WO2016071192A1 - Procédé de production d'un gaz riche en méthane - Google Patents

Procédé de production d'un gaz riche en méthane Download PDF

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Publication number
WO2016071192A1
WO2016071192A1 PCT/EP2015/075089 EP2015075089W WO2016071192A1 WO 2016071192 A1 WO2016071192 A1 WO 2016071192A1 EP 2015075089 W EP2015075089 W EP 2015075089W WO 2016071192 A1 WO2016071192 A1 WO 2016071192A1
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Prior art keywords
gas
methanation
methane
reactor
reactors
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PCT/EP2015/075089
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English (en)
Inventor
Christian Wix
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Haldor Topsøe A/S
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Publication of WO2016071192A1 publication Critical patent/WO2016071192A1/fr

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    • 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
    • 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
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/106—Removal of contaminants of water

Definitions

  • Embodiments of the invention generally relate to a process and a reactor system for production of a methane rich product gas.
  • embodiments of the invention relate to a process and a reactor system for the production of substitute natural gas (SNG) from carbonaceous materials.
  • SNG substitute natural gas
  • the invention relates to a process for the production of SNG from a carbonaceous material in which the carbonaceous material is converted to a synthesis gas.
  • Coke is a solid fuel produced from coal by baking the coal in an airless furnace.
  • volatile coal constituents are driven off, purified, and an off-gas comprising i.a. one or both of carbon dioxide and carbon monoxide, as well as hydrogen and hydrocarbons is produced.
  • This coke oven off-gas is energy rich, and may often be combusted for generation of heat, e.g. for heating the coke furnace.
  • excess off-gas may be available.
  • carbon formed depends on the operating conditions and the catalyst. Typically, carbon on a Ni-catalyst is in the form of carbon whiskers. Carbon whiskers are described in the literature, see e.g. "Concepts in Syngas Manufacture” of Jens Rostrup-Nielsen and Lars J. Christiansen, "Catalytic Science Series - Vol. 10", 2011, pages 233-235. As men ⁇ tioned, the choice of catalyst and operating conditions will determine whether or not carbon will form. According to the so-called principle of equilibrated gas, carbon will form if thermodynamics predict carbon formation from one or more of reactions (4-6) after equilibration of reactions (1-3) . See for example the above referenced book, pages 247-252. Means to avoid carbon formation in this case include reducing the temperature and increasing the steam content in the feed gas to the reactor.
  • Carbon may also form from higher hydrocarbons according a reaction similar to reaction (4) as given below (for ethane) :
  • the carbon formed from higher hydrocarbons may also be in the form of whisker, graphite, or gum. It is a complex task to assess the risk of carbon formation from higher hydro- carbons. The risk of carbon formation in this case also de ⁇ pends upon the catalyst and the selected operating condi ⁇ tions. Also in this case, increasing the content of steam is one way to ensure operation out of the carbon forming operating conditions. In some cases the so-called critical steam to higher hydrocarbon ratio (S/HHC) can be used as an indicator of whether or not carbon will form on the catalyst.
  • S/HHC critical steam to higher hydrocarbon ratio
  • an ejector causes the recycling of the first part of the first gas in step
  • the ejector has a steam feed as motive gas and a recycled methane rich product gas as a suction gas.
  • a first methanation reactor of the one or more methanation reactors is meant to denote the most upstream methanation reactor of the one or more methanation reactors.
  • methanation catalyst is meant to denote any material, in any configu ⁇ ration, catalytically active in methanation.
  • cat- alyst may also cover more than one material, so that the "one or more methanation reactors with methanation catalyst” may contain more than one kind of methanation cata ⁇ lyst, e.g. catalysts with different composition and/or form.
  • One methanation reactor may comprise more than one kind of catalyst and/or different methanation reactors may comprise different kinds of catalyst.
  • step (c) ajector for driving the recycle of gas in step (c)
  • a compressor for driving the recycle of gas in step (f) viz. an outer recy ⁇ cling.
  • This is due to the effect of increased steam addi ⁇ tion via an ejector in combination with the recycling of step (f) taking place after removal of water from the gas to be recycled.
  • the recycling in step (f) takes place after water removal from the gas to be recycled, the tem ⁇ perature of the gas may be relatively low.
  • the over- all system may be cheaper and/or the compressor may be more reliable than compressors arranged for higher temperatures.
