WO2015131818A1 - Formulation de peinture et son procédé de fabrication - Google Patents

Formulation de peinture et son procédé de fabrication Download PDF

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Publication number
WO2015131818A1
WO2015131818A1 PCT/CN2015/073621 CN2015073621W WO2015131818A1 WO 2015131818 A1 WO2015131818 A1 WO 2015131818A1 CN 2015073621 W CN2015073621 W CN 2015073621W WO 2015131818 A1 WO2015131818 A1 WO 2015131818A1
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Prior art keywords
shift
synthesis gas
gas stream
gasifier
catalyst
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PCT/CN2015/073621
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English (en)
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WO2015131818A8 (fr
WO2015131818A9 (fr
Inventor
Daniel Chin
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L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
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Priority claimed from CN201510087950.7A external-priority patent/CN105084313B/zh
Priority claimed from CN201520116309.7U external-priority patent/CN204689634U/zh
Application filed by L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude filed Critical L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority to AU2015226629A priority Critical patent/AU2015226629B2/en
Publication of WO2015131818A1 publication Critical patent/WO2015131818A1/fr
Publication of WO2015131818A8 publication Critical patent/WO2015131818A8/fr
Publication of WO2015131818A9 publication Critical patent/WO2015131818A9/fr

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    • 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]
    • 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
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • 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
    • 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
    • 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
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
    • 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
    • C01B2203/0294—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing three or more CO-shift steps
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/169—Controlling the feed
    • C—CHEMISTRY; METALLURGY
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal

