• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A method for the production of methane from biomass A multistage method and apparatus for the production of methane from biomass is provided, in which the biomass is hydropyrolized in a reactor vat containing molecular hydrogen and a deoxygenation catalyst. which is hydrogenated using a hydroconversion catalyst. The output of the hydroconversion step is provided to a water-gas-shift process providing a mixture of h2o and product gases, including co2, h2 and methane. The mixture components are separated, which results in a product stream comprising substantially only methane.
    公开号:BR112012032043B1
    申请号:R112012032043
    申请日:2011-06-09
    公开日:2019-10-22
    发明作者:Leppin Dennis；S Meyer Howard；G Felix Larry；B Linck Martin；L Marker Terry
    申请人:Gas Technology Inst；
    IPC主号:
    专利说明:

    [001] This invention relates to an integrated process to thermochemically transform biomass directly into methane. As used here, the term biomass refers to biological materials derived from living or dead organisms and includes lignocellulosic materials, such as wood, aquatic materials, such as algae, aquatic plants, algae, and animal waste and by-products, such as offal, fats and sewage sludge. In one aspect, the present invention relates to a multistage hydropyrolysis process for the production of methane from biomass.
    Description of Related Art [002] Conventional biomass pyrolysis, typically rapid pyrolysis, does not use or require H 2 or catalysts and produces a dense, acidic, reactive liquid product that contains water, oils and coal formed during the process. High methane yields can be achieved through conventional rapid pyrolysis, however, the highest coal yields are typically achieved through rapid pyrolysis in the absence of hydrogen, which decreases methane yield compared to the method of the present invention . Methane can also be produced from biomass by conventional pyrolysis and anaerobic digestion processes. In addition, gasification followed by methanation can be used to produce methane from biomass.
    SUMMARY OF THE INVENTION [003] It is an object of the present invention to provide a method and apparatus for the production of methane that provides superior methane yields when compared to conventional anaerobic digestion, gasification or rapid pyrolysis.
    [004] It is an object of the present invention to provide a method and apparatus for the production of methane that occupies a smaller physical coverage area than a comparable anaerobic digester or rapid pyrolyzer. The conversion of biomass into an anaerobic digester takes a long time (20-30 days of residence time in the digester), which requires a very large anaerobic digester.
    [005] It is yet another objective of the present invention to provide a
    Petition 870180126858, of September 5, 2018, p. 27/71
    2/11 method and apparatus for the production of methane, which is less expensive than conventional steam and gasification pressurized by oxygen followed by methanation. Gasification is capital intensive, because it is carried out at high temperatures, it requires an air separation plant to produce the necessary oxygen, whose air separation plant is capital intensive.
    [006] It is yet another objective of the present invention to provide a method and apparatus for the production of methane from biomass.