  • step (b) of reacting the feed gas takes place in one or two reactors with methana ⁇ tion catalyst in series.
  • the recycling of the first part of the first gas may take place after reaction in one or two methanation reactors, with optional further methana- tion reactors downstream the recycling.
  • the first methanation reactor is a boiling wa ⁇ ter reactor. In this case, no further methanation reactors are necessary in step b) downstream the boiling water reactor, even though the embodiment may comprise one or more optional methanation reactors of step (d) .
  • the methanation catalyst comprises nickel as a catalytically active constituent.
  • the methanation catalyst is provided on a support comprising alumina.
  • the support may further com ⁇ prise one or more constituents from the group consisting of MgAl spinel, alumina-zirconia, and calcium aluminates.
  • step (a) is preceded by a gas purifica ⁇ tion step wherein at least sulfur is removed from the feed gas.
  • the term "at least sulfur” is meant to cover components and compounds comprising sulfur, such as e.g. hydrogen sulfide 3 ⁇ 4S, COS, CS 2 , thiophene, or mercaptans .
  • the gas purification step may be arranged to remove further elements from the gas, such as for example chlorine, arse- nic, oxygen and/or olefins.
  • sulfur is removed is meant to denote that some sulfur is removed. The term is thus not meant to indicate that no sulfur is left after sulfur removal.
  • the feed gas to the first methanation re ⁇ actor is formed by combining:
  • step (f) the first part of the second gas from the recycling of step (f) .
  • step (d) comprises reacting the second part of said first gas rich in methane together with fresh synthesis gas in the second methanation reactor of the one or more methanation reactors.
  • This embodiment is called a split-flow reaction, in that the fresh synthesis gas is split between the first and second methanation reactor.
  • the fresh synthesis gas is a gas generat ⁇ ed from a carbonaceous material selected from the group of: coke, coal, petroleum coke, biomass, oil, black liquor, waste and combinations thereof. Petroleum coke is also de ⁇ noted “petcoke”.
  • the fresh synthesis gas further comprises at least 0.1 vol%, at least 0.2 vol% or at least 1 vol% C 2+ hydrocarbons.
  • C2+ hydrocarbons is meant to de- note any hydrocarbon or hydrocarbonaceous gas comprising at least two carbon atoms, also denoted “higher hydrocarbons” (abbreviated to "HHC”) . Examples of such C 2+ hydrocarbons, viz.
  • C 2 -, C3- or C4-hydrocarbons are for example ethane, propane, butane.
  • the fresh synthesis gas further comprises between 0 and 30 vol%, methane CH 4 .
  • the fresh synthesis gas could comprise between 4 and 18 vol% CH 4 , such as between 10 and 17 vol% CH 4 .
  • a stream comprising carbon oxides is add- ed to the gas downstream the first methanation reactor.
  • the carbon oxides are e.g. added upstream the second methana ⁇ tion reactor or the carbon oxides are mixed with the second part of the second gas, e.g. upstream one or more final methanation reactor (s) .
  • This is advantageous in case of ad- dition of a relatively large amount of carbon dioxide.
  • the stream comprising carbon oxides is a sub- stoichiometric stream with a ratio (H2-CO2) / (CO-CO2) ⁇ 3.
  • step (g) is preceded by the step of re- acting the second part of the second gas in the presence of a methanation catalyst in one or more final methanation reactors in order to provide the methane rich product gas.
  • step (g) further comprises the step of sepa ⁇ rating water from the third gas, thereby forming the me- thane rich product gas.
  • a stream comprising carbon oxides could be added to the second part of the sec- ond gas upstream the final methanation reactor, in order to control the quality of the product gas.
  • Embodiments of the invention further comprise cooling the gas output from one or more of the methanation reactors.
  • the feed gas entering said first methana ⁇ tion reactor has a temperature of between 280°C and 380°C, wherein the first gas exiting from the first methanation reactor has a temperature in the range from 500°C to 750°C.
  • the gas exiting subsequent methanation reactors will have a temperature equal to or lower than the temperature of the first gas exiting from the first methanation reactor.
  • at least one methanation reactor of the one or more methanation reactors used in step (b) further comprises a layer of shift catalyst directly upstream the methanation catalyst.
