Method for manufacturing valuable materials, apparatus for manufacturing valuable materials, and system for manufacturing valuable materials

Abstract

To provide a method for producing valuable materials, a valuable materials production apparatus, and a valuable materials production system that can reduce variations in the composition of the gas used to produce valuable materials and predict the amount of valuable materials produced. [Solution] According to one aspect of the present invention, a method for producing a valuable substance is provided, comprising: a first step of removing at least one of solid impurities and water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide and impurities; a second step of removing gaseous impurities from the raw material gas after the first step; a third step of separating and recovering a carbon monoxide-containing gas containing carbon monoxide from the raw material gas after the second step; and a fourth step of producing a valuable substance from the carbon monoxide-containing gas.

Description

[Technical Field]

[0001] This invention relates to a method for manufacturing valuable materials, an apparatus for manufacturing valuable materials, and a system for manufacturing valuable materials. [Background technology]

[0002] In recent years, the massive consumption of oils and alcohols produced from petroleum has led to concerns about the depletion of fossil fuel resources and global environmental problems such as the increase in carbon dioxide in the atmosphere. To address these issues, methods for producing organic substances using raw materials other than petroleum, such as the production of bioethanol from edible raw materials like corn through sugar fermentation, are attracting attention. Such sugar fermentation methods using edible raw materials may lead to soaring food prices because they require the use of limited farmland for non-food production. Therefore, methods are being considered to produce organic substances that were previously manufactured from petroleum using waste materials (garbage) that would otherwise be discarded.

[0003] For example, Patent Document 1 discloses a method for producing organic matter by supplying a gas with a higher carbon dioxide content than air, partially oxidizing waste (garbage) as a carbon source to generate synthesis gas containing carbon monoxide, and then fermenting this synthesis gas with microorganisms. However, synthesis gas produced from waste is prone to variations in gas composition. Therefore, it is difficult to predict the amount of organic matter (valuable material) produced by microbial fermentation. This problem stems from the gas composition of the synthesis gas, and the same applies when using a catalyst to produce organic substances (valuable materials) from synthesis gas. [Prior art documents] [Patent Documents]

[0004] [Patent Document 1] Japanese Patent Publication No. 2015-077120 [Overview of the project] [Problems that the invention aims to solve]

[0005] In view of the above circumstances, the present invention aims to provide a method for producing valuable materials, a apparatus for producing valuable materials, and a system for producing valuable materials that can reduce variations in the composition of the gas used to produce valuable materials and predict the amount of valuable materials produced. [Means for solving the problem]

[0006] According to one aspect of the present invention, a method for producing a valuable substance is provided, comprising: a first step of removing at least one of solid impurities and water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide, and impurities; a second step of removing gaseous impurities from the raw material gas after the first step; a third step of separating and recovering a carbon monoxide-containing gas containing carbon monoxide from the raw material gas after the second step; and a fourth step of producing a valuable substance from the carbon monoxide-containing gas.

[0007] According to this configuration, the amount of valuable material produced can be predicted. [Brief explanation of the drawing]

[0008] [Figure 1] This is a schematic diagram showing the configuration of a manufacturing system for valuable materials according to one embodiment. [Modes for carrying out the invention]

[0009] The following describes in detail the method for manufacturing valuable materials, the apparatus for manufacturing valuable materials, and the system for manufacturing valuable materials, based on the preferred embodiments shown in the attached drawings. Figure 1 is a schematic diagram showing the configuration of a valuable material manufacturing system according to one embodiment. The valuable product manufacturing system 100 shown in FIG. 1 (hereinafter, also simply referred to as "manufacturing system 100") includes a gasification furnace (gas generation unit for generating raw material gas) 10 and a valuable product manufacturing apparatus 1 (hereinafter, also simply referred to as "manufacturing apparatus 1") connected to the gasification furnace 10. In this specification, the upstream side with respect to the flow direction of gas and liquid is simply described as "upstream side", and the downstream side is simply described as "downstream side".

