (b) à réagir dans une section d'Oxydation Catalytique Partielle à temps de contact court pour former un premier gaz de synthèse, d) amener le premier flux gazeux, sélectionné de préférence parmi le gaz naturel et/ou un gaz de raffinerie, à réagir avec de la vapeur dans une section de Reformage Chauffée au Gaz pour produire un deuxième gaz de synthèse, et chauffer par convection le réacteur de Reformage Chauffé au Gaz au moyen du premier gaz de synthèse obtenu dans la section d'Oxydation Catalytique Partielle à temps de contact court.
PCT/EP2015/067292 2014-07-29 2015-07-28 Procédé intégré de reformage par oxydation catalytique partielle/chauffé au gaz à temps de contact court pour la production de gaz de synthèse WO2016016253A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI2014A001370 2014-07-29
ITMI20141370 2014-07-29

Publications (1)

Publication Number Publication Date
WO2016016253A1 true WO2016016253A1 (fr) 2016-02-04

Family

ID=51589400

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2015/067292 WO2016016253A1 (fr) 2014-07-29 2015-07-28 Procédé intégré de reformage par oxydation catalytique partielle/chauffé au gaz à temps de contact court pour la production de gaz de synthèse

Country Status (1)

Country Link
WO (1) WO2016016253A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT202100011189A1 (it) 2021-05-03 2022-11-03 Nextchem S P A Processo a basso impatto ambientale per la riduzione di minerali ferrosi in altoforno impiegante gas di sintesi
IT202100012551A1 (it) 2021-05-14 2022-11-14 Rosetti Marino S P A Processo per la conversione della co2
WO2022263409A1 (fr) 2021-06-14 2022-12-22 NextChem S.p.A. Procédé de production de catalyseurs pour procédés chimiques à haute température et catalyseurs ainsi obtenus

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1770059A1 (fr) * 2005-09-21 2007-04-04 Institut Français du Pétrole Procédé de production de gaz de synthèse par vaporéformage et oxydation partielle
US20080275143A1 (en) * 2003-03-16 2008-11-06 Kellogg Brown & Root Llc Catalytic Partial Oxidation Reforming for Syngas Processing and Products Made Therefrom
WO2011072877A1 (fr) * 2009-12-16 2011-06-23 Eni S.P.A. Procédé de production d'hydrogène à partir d'hydrocarbures liquides, gazeux et/ou de composés oxygénés également issus de biomasses
WO2013062415A1 (fr) * 2011-10-26 2013-05-02 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production de syngaz pour la production de méthanol
WO2013095130A1 (fr) * 2011-12-19 2013-06-27 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production d'ammoniac et d'urée

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080275143A1 (en) * 2003-03-16 2008-11-06 Kellogg Brown & Root Llc Catalytic Partial Oxidation Reforming for Syngas Processing and Products Made Therefrom
EP1770059A1 (fr) * 2005-09-21 2007-04-04 Institut Français du Pétrole Procédé de production de gaz de synthèse par vaporéformage et oxydation partielle
WO2011072877A1 (fr) * 2009-12-16 2011-06-23 Eni S.P.A. Procédé de production d'hydrogène à partir d'hydrocarbures liquides, gazeux et/ou de composés oxygénés également issus de biomasses
WO2013062415A1 (fr) * 2011-10-26 2013-05-02 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production de syngaz pour la production de méthanol
WO2013095130A1 (fr) * 2011-12-19 2013-06-27 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production d'ammoniac et d'urée

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
CHRISTENSEN ET AL: "Adiabatic prereforming of hydrocarbons - an important step in syngas production", APPLIED CATALYSIS A: GENERAL, ELSEVIER SCIENCE, AMSTERDAM, NL, vol. 138, no. 2, 9 May 1996 (1996-05-09), pages 285 - 309, XP022250773, ISSN: 0926-860X, DOI: 10.1016/0926-860X(95)00302-9 *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT202100011189A1 (it) 2021-05-03 2022-11-03 Nextchem S P A Processo a basso impatto ambientale per la riduzione di minerali ferrosi in altoforno impiegante gas di sintesi
WO2022233769A1 (fr) 2021-05-03 2022-11-10 NextChem S.p.A. Procédé d'utilisation de gaz de synthèse pour améliorer l'impact environnemental de la réduction de minerai de fer dans des hauts fourneaux
IT202100012551A1 (it) 2021-05-14 2022-11-14 Rosetti Marino S P A Processo per la conversione della co2
WO2022263409A1 (fr) 2021-06-14 2022-12-22 NextChem S.p.A. Procédé de production de catalyseurs pour procédés chimiques à haute température et catalyseurs ainsi obtenus

Similar Documents

Publication Publication Date Title
US9115045B2 (en) Method and system for producing methanol using an oxygen transport membrane based reforming system
US11649163B2 (en) Chemical synthesis plant
CA2787482C (fr) Procede pour le reformage d'hydrocarbures
KR102596309B1 (ko) 합성 가스의 제조 방법
ZA200508859B (en) Production of hydrocarbons by steam reforming and Fischer-Tropsch reaction
CA2939769C (fr) Procede de production de gaz de synthese
US20140357737A1 (en) Synthesis gas and fischer tropsch integrated process
JP5539517B2 (ja) メタノール製造のための複合改質プロセス
CA2914871C (fr) Methode et systeme pour produire du methanol par oxydation partielle
DK2723676T3 (en) PROCEDURE FOR MANUFACTURING AMMONIAK AND UREA
WO2016016251A1 (fr) Procédé de production sct-cpo/sr intégré pour la production de gaz de synthèse
WO2013013895A1 (fr) Procédé de production de gaz de synthèse
WO2016016256A1 (fr) Procédé intégré d'oxydation catalytique partielle à temps de contact court/reformage autotherme (sct-cpo/atr) pour la production de gaz de synthèse
CN113498403A (zh) 化学合成设备
WO2016016253A1 (fr) Procédé intégré de reformage par oxydation catalytique partielle/chauffé au gaz à temps de contact court pour la production de gaz de synthèse
EP4228999A1 (fr) Étage de gaz de synthèse pour usine de synthèse chimique
WO2015128456A1 (fr) Procédé de production de gaz de synthèse
WO2016016257A1 (fr) Procédé intégré d'oxydation catalytique partielle à temps de contact court pour la production de gaz de synthèse
NO314691B1 (no) Fremgangsmåte og reaktor for fremstilling av hydrogen og syntesegass
WO2022218854A1 (fr) Formation de poussière métallique réduite dans un reformeur à tubes à baïonnette
CA3192110A1 (fr) Methode de chauffage d'une alimentation en gaz naturel destinee a un reformeur a vapeur et systeme et utilisation associes

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: 15750947

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 15750947

Country of ref document: EP

Kind code of ref document: A1