  • the shift cat- alyst thus forms a layer directly on top of the methanation catalyst.
  • the shift catalyst may be a conventional shift catalyst.
  • Such conventional shift catalysts typically com ⁇ prise at least two of the metals Cu, Zn and Cr, optionally in the form of oxides and optionally on a carrier.
  • the weakly exothermic shift process (reaction (3) ) will heat the feed gas a little and partly convert carbon monox ⁇ ide.
  • reaction (3) When the gas is hereafter passed over the methanation catalyst, any tendency to nickel carbonyl formation has been substantially removed because of the weak temperature increase and lower CO-contents.
  • the inlet temperature to the first methanation reactor may be decreased compared to a situation without shift catalyst.
  • the inlet temperature to the first methanation reactor may e.g. be 250°C or even lower, whilst the first gas exiting from the first methanation reactor has a temperature in the range 500-750°C.
  • the water withdrawal in step (e) is car ⁇ ried out by condensation at a temperature of at least about 80°C.
  • Another aspect of the invention relates to a reactor system for production of a methane rich product gas from a feed gas, where the reactor system comprises:
  • a feed line arranged for providing the feed gas into a first methanation reactor of the one or more methanation reactors, where the feed gas comprises carbon oxide such as carbon monoxide and/or carbon dioxide, and hydrogen, and wherein the one or more methanation reactors is/are ar ⁇ ranged to react the feed gas in the presence of the feed gas
  • An ejector is arranged to cause the recycling in the first recycle line and a compressor is arranged to cause the re ⁇ cycling of the second recycle line.
  • the ejector is config ⁇ ured for having a steam feed as motive gas and a recycled methane rich product gas as a suction gas.
  • a separator is arranged to withdraw the methane rich product gas from a second part of the second gas, subsequent to a further methanation reactor.
  • Figure 1 illustrates a methanation process with an ejector according to prior art.
  • Figure 2 illustrates a methanation process with a compres ⁇ sor according to prior art.
  • Figure 3 illustrates a methanation process with an ejector and a compressor according to the invention.
  • Figure 4 illustrates a methanation process with an ejector and a compressor according to the invention, the process comprising a split-flow around the first methanation reactor .
  • the invention provides numerous advantages over the prior art.
  • embodiments of the invention may achieve advantages over other possible solutions and/or over the prior art, whether or not a particular advantage is achieved by a given embod ⁇ iment is not limiting of the invention.
  • the following aspects, features, embodiments and advantages are merely illustrative and are not considered elements or limitations of the appended claims except where explicitly recited in a claim (s).
  • reference to "the invention” shall not be construed as a generalization of any inventive subject matter disclosed herein and shall not be considered to be an element or limitation of the appended claims except where explicitly recited in a claim (s) .
  • Figure 1 illustrates a methanation process 100 with an ejector according to prior art.
  • the methanation process shown in figure 1 relates to a methanation process 100 with four adiabatic methanation reactors 124, 134, 140, 162 and an ejector 118.
  • a fresh synthesis gas 102 is heated 104 and led to a sulfur guard 112 in addition with steam 108, providing a desulfu- rized synthesis gas 114.
  • the desulfurized synthesis gas 114 is mixed with a mixture of steam and methane rich recycled gas 120 in order to obtain a first methanation reactor feed gas 122 to be inlet to a first methanation reactor 124.
  • the first methanation reactor feed gas 122 is directed to a first methanation reactor 124, providing a first methane rich gas 126, which is cooled in a heat exchanger 128.
  • a part of the first methane rich gas 126 is recy ⁇ cled around the first methanation reactor 124, driven by an ejector 118 with steam 110 as a motive gas.
  • the part 132 of the first methane rich gas which is not re ⁇ cycled, is allowed to react further in a second methanation reactor 134 and in a third methanation reactor 140 with intermediate cooling 138 of a second stage methane rich gas 136 from the second methanation reactor 134 and intermedi- ate cooling 144 of a third stage methane rich gas 142 from the third methanation reactor 140.
  • water 148 Prior to a fourth and final methanation reactor 162, water 148 is condensed, after cooling 144, in a separator 146 in order to shift the reaction equilibrium of a final methana ⁇ tion feed gas 150.
  • the final methanation feed gas 150 is subsequently heated in 160 and led to a final methanation reactor 162 resulting in a final stage methane rich gas 164.