[0010] In this embodiment, the gasification furnace 10 is not particularly limited, and examples thereof include a fluidized bed furnace, a kiln furnace, a shaft furnace, etc. The gas generation unit may be at least one business site selected from a combustion furnace (incinerator), a paper mill, a cement factory, a thermal power plant, an essential oil plant, an ethylene cracker, an oil refinery, a chemical factory, a blast furnace, a converter or an electric furnace (electric furnace) in an ironworks, in addition to the gasification furnace 10, and may be a CO X emission source. In each furnace, a raw material gas (hereinafter, also simply referred to as "raw material gas") containing hydrogen, carbon monoxide, carbon dioxide and impurities is generated (occurred) during combustion, melting, refining, etc. of the contents.

[0011] In the case of a combustion furnace or a gasification furnace 10 in a waste incineration plant, examples of the contents (waste) include plastic waste, raw garbage, municipal solid waste (MSW), industrial waste, waste tires, biomass waste, household garbage (quilts, papers), building materials, etc. These wastes may contain one kind alone or two or more kinds. In the case of a blast furnace, a converter or an electric furnace in an ironworks, for example, raw material gas is generated (occurred) when heating iron ore together with coke, limestone, etc. In the case of a chemical factory, for example, raw material gas is generated (occurred) when steam reforming methane or when debinding during the manufacture of a ceramic sintered body.

[0012] The carbon in the raw material gas derived from waste, etc. is different from the carbon in petroleum in terms of the abundance ratio of carbon isotopes such as 14 C, 13 C (for example, δ 14 C, δ 13The value of C) is different. Therefore, the abundance ratio of carbon isotopes contained in the valuable product produced by the production system 100 from such a raw material gas is also different from that of the valuable product derived from petroleum. Therefore, even if the valuable product produced by the production system 100 is converted into other compounds and used, it can be discriminated (traced) that it is derived from the valuable product produced by the method with a low environmental impact by the production system 100.

[0013] In addition to hydrogen, carbon monoxide, carbon dioxide and impurities, the raw material gas may usually contain other gas components such as nitrogen, oxygen, water vapor, methane, etc. Impurities include solid impurities, gaseous impurities, water-soluble impurities, etc. Specific examples of impurities include, for example, soot, tar, nitrogen compounds, sulfur compounds, phosphorus-based compounds, aromatic compounds, etc. The raw material gas may be produced as a gas containing 10% by volume or more of carbon monoxide by performing a heat treatment (commonly known as gasification) for incompletely burning the content (carbon source) (that is, partially oxidizing the carbon source). If such a raw material gas is used to produce a valuable product, carbon dioxide that has been conventionally discharged into the atmosphere can be effectively utilized, and the environmental load can be reduced. From the perspective of carbon circulation, it is preferable to use the exhaust gas generated in a combustion furnace or a smelter as the raw material gas.

[0014] The gasification furnace 10 may have an oxygen generation device for generating oxygen necessary for combustion. Examples of the oxygen generation device include a cryogenic separation type device capable of compressing, cooling, and liquefying air in the atmosphere to extract liquefied oxygen, liquefied nitrogen, etc. It is preferable to utilize the heat absorption when the obtained liquefied nitrogen vaporizes in the parts of the production system 100 that require cooling. In addition, the nitrogen gas obtained by vaporizing the liquefied nitrogen can be suitably used as a purge gas or the like for each part of the production system 100.

[0015] Further, the gasification furnace 10 may have a reforming area for reforming the raw material gas inside or outside thereof. The reforming area converts hydrocarbons (methane, ethane, char, tar, dioxins, etc.) contained in the raw material gas into carbon monoxide and hydrogen by, for example, keeping the raw material gas at a high temperature. At this time, a combustion-supporting gas such as oxygen or air may be supplied to raise the temperature. Furthermore, some of the carbon monoxide may be converted to carbon dioxide by reacting with oxygen. The temperature is preferably 1000°C or higher, and more preferably 1100°C to 1400°C.