Definitions

  • This invention relates to a process for converting a carbon monoxide (CO) containing crude synthesis gas (syngas) stream by reacting the crude syngas with water in the presence of a catalyst according to the so-called CO shift or CO conversion reaction into a syngas stream depleted with regard to CO, but enriched with regard to hydrogen (H 2 ) and carbon dioxide (CO 2 ) . It is among the objects of the invention to provide methods for safely performing such reaction under varying syngas load, especially as a downstream operation of a multi-stage reformer plant or gasifier plant, wherein the different reformer stages or gasifier stages may not all be operated at the same time and/or the flow rate of the crude syngas received from the reformer stages or gasifier stages may vary.
  • the subject invention relates to a plant suited for performing the CO shift reaction, especially downstream of a multi-stage reformer or gasifier in an integrated reforming plant.
  • the subject invention relates to a method of starting up such plant, especially in situations where the different reformer stages or gasifier stages are started up successively.
  • CO shift reaction is per se well known in the technical field of chemical engineering. General concepts and applications of the CO shift reaction in the context of reforming plants or gasification plants can be found in textbooks like C.Higman and M. van der Burgt, Gasification, Chapter 8.3 “CO Shift” , Gulf Professional Publishing (Elsevier) 2003, or Ullmann′sEncyclopedia of Industrial Chemistry, Sixth Edition, 1998 Electronic Release, keyword “Ammonia”, chapter 4.5.1.2 “Carbon Monoxide Shift Conversion” , and keyword “Hydrogen” , chapter 4.1.2.2 “Gasification of Liquid and Gaseous Hydrocarbons” .
  • CO shift is widely applied in reformer plants designed to produce ammonia syngas, since for ammonia synthesis carbon oxides must be completely removed from the raw synthesis gas of the reforming or gasification process.
  • the CO shift reaction will operate with a variety of catalysts between 200 °C to 500 °C at sufficient reaction rates.
  • the types of catalyst are distinguished by their temperature range of operation and the quality, especially the sulfur content, of the syngas to be converted.
  • HT shift high temperature shift
  • iron oxide–based catalyst promoted typically with chromium and more recently with copper.
  • the operating range of these catalysts is between 300 and 500 °C. Much above 500 °C sintering of the catalyst occurs which leads to catalyst deactivation.
  • HT shift catalyst is tolerant of sulfur up to a practical limit of about 100 vol-ppm, but it is likely to lose mechanical strength, particularly if subjected to changing amounts of sulfur.
  • reaction is mostly performed in several stages, operated in series, with intermediate heat removal between the individual catalyst beds in which the reaction runs adiabatically, to avoid excessive catalyst temperatures and to have an advantageous equilibrium.
  • Low temperature shift operates in the temperature range from 200 °Cto 270 °C and uses a copper-zinc-aluminum catalyst. It is used in most steam reforming-based ammonia plants to reduce residual CO to about 0.3 mol-%, a requirement for a downstream methanator.
  • the catalyst used is highly sulfur-sensitive, and even with 0.1 vol-ppm H 2 S in the inlet gas, will over time become poisoned. Further the catalyst is also sensitive with regard to water condensation. Operation near the dewpoint will cause capillary condensation and consequent damage to the catalyst. With a dewpoint of about 215 °C and a temperature rise of 25 to 30 °C, there is not much margin for error below the upper temperature limit of 270 °C when recrystallization of the copper catalyst begins.
  • the gas from the secondary reformer cooled by recovering the waste heat for raising and superheating steam, enters the HT shift reactor filled with an iron–chromium catalyst at 320 to 350 °C. After a temperature increase of around 50 to 70 °C (depending on initial CO concentration) and with a residual CO content of around 3 %, the gas is then cooled to 200 to 210 °C for the LT shift, which is carried out on a copper–zinc–alumina catalyst in a downstream reaction vessel and achieves a carbon monoxide concentration of 0.1 to 0.3 vol-%.
  • SMR methane steam reforming
  • a cobalt-molybdenum catalyst for applications where it is desired to perform CO shift on raw syngas, a cobalt-molybdenum catalyst, variously described as a “sour shift” or “dirty shift” catalyst, can be used.
  • the catalyst is sulfur tolerant since it requires sulfur in the feed gas to maintain it in the active sulfided state. It is generally applied after a water quench of the raw syngas, which typically will provide a gas at about 250 °C saturated with sufficient water to conduct the shift reaction without any further steam addition.
  • the raw gas shift is typically configured as two or three adiabatic beds with intermediate cooling resulting in a residual CO of about 1.6 or 0.8 mol-%, respectively.
  • each subreactor comprises a multitude, for example two, catalyst beds with an internal bypass around the first catalyst bed in direction of gas flow. Typically there is also another main bypass line across both parallel first shift subreactors. This design is shown schematically in figure 1.
  • this setup is often controlled manually by limiting the rawgas flowrate through each catalyst bed by adjusting a manual valve for the respective flow path.
  • the sound application of this method depends on operator experience; thus, chances of undesired temperature overshooting in the reactors is relatively high.
  • a further disadvantage is can be seen in the additional investment costs required for the reactor design because of double layers of catalyst bed, supporting means for the latter, and large isolation valves together with extra piping to control the flow in the main and bypass lines.
  • the aforementioned object is solved with the invention according to claim 1 substantially with a process for producing a treated synthesis gas, containing carbon oxides and hydrogen, the process comprising the following steps:
  • the first shift reactor comprises at least two subreactors which are operated in parallel, wherein the at least two subreactors contain different volumes of the shift catalyst.
  • the aforementioned object is solved with the invention according to claim 7 substantially with a plant for producing a treated synthesis gas, containing carbon oxides and hydrogen, the plant comprising the following units:
  • a CO shift reaction section in fluid connection with the at least one gasifier or reformer stage, comprising at least a first shift reactor, containing a shift catalyst, the CO shift reaction section being suited for converting the crude synthesis gas stream under CO shift conditions to a treated synthesis gas stream under CO shift conditions,
  • the first shift reactor comprises at least two subreactors which are operated in parallel, wherein the at least two subreactors contain different volumes of the shift catalyst.
  • the aforementioned object is solved with the invention according to claim 13 substantially with a method for starting up a plant for producing a treated synthesis gas, the plant comprising
  • a CO shift reaction section in fluid connection with the gasifier or reformer stages, comprising at least a first shift reactor, containing a shift catalyst, wherein the first shift reactor comprises at least two subreactors which are operated in parallel and which contain different volumes of the shift catalyst,
  • the crude synthesis gas stream is routed to all subreactors.