    [007] These and other objectives of the present invention are addressed by a multistage method and apparatus for the production of methane from biomass comprising the steps of hydropyrolize biomass in a hydropyrolysis reactor vat containing molecular hydrogen and a deoxygenation catalyst , at a hydropyrolysis temperature greater than about 1000 ° F and a hydropyrolysis pressure in a range of about 100 psig and about 600 psig, produce a hydropyrolysis product comprising coal and a gas containing a large proportion of methane, very small amounts of higher hydrocarbons including unsaturated hydrocarbons, but no tar-like material, other than H2, CO, CO2, and H2O (steam), and also H2S insofar as there is sulfur in the raw material, separate the coal from the product hydropyrolysis, resulting in a reduced coal hydropyrolysis product, and hydroconverter the reduced coal hydropyrolysis product in a hydroconversion reactor vat, using a hydroconversion catalyst at a hydroconversion temperature greater than about 850 ° F and a hydroconversion pressure in a range of about 100 psig to about 600 psig. Thus, a stream of hydropyrolysis product containing substantial amounts of methane is produced. The hydroconversion product is cooled and introduced into a water-gas displacement reactor to convert most of the CO by reaction with 0 water vapor, producing a water-gas-shift product that comprises steam and a gas mixture comprising CO2, H2 and methane, but with reduced levels of CO. The CO2, H2 and methane are then separated, producing a stream of CO2, a stream of H2, and a stream of methane. Ο H2 is recovered, for example, through a PSA unit, and recycled back to the hydropyrolysis unit. The methane stream is then compacted and divided between a gaseous product which is methaned as needed
    Petition 870180126858, of September 5, 2018, p. 28/71
    3/11 to remove any residual CO and H2, or both, by conversion to methane, to produce an acceptable methane product for a pipeline that carries natural gas for customers who purchase the final gas from it, and the rest of methane is sent to the steam reformer, where, after adding appropriate levels of steam to prevent the formation of carbon in the catalyst tubes suspended in the reformer oven box, a portion (typically 10-15%) is used as fuel for the reformer's furnace box, and the rest is steam reformed to produce hydrogen for the hydropyrolysis unit. A portion of the hydrogen stream from the reformer proportional to the level of CO, CO2, H2 and which enters the methanation unit before the addition of hydrogen is introduced into the aforementioned methanation tank. There, the hydrogen reacts with any remaining amounts of carbon oxides (CO2 and CO) in the methane product stream, forming additional methane and thereby minimizing the carbon oxides in the methane product stream. The multiple reactors and final stage reactors to achieve the desired degree of conversion and to accommodate the heat released by the methanation reactions are supplied as needed, as known to those skilled in the art.
    BRIEF DESCRIPTION OF THE DRAWINGS [008] These and other objectives and characteristics of the present invention will be better understood from the detailed description that follows taken together with the drawings in which:
    Fig. 1 is a schematic flow diagram of a process for the production of methane from biomass, according to an embodiment of the present invention; and
    Fig. 2 is a schematic flow diagram of a process for the production of methane, according to another embodiment of the present invention.
    DETAILED DESCRIPTION OF THE PRESENTLY PREFERRED EMBODIMENTS [009] The process of the present invention, shown in Fig. 1, is a compact, integrated multistage process for thermochemically transforming biomass into methane. The first stage or reaction stage of the present process employs a pressurized hydropyrolysis reactor vat 10, catalytically
    Petition 870180126858, of September 5, 2018, p. 29/71
    4/11 reinforced, to create a partially deoxygenated hydropyrolysis product with a low amount of coal, from which the coal is removed. Although any reactor well suitable for hydropyrolysis can be employed, the preferred reactor well is a fluidized bed reactor. The hydropyrolysis stage employs rapid heating in which the average internal temperature of the particle rises at a rate of about 10,000 O / second. The residence time of the pyrolysis vapors in the reactor tank is less than about 1 minute. In contrast to this, the residence time of the coal is relatively long, because it is not removed through the bottom of the reactor bowl and thus must be reduced in particle size until the aerodynamic diameter of these particles is sufficiently reduced to allow them to be eluted and transported with the vapors that come out near the upper part of the reactor bowl. The second reaction stage (after coal removal) employs a