[0016] In the reforming area, a method may be employed in which hydrocarbons such as methane contained in the raw gas are reacted with water vapor at high temperature in the presence of a catalyst to convert them into carbon monoxide and hydrogen. At this time, some of the carbon monoxide may be further converted into carbon dioxide and hydrogen by reacting with water vapor. The reaction temperature is preferably between 500°C and 1200°C. Examples of catalysts include metal catalysts. These metal catalysts include, for example, nickel catalysts, nickel oxide catalysts, ruthenium catalysts, rhodium catalysts, palladium catalysts, and platinum catalysts.

[0017] Here, the stable isotope ratio of carbon δ 13 It is known that carbon (C) tends to have a higher value under high-temperature combustion conditions and a lower value under incomplete combustion conditions. Therefore, by providing a reforming area, the raw material gas can be reformed to produce a unique δ (δ) according to the combustion conditions. 13 It may have a C value. Therefore, even if the valuable material produced by the manufacturing system 100 is converted into other compounds and used, it can be identified (trace) that it originated from the valuable material produced by the manufacturing system 100 using an environmentally friendly method.

[0018] The raw gas (synthesis gas) generated by the gasifier 10 is at a high temperature. The heat of this high-temperature raw gas may be utilized to generate steam from water. For example, a tank storing water may be provided in the middle of the gas line GL1 connected to the downstream side of the gasifier 10, and steam may be generated by heat exchange between the raw gas and water. Further, a heat recovery device (for example, an economizer, a heat pump, etc.) that is more suitable for recovering the high-temperature heat provided near the gas line GL1 near the outlet of the gasifier 10 may be used to generate steam by heat exchange with the raw gas. In this way, by efficiently recovering and utilizing the heat of the raw gas without leaving any, the environmental load during the production of valuable substances can be further reduced. Note that the heat of the raw gas is not limited to the utilization for the above purpose and can be utilized for various purposes. Also, the heat of the gas discharged from the reforming area may be recovered. As a heat recovery method, when a scrubber is used for cooling, the heat energy recovered through the scrubber may be utilized.

[0019] A manufacturing apparatus 1 is connected to such a gasifier 10. This manufacturing apparatus 1 includes a culture tank (valuable substance generation unit) 2, a purification apparatus 6, a gas line GL1 connecting the gasifier 10 and the culture tank 2, and a liquid line LL connecting the culture tank 2 and the purification apparatus 6. In the culture tank 2, a first valuable substance is generated from the processed raw gas (carbon monoxide-containing gas) using microorganisms (particularly, gas-utilizing bacteria or algae). That is, in the culture tank 2, the first valuable substance is generated by microbial fermentation of the raw gas.

[0020] Here, since the first valuable substance generated in the culture tank 2 is generated using carbon derived from the raw gas, it is different from valuable substances derived from petroleum. 14 C, 13 The abundance ratios of carbon isotopes such as C (for example, δ 14 C, δ 13 The value of C) is different. Therefore, even if this first valuable substance is converted and used as a product such as other compounds, it can be discriminated (traced) that it is derived from the first valuable substance generated by a method with a low environmental load by the manufacturing system 100.

[0021] Examples of gas-assimilating bacteria include Butyribacterium methylotrophicum, Clostridium autoethanogenum, Clostridium carboxidivorans, Clostridium ljungdahlii, Clostridium ragsdalei, Moorella, and Carboxydothermus. Examples of algae include cyanobacteria, Chlorella, Botryococcus, Nannochloropsis, Haematococcus, Senedesmus, Stichococcus, Nannochloris, and Desmodesmus.

[0022] When using microorganisms such as gas-utilizing bacteria or algae, in the first valuable substance 14 C, 13 The abundance of carbon isotopes such as ¹¹C (e.g., δ¹¹C) 14 C, δ 13 The value of C can be made to deviate even more significantly from the value of petroleum-derived products. Therefore, even if the first valuable substance generated is converted into other compounds and used, it can be more easily identified (traceable) that it originates from the first valuable substance produced by the environmentally friendly manufacturing system 100.