  • the final stage methane rich gas 164 led from the fi ⁇ nal methanation reactor 162 is cooled 166 and led to a sep ⁇ arator 168 in order to separate water 170 from the final stage methane rich gas 164.
  • the separator 168 is arranged to separate water 170 from the final stage methane rich gas and thereby produce a synthetic natural gas 172.
  • Figure 2 illustrates a methanation process 200 with a com- pressor according to prior art.
  • the methanation process shown in figure 2 relates to a methanation process 200 with four adiabatic methanation reactors 224, 234, 240, 262 and a compressor 254.
  • a feedstock gas 202 e.g. a synthesis gas
  • a sulfur guard 212 in addition with steam 208, providing a desulfurized synthesis gas 214.
  • the desulfu ⁇ rized synthesis gas 214 is mixed with a mixture of steam 210 and methane rich gas recycled 256 in order to obtain a first methanation feed gas 222 to be inlet to a first methanation reactor 224.
  • the first methanation feed gas 222 is directed to a first methanation reactor 224, providing a first stage methane rich gas 226, which is cooled in a heat exchanger 228. Sub ⁇ sequently, the cooled, first methane rich gas 226 is driven to a second methanation reactor 234, providing a second stage methane rich gas 236, and thereafter to a third methanation reactor 240, with intermediate cooling the second stage methane rich gas 236.
  • water 248 Prior to a fourth and final methanation reactor 262, water 248 is condensed, after cooling 244, in a separator 246 in order to shift the reaction equilibrium of a final methana ⁇ tion feed gas 250.
  • methanation feed gas 250 is recycled as recycled methane rich gas 252 to the first methanation 224, via a cold compressor 254, and heated by means of a heat exchanger 255, providing the recycle stream 256.
  • the part 258 of the final methanation feed gas not recycled is heated 260 and allowed to react further in a fourth and final methanation reactor 262 resulting in a final stage methane rich gas 264.
  • the final stage methane rich gas 264 is cooled 266 and led to a separator 268 in order to separate water 270 from the final stage methane rich gas 264 and thereby produce a synthetic natural gas 272.
  • Figure 3 illustrates a methanation process 300 with an ejector and a compressor according to the invention.
  • the methanation process 300 shown in Figure 3 is a methana ⁇ tion process with four adiabatic methanation reactors 324, 334, 340, 362, an ejector 318 and a compressor 354.
  • a feedstock gas 302 e.g. a synthesis gas comprising carbon monoxide and/or carbon dioxide, and hydrogen
  • a feedstock gas 302 is heated 304 and directed to a sulfur guard 312 in addition with steam 308 from a source 306 or steam, providing a desulfurized feedstock gas 314.
  • a sulfur guard 312 in addition with steam 308 from a source 306 or steam, providing a desulfurized feedstock gas 314.
  • the desulfurized synthesis gas 314 is mixed with a mixture 320 of steam, a first recycle stream 330 of methane rich gas and a second recycle stream 356 of methane rich gas in order to obtain a feed gas 322 for the first methanation reactor.
  • the first recycle is driven by an ejector 318 with steam 310 from the steam source 306 as a motive gas.
  • the feed gas 322 is directed to a first methanation reactor 324, providing a first gas 326 rich in methane; this first methane rich gas 326 is subsequently cooled in a heat ex ⁇ changer 328.
  • the first part 330 of the first methane rich gas 326 is recycled back to the first methanation re ⁇ actor 324.
  • This first part 330 of the first gas is driven together with steam 310 by the ejector 318, providing the first recycle stream 320.
  • the part 332 of the first methane rich gas 326 which is not recycled is allowed to react fur ⁇ ther in a second methanation reactor 334 providing a second stage methane rich gas 336 and is cooled 338.
  • the cooled second stage methane rich gas 336 is allowed to react further in a third methanation reactor 340 providing a third stage methane rich gas 342 which is cooled 344.
  • the cooled third stage methane rich gas is led to a separator 346 in order to condense water 348, re ⁇ sulting in a second gas 350 rich in methane.
  • the separation of water from the cooled third stage methane rich gas 342 ensures that the equilibrium is shifted in further methana ⁇ tion reactor.
  • a first part 352 of the second gas 350 is recycled to the feed gas to the first methanation reactor 324.