hydroconversion reactor bowl 11, in which the hydroconversion step is performed at substantially the same pressure as that of the first reaction stage, as needed to convert any olefins to methane. The product from the second reaction stage is then sent to a water-gas displacement reactor 12, in which the product is converted to a displacement product, comprising a mixture of CO2, H2O, H2, and methane and the concentration of CO is decreased. The displacement product is cooled and separated in water, which is used, after the water treatment, for steam reforming a portion of the methane product in the steam reformer 14, 0 which in itself is a component of a unit reformer-packaged PSA 15, and gas fractions using high pressure separator 13. The mixture of CO2, H2, and methane is supplied to an H216 recovery unit in which ο H2 is separated from the mixture and combined with H2 from the packaged reformer-PSA unit. Ο H2 is then compressed in the steam powered compressor 17 and recycled back to the hydropyrolysis reactor bowl 10 for use in the hydropyrolysis process therein. The remaining mixture with a small amount of CO and CO2 is compressed. The methane-rich stream leaving the H2 16 separation unit may still contain small amounts of CO as an impurity in excess of that allowed for methane to be acceptable in a natural gas piping system. A portion of the remaining methane is supplied to the methanator 19 in which any residual CO and a
    Petition 870180126858, of September 5, 2018, p. 30/71
    5/11 portion of the H2 from the packaged reformer-PSA unit is reacted to produce additional methane. Depending on the level of H2S, a sulfur trace removal system or sulfur protection bed may be required to protect the methanation catalyst 0 which is poisoned by sulfur. The stream leaving the methanator 19 will be a stream of high purity methane, containing only traces of CO, CO2, H2, and water vapor. This stream will be dehydrated and compressed to an adequate pressure for the admission to the transport of natural gas or other drainage pipes. The remaining portion of methane from the H2 recovery separation unit 16 is sent to the steam reformer 14, together with water as steam for the conversion of methane to H2 and CO2. A portion of the methane gas is burned in a furnace or other combustor 20 to heat the remaining portion of the methane gas to the operating temperature of the steam reformer, which is about 1700 ° F. Alternatively, this furnace can be powered using the coal eliminated from the hydropyrolysis product stream downstream of the hydropyrolysis reactor 10. Steam reformers require a 3/1 vapor to hydrocarbon ratio in their feed to prevent carbon formation and to push the reaction equilibrium to displace 0 CO in H2, but this is more than the amount needed for the reforming reaction. The excess water is recovered, treated as necessary for the feed water boiler needs, and recycled to the steam reformer. CO2 is removed from the process by pressure swing adsorption (PSA) and any H2 not sent to methanator 19 is recirculated back to the first reaction stage (hydropyrolysis, which occurs in hydropyrolysis reactor 10) in the process.
    [010] A key aspect of the present invention is that the thermal energy required in the process is supplied by the heat of the deoxygenation reaction reaction, which is exothermic, occurring in both the first and the second phases. Another important aspect of the present invention is that the biomass feed does not need to be strictly dry and, in fact, the addition of water either in the feed or as a separate feed is advantageous for the process because it improves the formation of H2 in-situ through of a water-gas displacement reaction.
    [011] The biomass feed used in the process of the present invention may be in the form of loose biomass particles having a majority of
    Petition 870180126858, of September 5, 2018, p. 31/71
    6/11 particles preferably less than about 3 mm in size or in the form of a biomass / liquid paste. However, it will be appreciated by those skilled in the art that the biomass feed can be pre-treated or otherwise processed in such a way that larger particle sizes can be accommodated. Suitable means for introducing the biomass feed into the hydropyrolysis reactor vat include, but are not limited to, an auger, fast-moving current (greater than about 5m / s) of carrier gas, such as inert gases or CO2 and H2, and constant displacement pumps, impellers, or turbine pumps.
    [012] Hydropyrolysis is carried out in the reaction vessel at a temperature greater than about 1000 ° F, preferably in the range of about 1000 ° F to about 1200 ° F, and at a pressure in the range of about 100 psig and about 600 psig. Heating rate of biomass is preferably greater than about 10,000 / second. The hourly space velocity by weight (WHSV) in gm of biomass / gm of catalyst / hr for this step is in the range of about 0.2 to about 10.