[0023] The culture medium (culture solution) used when culturing microorganisms is not particularly limited, as long as it has an appropriate composition for the type of microorganism. When using Clostridium bacteria as gas-assimilating bacteria, for example, paragraphs 0097-0098 of U.S. Patent Application Publication No. 2017 / 260552 can be used as a reference for the culture medium. The culture tank 2 can be, for example, a culture reactor that agitates the culture medium with a stirring plate, a culture reactor that agitates the culture medium by circulating the culture medium itself, or a culture reactor that agitates the culture medium with a water flow associated with a bubble flow generated by the aeration of the supplied raw material gas.

[0024] Furthermore, the valuable substance generation section may be composed of a reactor containing a catalyst instead of the culture tank 2. In this case, examples of catalysts include ruthenium, rhodium, manganese, germanium, tantalum, zirconium, niobium, hafnium, lanthanum, cerium, aluminum, magnesium, copper, zinc, silicon, or oxides thereof. These substances may be used individually or in combination of two or more.

[0025] The manufacturing apparatus 1 includes a pre-processing unit (separation unit) 5 located in the middle of the gas line GL1 (i.e., between the gasification furnace 10 and the culture tank 2). This pre-processing unit (separation unit) 5 removes various impurities from the raw material gas containing hydrogen, carbon monoxide, carbon dioxide, and other impurities, and also separates and recovers the carbon monoxide-containing gas, including carbon monoxide. Specifically, the pre-processing unit 5 includes, in order from the upstream side (gasifier 10 side), a dust removal device (first impurity removal unit) 54, a first PSA device (second impurity removal unit) 51, and a second PSA device (recovery unit) 52.

[0026] The dust removal device 54 has the function of removing at least one of solid impurities and water-soluble impurities. By installing this dust removal device 54, the amount of impurities, especially solid impurities (soot generated during combustion in the gasification furnace 10), brought into the first PSA device 51 and the second PSA device 52 can be reduced. As a result, the frequency of maintenance of the first PSA device 51 and the second PSA device 52 can be reduced. In addition, since the amount of soot contained in the raw material gas supplied to the valuable product generation section can be reduced, it becomes less likely to adversely affect microorganisms and catalysts, and the efficiency of the first valuable product generation can be increased. Examples of water-soluble impurities include sulfur compounds such as hydrogen sulfide. Removing sulfur compounds also reduces the likelihood of adverse effects on microorganisms and catalysts in the valuable product generation section.

[0027] This dust removal device 54 can be composed of, for example, a wet washing tower, a filter, and the like. A wet scrubbing tower is a type of scrubber used to remove contaminants (such as soot, compounds containing benzene rings (e.g., naphthalene)) and water-soluble substances contained in the raw gas. In a wet scrubbing tower, the removal process is carried out by bringing a cleaning solution into contact with the object to be removed (wet scrubbing method). One example of a wet scrubbing method is a cleaning method using a water curtain. Examples of cleaning solutions include water, acidic solutions, and alkaline solutions. Among these, water is preferred as the cleaning solution. The temperature of the cleaning solution is usually 40°C or lower, preferably 30°C or lower, more preferably 25°C or lower, and even more preferably 15°C or lower. Filters are used to remove fine particles smaller than the size of soot. These filters can be, for example, bag filters.

[0028] The first PSA device 51 is a pressure swing adsorption type separator and has the function of removing gaseous impurities from the raw material gas after it has passed through the dust removal device (first impurity removal unit) 54. Examples of gaseous impurities include BTEX, carbon dioxide, and nitrogen. The first PSA device 51 comprises a first container, a first adsorbent contained in the first container, and a first vacuum pump connected to the first container. The first adsorbent can consist of one or more porous materials such as zeolite, bentonite, sericite, perlite, coral reef rock, vermiculite, silica gel, molecular sieves, activated carbon, and MOF (metal-organic framework). Among these, activated carbon or zeolite is preferably used as the first adsorbent. By setting the type of porous material and the size of the pores, the compounds that can be separated can be selected.