  • the recy- cling of the first part 352 of the second gas 350 is driven or caused by a cold compressor 354.
  • the first part 352 of the second gas 350 is heated by a heat exchanger 355, providing a second recycle stream 356 of methane rich gas.
  • the second recycle stream of methane rich gas 356 is mixed with the desulfurized synthesis gas 314 and with a first recycle of methane rich gas 320 at or upstream of an inlet to the first methanation reactor 324 with methanation catalyst.
  • the fresh synthesis gas 302 may be provided directly to the first methanation reac ⁇ tor 324 together with steam added by the ejector 318, the first part 330 of the first methane rich gas 326 recycled and the second recycle stream of methane rich gas 356.
  • a second part 358 of the second gas i.e. the part of me ⁇ thane rich gas 350 not recycled, is heated 360 and allowed to react further in a fourth and final methanation reactor 362.
  • a final stage methane rich gas 364 exiting the fourth reactor 362 is cooled 366 and led to a separator 368.
  • water 370 is separated from the cooled final stage methane rich gas 364 and the remaining gas 372 is the methane rich product gas 372 in the form of a syn ⁇ thetic natural gas 372.
  • Figure 4 illustrates a methanation process 400 with an ejector 418 and a compressor 454 according to the invention, the process comprising a split-flow around the first methanation reactor 424.
  • the methanation process 400 shown in figure 4 is a methana ⁇ tion process with five adiabatic methanation reactors 424, 434, 440, 444, 462, an ejector 418 and a compressor 454.
  • a feedstock gas 402 e.g. a synthesis gas comprising carbon oxides and hydrogen, is heated in a heat exchanger 404 and directed to a sulfur guard 412 in addition with steam 408, providing a desulfurized synthesis gas 414.
  • the desulfu ⁇ rized synthesis gas 414 is heated in a heat exchanger 413.
  • the desulfurized synthesis gas 414 is split into a first part 415 and a second part 421.
  • the first part 415 of the desulfurized synthesis gas is mixed with a second recycle stream 456 of methane rich gas in order to provide stream 416.
  • the mixed stream 416 is mixed with a mixture 420 of steam, a first recycle stream 423 of methane rich gas in order to obtain a feed gas 422 for the first methanation reactor 424.
  • the first recycle is driven by an ejector 418 with steam 410 from a steam source 406 as a motive gas.
  • the second recycle is driven by a cold compressor 454.
  • the feed gas 422 is directed to a first methanation reactor 424, providing a first methane rich gas 426.
  • the first me ⁇ thane rich gas 426 is subsequently cooled in a heat ex ⁇ changer 425.
  • the first part 423 of the first methane rich gas 426 is recycled back to the first methanation re ⁇ actor 424.
  • This first part 423 of the first gas is driven together with steam 410 by the ejector 418, providing the first recycle stream 420.
  • the part 427 of the first methane rich gas 426, which is not recycled, is mixed with a second part 421 of the desulfurized synthesis gas 414.
  • the mixture 428 of the non-recycled part 427 of the first methane rich gas and the second part 421 of the desulfurized synthesis gas is allowed to react further in a second methanation re- actor 434, a third methanation reactor 440 and a fourth methanation reactor 444 with intermediate cooling of the second stage 437 and third stage 443 methane rich gas, by means of the heat exchangers 436, 442.
  • the fourth stage me ⁇ thane rich gas 446 exiting from the fourth methanation re- actor 444 is cooled by the heat exchanger 445.
  • the cooled fourth stage methane rich gas 446 is led to a separator 447 in order to condense water 448, resulting in a second gas 450 rich in methane.
  • the separa- tion of water from the cooled fourth stage methane rich gas 446 ensures that the equilibrium is shifted in a further methanation reactor.
  • a first part 452 of the second gas 450 is recycled to the feed gas to the first methanation reactor 424.
  • the recy ⁇ cling of the first part 452 of the second gas 450 is driven or caused by a cold compressor 454.
  • the first part 452 of the second gas 450 is heated by a heat exchanger 455, providing a second recycle stream 456 of methane rich gas.
  • the second recycle stream of methane rich gas 456 is mixed with the first part 415 of the desulfurized synthesis gas 414 and with a first recycle of methane rich gas 423 at or upstream of an inlet to the first methanation reactor 324 with methanation catalyst.