  • the aforementioned object is solved with the invention according to claim 14 substantially with a method for shutting down a plant for producing a treated synthesis gas, the plant comprising
  • a CO shift reaction section in fluid connection with the gasifier or reformer stages, comprising at least a first shift reactor, containing a shift catalyst, wherein the first shift reactor comprises at least two subreactors which are operated in parallel and which contain different volumes of the shift catalyst,
  • the crude synthesis gas stream is routed to the subreactor containing the larger volume of the shift catalyst.
  • Fluid connection between two regions of the reformer tube is understood to be any kind of connection which enables a fluid, for example the crude synthesis gas stream or the treated synthesis gas stream, to flow from the one to the other of the two regions, regardless of any interposed regions or components.
  • Adiabatic reactor operation is understood to be a reactor operation which is characterized in that except for the convective heat stream introduced with the feed stream no foreign energy is supplied to the reactor and in addition a heat exchange of the reactor with the surroundings is reduced or even completely inhibited by constructive measures, for example by mounting thermal insulations.
  • These conversion conditions are known in principle to the skilled person from the prior art, for example from the documents discussed above. Necessary adaptations of these conditions to the respective operating requirements, for example to the composition of the feed stream or to the type of catalysts used, will be made on the basis of routine experiments.
  • Catalysts which are active for CO shift, especially sour gas shift are in principle known to the skilled person and are commercially available from the trade for a variety of different applications.
  • the expert will select a suited CO shift catalyst with regard to the reaction temperature (HT /MT /LT shift) to be employed, and for special applications like sour /dirty gas CO shift.
  • any devices that are suited for this purpose are understood, especially piping or tubing systems, possibly in combination with conveyors like blowers or pumps.
  • Gasifier stages or reformer stages are to be understood as defined regions or spaces where a gasification or reforming reaction takes place.
  • stage is not be understood as implying any specific interconnection with other stages, e.g. whether the stages are connected in series or in parallel.
  • the invention is based on the fact that the CO shift reaction is strongly exothermic as outlined above.
  • varying the flow rate of the crude syngas to the CO shift reactor with regard to a given catalyst inventory i.e., varying the space velocity of the crude syngas, may lead to high temperature fluctuations.
  • the reaction equilibrium will be established, and the heat of rection liberated, in a small portion of the catalyst bed. This will lead to temperature overshooting and hot spot formation in this catalyst bed portion, and eventually to premature catalyst deactivation due to thermal ageing or sintering of the catalyst in this location.
  • the first shift reactor either designed as stand-alone reactor or being the first, most upstream reactor stage in a series of consecutive CO shift reactor stages, for example downstream of a multi-stage reformer or gasifier unit, so as to comprise at least two subreactors which are operated in parallel, wherein the at least two subreactors contain different volumes of the shift catalyst.
  • This allows for a greater flexibility when changes of flow rate of the crude syngas occur, for example during start-ups or shutdowns of the crude syngas preparation section, i.e. the successive gasifier or reformer stages.
  • the crude synthesis gas stream is produced by gasifying a carbonaceous feed stream in at least one gasifier, and the crude synthesis gas stream comprises at least 50 mol-%, preferably 60 to 70 mol-%CO and acidic gas components
  • the crude synthesis gas stream is routed to a CO sour shift reaction section, containing a sour shift catalyst.
  • the heat liberated per unit volume of catalyst is high, as is the tendency for temperature overshooting upon fluctuations of the crude syngas flow rate. This tendency is even more pronounced if the reaction is carried out in adiabatic reactors.
  • the first shift reactor consists of two subreactors which are operated in parallel, wherein the catalyst volumes in the two subreactors are present in a ratio of one third in the one subreactor to two thirds in the second subreactor.
  • Such an arrangement has the advantage of being simple from a constructional point of view, while, at the same time, being capable of dealing with a wide range of different crude syngas flow rates, as they are observed on start-up or shutdown of a syngas production plant comprising a multitude of gasifier stages and/or reforming stages which are operated in series and/or in parallel.
  • the crude synthesis gas stream is produced in three gasifier stages and/or reforming stages.
  • all crude syngas flow rates that occur during start-up or shutdown of the gasifier and/or reforming stages can be processed in the CO shift unit under optimum space velocity conditions: In case one gasifier and/or reforming stage is in operation, the complete crude syngas flow will exclusively be routed to the subreactor comprising one third of the total CO shift catalyst.
  • the complete crude syngas flow will exclusively be routed to the subreactor comprising two thirds of the total CO shift catalyst.
  • the complete crude syngas flow will be routed to both subreactors, wherein the ratio of total crude syngas flow rate to total catalyst volume is in agreement with the optimum design value for the space velocity.
  • the process according to the invention is carried out in adiabatic reactors, especially with regard to the fact that that at least the two subreactors in the first shift reactor are adiabatic reactors.
  • Adiabatic reactors are advantageous due to their simple construction; however, due to the fact that they comprise thermal insulations to reduce the heat loss from the reactor interior to the environment, they are rather sensitive with regard to temperature overshooting. Thus, they work especially well in combination with a process as outlined in claims 1 to 5.
  • the CO shift reaction section contains a sour shift catalyst.
  • the heat liberated per unit volume of catalyst is high, as is the tendency for temperature overshooting upon fluctuations of the crude syngas flow rate. This tendency is even more pronounced if the reaction is carried out in adiabatic reactors.
  • the first shift reactor consists of two subreactors which are operated in parallel, wherein the catalyst volumes in the two subreactors are present in a ratio of one third in the one subreactor to two thirds in the second subreactor.
  • the crude synthesis gas stream is produced in a multitude of gasifier stages and/or reforming stages which are operated in series and/or in parallel.
  • This embodiment has specific advantages when employed in a flow sheet comprising a first shift reactor, consisting of two subreactors which are operated in parallel, wherein the catalyst volumes in the two subreactors are present in a ratio of one third in the one subreactor to two thirds in the second subreactor.
  • this embodiment allows different options and scenarios of distributing the crude syngas flow to the two CO shift subreactors, e.g. during start-up or shutdown of the crude synthesis gas production, as will be explained in the exemplary embodiment below.