[0029] When separating two or more compounds in the first PSA apparatus 51, multiple separators filled with porous materials of different types and pore sizes may be used, or a single separator filled with porous materials of different types and pore sizes may be used. The average particle size of the first adsorbent is preferably 0.5 mm to 10 mm, more preferably 0.8 mm to 8 mm, and even more preferably 1 mm to 6 mm. In this case, the contact area of ​​the first adsorbent with the raw material gas can be sufficiently large. The shape is not limited to spherical, but may be cylindrical, for example. In this specification, average particle size means the average value of the particle sizes of any 200 particles in a single field of view observed with an electron microscope. In this context, "particle size" means the maximum distance between any two points on the contour line of the particle.

[0030] Furthermore, the BET specific surface area of ​​the first adsorbent is 50 m². 2 / g or more 1200m 2 It is preferable that it be less than or equal to / g, and 100m 2 / g or more 1000m 2 It is more preferable that it be less than or equal to / g, and 200m 2 / g or more 800m 2 It is even more preferable that the amount is less than or equal to / g. In this case, the contact area of ​​the first adsorbent with the raw material gas can be sufficiently large. In this specification, the BET specific surface area is a value measured using a BET specific surface area meter in accordance with the BET single-point method ("Method for measuring the specific surface area of ​​fine ceramic powder by gas adsorption BET method" as specified in JIS R 1626:1996). The average pore size of the first adsorbent is preferably 0.5 Å to 200 Å, more preferably 2.5 Å to 175 Å, and even more preferably 5 Å to 150 Å. In this specification, the average pore diameter is a value measured by pore diameter distribution measurement using the mercury intrusion method with a mercury porosimeter.

[0031] The method for utilizing the carbon dioxide separated in the first PSA device 51 will be described in detail later. Furthermore, the nitrogen separated in the first PSA device 51 may be used to fill the culture tank 2 when culturing microorganisms (gas-assimilating bacteria), or it may be used to fill the first PSA device 51, the second PSA device 52, and the TSA device (if used) for cleaning (purging). Note that the nitrogen may be filled into only one of the above devices, or into two or more. In this way, by removing nitrogen from the raw material gas, the volume of the raw material gas to be processed downstream can be reduced, thus enabling miniaturization of the pre-processing unit 5 located downstream.

[0032] The second PSA device 52 has the function of separating and recovering carbon monoxide-containing gas, including carbon monoxide, from the raw material gas after it has passed through the first PSA device (second impurity removal unit) 51. The second PSA device 52 comprises a second container, a second adsorbent contained in the second container, and a second vacuum pump connected to the second container. The second adsorbent can be composed of a porous material similar to that of the first adsorbent. Among these, activated carbon, zeolite, or MOF are preferably used as the second adsorbent. This is because they have particularly excellent carbon monoxide adsorption and release capabilities. By setting the type of porous material and the size of the pores, carbon monoxide can be selectively adsorbed.

[0033] The average particle size of the second adsorbent is preferably 0.5 mm or more and 10 mm or less, more preferably 0.8 mm or more and 8 mm or less, and even more preferably 1 mm or more and 6 mm or less. Furthermore, in the case of the first adsorbent and the second adsorbent, if their shapes are elliptical or columnar, the average value of the length of the major axis and the length of the minor axis is defined as the particle size of the adsorbent, and the average value of this particle size is defined as the average particle size of the adsorbent. Furthermore, the BET specific surface area of ​​the second adsorbent is 100 m². 2 / g or more 2500m 2 It is preferable that it be less than / g, and 200m 2 / g or more 2000m 2 It is more preferable that it be less than / g, and 300m 2 / g or more 1500m 2 It is even more preferable that the amount be less than or equal to / g. The average pore size of the second adsorbent is preferably 1 Å or more and 300 Å or less, more preferably 3 Å or more and 250 Å or less, and even more preferably 5 Å or more and 200 Å or less. By appropriately setting these numerical ranges, the contact area of ​​the second adsorbent with the raw material gas can be sufficiently increased.