    [013] As previously indicated, in the hydropyrolysis step of the present invention, the feed of the solid biomass is rapidly heated, preferably in a hot fluidized bed, resulting in the conversion of biomass to non-coal products that are comparable and possibly better than the yields obtained with conventional rapid pyrolysis. However, hydropyrolysis vapors during hydropyrolysis are in the presence of a catalyst and a high partial pressure of H2 within the fluidized bed, which provides the hydrogenation activity and also some deoxygenation activity. Hydrogenation activity is very desirable to prevent reactive olefins from polymerizing, thereby reducing the formation of unstable free radicals. Likewise, deoxygenation activity is important so that the heat of reaction from hydropyrolysis is provided by means of the exothermic deoxygenation reaction, thus obviating the need for external heating of the hydropyrolysis reactor. The advantage of hydropyrolysis over existing pyrolytic processes is that hydropyrolysis prevents retrograde reactions from pyrolysis, which is normally performed in an inert atmosphere, certainly in the absence of H2 and,
    Petition 870180126858, of September 5, 2018, p. 32/71
    7/11 normally, in the absence of a catalyst, thus promoting the undesirable formation of polynuclear aromatic compounds, free radicals and olefinic compounds that are not present in the original biomass. If hydropyrolysis is carried out at low temperatures, longer chain molecules will tend to be produced. If hydropyrolysis is carried out at higher temperatures, these molecules will tend to be broken down, producing molecules with shorter carbon chains and increasing the proportion of methane produced during this step.
    [014] The first stage of the hydropyrolysis step of the present invention operates at a warmer temperature than is typical of a conventional hydroconversion process, and as a result of which, the biomass is rapidly devolatilized. Thus, the step requires that an active catalyst stabilizes the hydropyrolysis vapors, but not so actively causes the catalyst to quickly become coke. The catalyst particle sizes are preferably greater than about 100 micrometers. Although any deoxygenation catalyst of suitable size for use in the temperature range of this process can be used in the hydropyrolysis step, the catalysts according to preferred embodiments of the present invention are as follows:
    [015] Glass-ceramic catalyst - Glass-ceramic catalysts are extremely strong and resistant to friction and can be prepared as thermally impregnated (ie supported), or as mass catalysts. When used as a sulphitized NiMo, Ni / NiO, CoMo, or Co- catalyst, active sulfur catalyst, the resulting catalyst is an abrasion resistant version of a NiMo, Ni / NiO catalyst , or Co-conventional, readily available, but smooth. Sulfited NiMo, Ni / NiO, or glass-ceramic Co-based catalysts are particularly suitable for use in a hot fluidized bed because these materials can provide the catalytic effect of a supported conventional catalyst, but in a friction-resistant form much more robust. In addition, due to the resistance to friction of the catalyst, the biomass and coal are simultaneously ground into smaller particles, since hydropyrolysis reactions proceed inside the reaction vessel. In this way, coal
    Petition 870180126858, of September 5, 2018, p. 33/71
    8/11 which is finally recovered is substantially free of catalyst contaminants from the catalyst, due to the frictional resistance and extremely high catalyst strength. The catalyst friction rate will typically be less than about 2% by weight per hour, preferably less than 1% by weight per hour, as determined in a standard high-speed jet-cup friction test. The catalyst will be added periodically to compensate for the catalyst losses.
    Í0161 Nickel phosphide catalyst - Ni phosphide catalysts do not require sulfur to operate, nor are they sulfur-poisoned and therefore will be as active in a sulfur-free environment as in an environment containing H2S, COS and other compounds containing sulfur. Therefore, this catalyst will be just as active for biomass, which has little or no sulfur present as it is for biomass containing sulfur (for example, corn straw). This catalyst can be impregnated on carbon as a separate catalyst or impregnated directly into the raw material of the biomass itself.
    [0171 Bauxite - Bauxite is an extremely inexpensive material and, therefore, can be used as a disposable catalyst. Bauxite can also be impregnated with other materials, such as Ni, Mo, or be sulphitized as well.
    [018] Small spray-dried silica-alumina catalyst impregnated with NiMo or C0M0 and sulphitized to form a hydroconversion catalyst - commercially available NiMo or C0M0 catalysts are usually supplied in the form of 1/8 large size tablets -1 / 16 inch for use in fixed beds. In the present case, 0 NiMo is impregnated in the spray dried silica alumina catalyst and used in a fluidized bed. This catalyst exhibits a higher strength than a conventional NiMo or C0M0 catalyst and would be the right size for use in a fluid bed.