  • a first part of the fresh synthesis gas 402 may be provided directly to the first methanation reactor 424 together with steam added by the ejector 418, the first part 430 of the first methane rich gas 423 recycled and the second recycle stream of me ⁇ thane rich gas 456, whilst a second part of the fresh syn ⁇ thesis gas 402 may be provided to the second methanation reactor 434.
  • a second part 458 of the second gas i.e.
  • water 470 is separated from the cooled final stage me ⁇ thane rich gas 464 and the remaining gas 472 is the methane rich product gas 472 in the form of a synthetic natural gas 472.
  • PRODUCT QUALITY Tables 2 and 3 below show the low heating value and the composition of the final methane rich product gas from the processes shown in figure 1-4, with the fresh synthesis gas as indicated in Table 1.
  • Table 3 Tables 2 and 3 above show that the process 100 shown in figure 1, having an ejector for recycling around the first methanation reactor 124, results in a final product gas comprising 95.5 mole% of CH 4 and having a Lower Heating Value (LHV) of 8,226 kcal/Nm 3 .
  • LHV Lower Heating Value
  • the tables show that the process 200 of figure 2 comprising a cold compressor for recycling methane rich gas from a third methanation reactor 240 to the first methana- tion reactor 224, results in a final product gas comprising 97.4 mole% of CH 4 and having a LHV of 8,359 kcal/Nm 3 .
  • Table 4 indicates the shaft power necessary for driving the compressor in the examples shown in figures 1-4 as well as the methane content of the product gas. It is clear that the embodiments of the invention shown in figures 3 and 4 provides a product gas with a comparable methane content to the embodiment shown in figure 2, whilst the power consump ⁇ tion for driving the process is reduced considerably. Com ⁇ pared to the embodiment where only an ejector is used, fig ⁇ ure 1, the power consumed for driving the processes of the invention, shown in figures 3 and 4, is higher; however, the methane content in the product gas is also higher.
  • the carbon limit for a methanation reactor depends upon i.a. the catalyst used and the compo ⁇ sition of the fresh synthesis gas.
  • the appli ⁇ cant has carried out calculations on the carbon limit for the catalyst in the embodiment shown in figure 3 for the two different compositions of fresh synthesis gas indicated in table 1 above.

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Abstract

L'invention concerne un procédé de production d'un produit gazeux riche en méthane comprenant les étapes consistant : (a) à utiliser un gaz d'alimentation comprenant de l'oxyde de carbone tel que le monoxyde de carbone et/ou le dioxyde de carbone, et de l'hydrogène, (b) à faire réagir ledit gaz d'alimentation en présence d'un catalyseur dans un ou plusieurs réacteurs de méthanation avec un catalyseur de méthanation, pour former un premier gaz riche en méthane, (c) à recycler une première partie dudit premier gaz au niveau dudit gaz d'alimentation introduit dans un ou plusieurs réacteurs de méthanation, (d) éventuellement, à faire réagir une seconde partie dudit premier gaz riche en méthane dans un ou plusieurs autres réacteurs de méthanation parmi le ou les réacteurs de méthanation, (e) à extraire l'eau hors de ladite seconde partie dudit premier gaz ou hors du gaz résultant de la réaction de ladite seconde partie dudit premier gaz riche en méthane dans le ou les autres réacteurs de méthanation, ce qui permet d'obtenir un second gaz, (f) à recycler une première partie dudit second gaz au niveau dudit gaz d'alimentation introduit dans un premier réacteur de méthanation parmi le ou les réacteurs de méthanation, (g) à obtenir ledit produit gazeux riche en méthane à partir d'une seconde partie dudit second gaz, un éjecteur entraînant ledit recyclage de ladite première partie dudit premier gaz à l'étape (c) et un compresseur entraînant ledit recyclage de ladite première partie dudit second gaz à l'étape (f), et ledit éjecteur utilisant une charge de vapeur en tant que gaz moteur et un produit gazeux riche en méthane recyclé en tant que gaz d'aspiration.
PCT/EP2015/075089 2014-11-04 2015-10-29 Procédé de production d'un gaz riche en méthane WO2016071192A1 (fr)

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WO2018234695A1 (fr) 2017-06-20 2018-12-27 Michel Bonhomme Procédé de et dispositif de production de biométhane en réacteur compartimente en voie visqueuse

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