  • the plant according to the invention comprises adiabatic reactors, especially with regard to the fact that that at least the two subreactors in the first shift reactor are adiabatic reactors.
  • Adiabatic reactors are advantageous due to their simple construction; however, due to the fact that they comprise thermal insulations to reduce the heat loss from the reactor interior to the environment, they are rather sensitive with regard to temperature overshooting. Thus, they work especially well in combination with a plant as outlined in claims 7 to 12.
  • the plant comprising
  • a CO shift reaction section in fluid connection with the gasifier or reformer stages, comprising at least a first shift reactor, containing a shift catalyst, wherein the first shift reactor comprises at least two subreactors which are operated in parallel and wherein the catalyst volumes in the two subreactors are present in a ratio of one third in the one subreactor to two thirds in the second subreactor,
  • the crude synthesis gas stream is routed to the subreactor containing the smaller volume of the shift catalyst,
  • the crude synthesis gas stream is routed to all subreactors.
  • the crude synthesis gas stream is routed to the subreactor containing two thirds of the total volume of the shift catalyst.
  • This start-up and shutdown philosophy is consistent with the observation that larger crude syngas flows may preferably be sent to the subreactor containing the larger volume portion of the CO shift catalyst, while smaller crude syngas flows may be sent to the subreactor containing the smaller volume portion of the CO shift catalyst.
  • the advantage is that in start-up and shutdown scenarios in which the single reformer and/or gasifier stages in a multi-stage reformer and/or gasifier plant are started up or shut down successively, the deviation from the design value for the optimum space velocity is smaller compared to a situation where either large or small flow rates of crude syngas are routed to the same catalyst volume, for example in an arrangement where two subreactors are symmetrically filled with the same amount of catalyst. This leads to less temperature overshooting and thus to less thermal stress on the catalyst and reactor materials.
  • Fig. 1 schematically shows a CO shift process and plant according to the prior art (comparative example)
  • Fig. 2 schematically shows a CO shift process and plant according to the invention.
  • a crude syngas stream received from a multi-stage coal gasification unit comprising three gasifier stages, not shown in the figure, is routed via line 1 to heat exchanger 2, which serves for adjustment of temperature to CO shift reaction temperature.
  • the crude syngas stream is directed via line 3 to the CO shift reaction section, consisting of two symmetrical subreactors 7 a, b.
  • the flow of the crude syngas stream to subreactors 7 a, b via lines 5 a, b is controlled by valves 6 a, b.
  • Both subreactors comprise two catalyst beds, each of which comprises an identical catalyst volume relative to the other catalyst beds.
  • both subreactors are equipped with bypass lines 11 a, b and valves 12 a, b in order to bypass the crude syngas stream around the respective first catalyst bed in flow direction.
  • the treated synthesis gas stream from the CO shift reaction section depleted in carbon monoxide and enriched in hydrogen and carbon dioxide with regard to the crude synthesis gas stream is withdrawn via line 8 a, b and valve 9 a, b, collected in line 10 and routed to optional further processing stages, e. g additional CO shift stages, which are know per se and are not shown in the figure.
  • the complete CO shift reaction section may be bypassed via line 10 by shutting off valves 4 a, b and optionally valves 9 a, b and opening valve 13 which is closed in normal operation.
  • the single stages are normally started up successively.
  • the gasifier unit runs at one third or two thirds of its full production capacity, with either one or two out of three gasifier stages in operation.
  • the processing of the crude syngas streams received in these operation modes in the downstream CO shift section is difficult in terms of adjustment of the optimum space velocity.
  • the operator has the choice to either direct the crude syngas stream completely to one or two catalyst beds, both choices being suboptimal with regard to adjustment of the optimum space velocity, or, alternatively, to adjust the flow rate of the crude syngas stream to one subreactor by means of regulating valve 6 a, b.
  • the performance of the latter methods critically depends on operator experience and skillfulness and is prone to operator errors.
  • the operator has the choice to either direct the crude syngas stream to two catalyst beds, e.g. one complete subreactor, or to three catalyst beds, e.g. to the complete first subreactor plus to the downstream bed of the second subreactor, the upstream bed of the latter being bypassed.
  • both choices are suboptimal with regard to adjustment of the optimum space velocity.
  • a crude syngas stream received from a multi-stage gasifier unit comprising three parallel gasifier stages, not shown in the figure, is routed via line 1 to heat exchanger 2, which serves for adjustment of temperature to CO shift reaction temperature.
  • the crude syngas stream is directed via line 3 to the CO shift reaction section, consisting of two subreactors 7 a, b which exhibit different catalyst volumes. Both subreactors comprise only one catalyst bed each, wherein reactor 7a comprises two thirds and reactor 7b one third of the total catalyst volume with regard to the optimum space velocity.
  • the treated synthesis gas stream from the CO shift reaction section depleted in carbon monoxide and enriched in hydrogen and carbon dioxide with regard to the crude synthesis gas stream is withdrawn via line 8 a, b and valve 9 a, b, collected in line 10 and routed to optional further processing stages which are know per se and are not shown in the figure.
  • the complete CO shift reaction section may be bypassed via line 10 by shutting off valves 4 a, b and optionally valves 9 a, b and opening valve 11 which is closed in normal operation.
  • subreactor 7b On start-up of the first gasifier stage of the three parallel-stage gasifier unit in the process and plant according to the invention in Fig. 2, which corresponds to the one third production capacity scenario described above, the crude syngas stream is routed completely to subreactor 7b, comprising one third of the total catalyst volume with regard to the optimum space velocity.
  • subreactor 7b is automatically operated in the optimum space velocity regime.
  • subreactor 7a comprising two thirds of the total catalyst volume with regard to the optimum space velocity.
  • subreactor 7a is automatically operated in the optimum space velocity regime.
  • the crude syngas stream is routed completely to subreactor 7a, comprising two thirds of the total catalyst volume with regard to the optimum space velocity.
  • subreactor 7b comprising one third of the total catalyst volume with regard to the optimum space velocity.
  • the proposed process and plant are more flexible with regard to turnarounds in the upstream syngas generation plant, e.g. a multi-stage reformer and/or gasifier plant.
  • the asymmetric split of the first CO shift reactor in direction of flow of the crude syngas stream into two or more subreactors with different catalyst volumes allows for greater flexibility during start-up or shutdown of the single syngas generation stages, while operating in the or next to the optimum space velocity regime in the single catalyst beds in the CO shift subreactors.