    [019] An alumina support can also serve as a hydropyrolysis catalyst. This alumina support can be alumina range of a suitable size and surface area, or have phosphorus arranged on top of it as is typical for a hydrotreating catalyst support.
    [020] Among the steps of hydropyrolysis and hydroconversion, the coal is removed from the hydropyrolysis product, usually through separation by
    Petition 870180126858, of September 5, 2018, p. 34/71
    9/11 inertia, such as cyclones, or barrier filtration, such as bayonet filters. In conventional rapid pyrolysis, efficient coal removal is hampered because as the coal is captured on the surface of a filter, it reacts with the highly oxygenated hydrocarbon vapors resulting from pyrolysis to create tar-type hydrocarbons that coat and they bind to the coal captured in a dense powder cake that can permanently cover up the hot process filters. In contrast to the rapid pyrolysis carried out in an inert atmosphere, in hydropyrolysis, the hydrogenated vapors that are produced are non-reactive, the low molecular weight hydrocarbons that remain in the gaseous state at all times and pass through a barrier filter without reaction or deposition. Thus, in hydroconversion and integrated hydropyrolysis, the carbon can be removed according to the process of the present invention by filtration from the vapor stream. Retropulsation can be used to remove carbon from the filters, provided that the hydrogen used in the process of the present invention is sufficiently hydrogenated and, therefore, reduces the reactivity of the hydropyrolysis vapors leaving the hydropyrolysis reactor. Electrostatic precipitation, inertial separation, magnetic separation, or a combination of these technologies can also be used to remove coal and ash particles from the hot vapor stream.
    [021] Because of their resistance to friction, glass ceramic heaters are more easily separated from coal by energy inertial separation technologies that typically employ energy impaction, interception and / or diffusion processes sometimes combined with electrostatic precipitation to separate , concentrate and collect coal in a secondary stream for recovery. An additional virtue of these materials is that, since they are susceptible to magnetic separation (in a reduced state, being attracted by an electrically induced or permanent magnetic field), magnetic techniques as well as combinations of magnetic, inertial and electrostatic media can used to separate coal from these catalysts, which are not possible with softer materials.
    [022] In accordance with an embodiment of this invention, hot gas filtration can be used to remove coal. In the case of hydropyrolysis, because the hydrogen has stabilized free radicals and saturated olefins, the powder cake
    Petition 870180126858, of September 5, 2018, p. 35/71
    10/11 captured in the filters was found to be more easily cleaned than the carbon removed in the hot filtration of aerosols produced in conventional rapid pyrolysis.
    [023] According to another embodiment of this invention, filtration with hot gases is coupled with the injection of suitable adsorbent or mixture of adsorbents for the removal of certain impurities. In this embodiment, the adsorbents form a filter cake on the filter element prior to the admission of particulate-loaded gas, or on a second, hot gas filter, where the dust / fine particles of hydropyrolysis or hydrogasification have already been removed. . Cooling can be provided in order to operate the filter in optimum conditions that remove a particular contaminant or contaminants with the selected adsorbent or adsorbent. Means are provided to counter-pulse the accumulated adsorbent and / or fines / adsorbent cake accumulated on the filter, thus removing impurities that react under the chosen operating conditions with the adsorbents used.
    [024] After removing the coal, the product from the first reaction stage of the hydropyrolysis stage is introduced into a second stage 11 hydroconversion reactor vat, in which it is subjected to a second hydroconversion stage of the reaction to convert any olefins to methane. This step is preferably carried out at a lower temperature (850,950 ° F) than that of the first stage of hydropyrolysis of the reaction stage and substantially the same pressure (100 - 600 psig) as that of the first stage of hydropyrolysis of the reaction stage. The hourly space velocity in weight (WHSV) for this step is in the range of about 0.2 to about 3. If the hydroconversion catalyst can be protected from poisons, the life of the catalyst can be expected to be increased. Thus, the catalyst used in this step must be protected from Na, K, Ca, P, and other metals present in the biomass, which can poison the catalyst. This catalyst must also be protected from olefins and free radicals by the catalytic improvement carried out in the hydropyrolysis reactor. The catalysts typically selected for this step are high activity hydroconversion catalysts, for example, sulfite NiMo and sulfite CoMo catalysts. In this second reaction stage, the catalyst can be used
    Petition 870180126858, of September 5, 2018, p. 36/71
    11/11 to catalyze the water-gas displacement reaction of CO + H2O to produce CO2 + H 2 , thus allowing the in-situ production of hydrogen, which in turn reduces the hydrogen required for hydroconversion . Both NiMo and C0M0 catalysts catalyze the water-gas displacement reaction.
    [025] According to an embodiment of the present invention, the biomass feed is an aquatic biomass, possibly containing a high proportion of lipids, such as algae or aquatic plants with a low amount of lipids, such as Lemna. The integrated process of the present invention is ideal for the conversion of aquatic biomass, since the same can be carried out on aquatic biomass which is normally only partially dehydrated and still capable of producing high yields of gaseous product.
    [026] Fig. 2 shows an additional embodiment of the method of the present invention in which the product of the CO2 separation unit 18 is supplied for a methane hydrate recovery process 25 which produces a stream of pure methane and a stream of H 2 that can be recycled back to the first stage 10 hydropyrolysis reactor vat. Using the methane hydrate recovery process eliminates the need for the methanator and produces a much purer methane product.
    [027] Although the preceding specification of the present invention has been described in relation to certain preferred embodiments of it and many details have been presented for purposes of illustration, it will be apparent to those skilled in the art that the invention is susceptible to additional modalities and that certain of the details described here can vary considerably without departing from the basic principles of the invention.
    权利要求:
    Claims (17)
    [1]
    1. Method for producing methane from biomass CHARACTERIZED by the fact that it comprises the steps of:
    a) hydropyrolize the biomass in a hydropyrolysis reactor vat containing molecular hydrogen and a deoxygenation catalyst at a hydropyrolysis temperature greater than 1000 ° F and a pyrolysis pressure in the range of 689 kPa to 4136 kPa (100 to 600 psig) , producing a hydropyrolysis product comprising coal and vapors;
    b) separating said coal from said hydropyrolysis product, producing a reduced coal hydropyrolysis product;
    c) hydroconverting said reduced carbon hydropyrolysis product in a hydroconversion reactor vat using a hydroconversion catalyst at a hydropyrolysis temperature greater than 800 ° F and a pyrolysis pressure in the range of 689 kPa to 4136 kPa (100 to 600 psig), producing a hydroconversion product;
    d) cooling and introducing said hydroconversion product into a water-gas displacement reactor, producing a water-gas displacement product and separating condensed liquid water from said water-gas displacement product to provide a gas mixture comprising CO2, H 2 and methane, wherein said gas mixture is free of coal;
    e) separating said CO 2 , H 2 and methane, producing a stream of CO 2 , a stream of H 2 and a stream of methane product;
    f) introducing at least a first portion of said methane product and said condensed liquid water into a steam reformer in which said first portion of said methane product stream is reformed, producing reformer CO 2 and reformer H 2 ; and
    g) introducing at least a second portion of the said methane product stream into a methanation reactor, in which at least a portion of the reformer H 2 is introduced into a methanation reactor, reacting with any remaining CO and / or CO 2 in a second portion of the methane product stream and forming additional methane, through which a second portion of said methane product stream is made suitable for a pipeline system.
    Petition 870190021627, of 03/05/2019, p. 21/24
    [2]
    2/4 natural gas, where step a) to hydropyrolize and step c) to hydroconverter are exothermic.
    2. Method according to claim 1, CHARACTERIZED by the fact that water from an external source is introduced into the steam reformer for the reforming of said first portion of said stream of methane product.