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  • Organic Chemistry (AREA)
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  • Engineering & Computer Science (AREA)
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Abstract

L'invention concerne un procédé et une installation permettant de convertir un courant de gaz de synthèse brut contenant du monoxyde de carbone, généré dans une installation d'appareil de reformage et/ou de gazéifieur multi-étagée, par conversion du CO en un courant de gaz de synthèse traité appauvri en ce qui concerne le monoxyde de carbone, mais enrichi en ce qui concerne l'hydrogène et le dioxyde de carbone. À cet effet, le courant de gaz de synthèse brut est acheminé vers une section de réaction de conversion de CO, comprenant au moins un premier convertisseur et comprenant également, éventuellement, des convertisseurs supplémentaires en aval. Le premier convertisseur comprend au moins deux sous-réacteurs (7a, 7b) qui sont actionnés en parallèle, les deux sous-réacteurs (7a, 7b) ou plus contenant des volumes différents du catalyseur de conversion.
PCT/CN2015/073621 2014-03-05 2015-03-04 Formulation de peinture et son procédé de fabrication WO2015131818A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2015226629A AU2015226629B2 (en) 2014-03-05 2015-03-04 Process and plant for performing CO shift

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
CN2014072939 2014-03-05
CNPCT/CN2014/072939 2014-03-05
CN201510087950.7A CN105084313B (zh) 2014-03-05 2015-02-26 用于执行co变换的方法和设备
CN201510087950.7 2015-02-26
CN201520116309.7 2015-02-26
CN201520116309.7U CN204689634U (zh) 2014-03-05 2015-02-26 用于生产含有二氧化碳和氢气的处理过的合成气的设备

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WO2015131818A1 true WO2015131818A1 (fr) 2015-09-11
WO2015131818A8 WO2015131818A8 (fr) 2016-04-28
WO2015131818A9 WO2015131818A9 (fr) 2016-06-02

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WO2015131818A9 (fr) 2016-06-02

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