    [3]
    3. Method according to claim 1, CHARACTERIZED by the fact that a first part of said first portion of said stream of methane product that is introduced into the steam reformer is introduced into a combustion and burned, thereby heating a second part of said first portion of said stream of methane product which is introduced into the steam reformer together with said condensed liquid water, forming said reformer CO2 and said reformer H 2 .
    [4]
    4. Method according to claim 1, CHARACTERIZED by the fact that a portion of the charcoal separated from said hydropyrolysis product is burned in an oven, thus heating said first portion of said pyrolysis product stream which is introduced into the steam reformer together with said condensed liquid water, forming said reformer CO2 and said reformer H 2 .
    [5]
    5. Method according to claim 1, CHARACTERIZED by the fact that a portion of said coal separated from said hydropyrolysis product is burned in a combustion chamber of a steam boiler for the production of steam from said liquid water condensate, the steam of which is introduced into the steam reformer together with said first portion of said stream of methane product.
    [6]
    6. Method according to claim 1, CHARACTERIZED by the fact that at least a portion of said reformer H 2 is recycled to said hydropyrolysis reactor tank for said hydropyrolization of said biomass.
    [7]
    7. Method according to claim 1, CHARACTERIZED by the fact that said deoxygenation catalyst or said hydroconversion catalyst is a glass-ceramic material.
    [8]
    8. Method, according to claim 1, CHARACTERIZED by the fact that
    Petition 870190021627, of 03/05/2019, p. 22/24
    3/4 that said hydropyrolysis is carried out at an hourly space speed by weight in a range of 0.2 to 10 gm of biomass / gm of catalyst / hr.
    [9]
    9. Method, according to claim 1, CHARACTERIZED by the fact that said hydroconversion is performed at an hourly space speed in weight in a range of 0.2 to 3 gm of biomass / gm of catalyst / hr.
    [10]
    10. Method according to claim 1, CHARACTERIZED by the fact that said hydropyrolysis reactor tank is a fluidized bed reactor containing a fluidized bed.
    [11]
    11. Method according to claim 10, CHARACTERIZED by the fact that a gas residence time in said hydropyrolysis reactor tank is less than one minute.
    [12]
    12. Method according to claim 10, CHARACTERIZED by the fact that said coal is removed from said fluidized bed reactor substantially only from above said fluidized bed.
    [13]
    13. Method according to claim 1, CHARACTERIZED by the fact that said hydropyrolysis reactor tank is a fluidized bed reactor containing a fluidized bed and said coal is removed from said fluidized bed reactor by separating the energy coal employing an inertial, electrostatic or magnetic process.
    [14]
    14. Method, according to claim 1, CHARACTERIZED by the fact that said deoxygenation catalyst is selected from the group consisting of catalytically active glass-ceramic catalysts of sulphite CoMo, sulphite NiMo, bauxite, and mixtures and combinations of the same.
    [15]
    15. Method, according to claim 1, CHARACTERIZED by the fact that a hot gas filter preheated by injection of selected mixtures or unique adsorbents is used to remove selected impurities from a gas leaving the reactor tank. hydropyrolysis and the hydroconversion reactor tank.
    [16]
    16. Method, according to claim 1, CHARACTERIZED by the fact that said portion of reformer H 2 that is introduced into said methanation reactor is H 2 that is separated from said reformer CO 2 through the use of oscillation adsorption pressure (PSA).
    [17]
    17. Method, according to claim 1, CHARACTERIZED by the fact
    Petition 870190021627, of 03/05/2019, p. 23/24
    4/4 that it also comprises a reaction of changing the water vapor in the gases of the said hydroconversion product.
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    法律状态:
    2018-05-29| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2018-12-04| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2019-08-13| B09A| Decision: intention to grant|
    2019-10-22| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 09/06/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US12/815,743|US8915981B2|2009-04-07|2010-06-15|Method for producing methane from biomass|
    PCT/US2011/001048|WO2011159334A1|2010-06-15|2011-06-09|Method for producing methane from biomass|
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