[0034] A moisture removal device (water vapor removal device) may be provided between the dust removal device 54 and the first PSA device 51. The moisture removal device comprises a container and a moisture adsorbent contained within the container. The moisture adsorbent can be composed of one or more materials, such as alumina, zeolite, or silica gel. Removing moisture (water vapor) upstream of the first PSA unit 51 and the second PSA unit 52 makes it easier to improve the processing efficiency of the raw material gas in the first PSA unit 51 and the second PSA unit 52. Furthermore, since moisture is difficult to remove once it is adsorbed onto a moisture adsorbent, using a relatively inexpensive moisture adsorbent can reduce the manufacturing cost of the first valuable material.

[0035] Furthermore, the moisture removal device is not limited to being a separate device from the first PSA device 51, but may, for example, be integrated with the first PSA device 51. Furthermore, it is preferable that the moisture removal device has an adsorption selectivity ratio of 2 or higher for water vapor to carbon dioxide. In this case, moisture can be selectively (preferentially) removed, and thus the gas density flowing into the area where the adsorbent is placed (contained) in the first PSA device 51 and the second PSA device 52 can be increased. This is preferable because it is expected to extend the lifespan of the adsorbent for hydrogen sulfide removal and carbon dioxide removal. Note that the adsorption selectivity ratio refers to the ratio of the adsorption energy of water vapor to carbon dioxide relative to the adsorbent. Furthermore, the temperature of the moisture removal device is preferably 20°C or lower. By reducing the temperature inside the moisture removal device in this way, the amount of saturated water vapor can be reduced, thereby preventing or suppressing variations in gas composition even within a certain humidity range.

[0036] Furthermore, in addition to the first PSA apparatus 51 and the second PSA apparatus 52, the pre-processing unit 5 may also include, for example, a deoxygenation apparatus, an acetylene deoxygenation apparatus, a TSA apparatus, a PTSA apparatus, etc. These can be used individually or in any combination, and their arrangement order is also arbitrary. Deoxygenation devices are used to remove oxygen and can consist of a reactor packed with metal particles such as copper (Cu), platinum (Pt), or nickel (Ni) as an oxygen removal catalyst. The oxygen removal catalyst is preferably heated to a temperature between 150°C and 400°C. A deacetylene removal apparatus is used to remove acetylene and can consist of a reactor filled with particles of a precious metal such as palladium (Pd) or platinum (Pt) as an acetylene removal catalyst. Furthermore, removing acetylene prior to deoxygenation has the advantage of effectively preventing or reducing the adverse effects of acetylene on the oxygen removal catalyst.

[0037] The TSA device is a temperature swing adsorption type separator, used, for example, to remove aromatic compounds other than BTEX. The PTSA device is a pressure and temperature swing adsorption type separator, and is used, for example, to remove components that are removed by the first PSA device 51, the second PSA device 52, and the TSA device all at once. The type of adsorbent and constituent materials used in the TSA and PTSA devices can be the same as those described for the first PSA device 51 and the second PSA device 52.

[0038] The raw material gas processed in the pre-processing unit 5 (carbon monoxide-containing gas separated and recovered in the second PSA device 52) is supplied to the culture tank 2. With such a carbon monoxide-containing gas, variations in its composition can be reduced. Therefore, the amount of the first valuable substance produced in the culture tank (valuable substance production unit) 2 can be predicted. Consequently, the valuable substance production system 100 can be operated stably. The concentration of carbon monoxide in the carbon monoxide-containing gas supplied to the culture tank 2 is preferably 10% by volume or more and 90% by volume or less, more preferably 15% by volume or more and 70% by volume or less, and even more preferably 20% by volume or more and 45% by volume or less.

[0039] The concentration of carbon dioxide in the carbon monoxide-containing gas supplied to the culture tank 2 is preferably 0.1% by volume or more and 30% by volume or less, more preferably 0.3% by volume or more and 25% by volume or less, even more preferably 0.5% by volume or more and 20% by volume or less, particularly preferably 0.8% by volume or more and 15% by volume or less, and most preferably 1% by volume or more and 10% by volume or less. Furthermore, the concentration of hydrogen in the carbon monoxide-containing gas supplied to the culture tank 2 is preferably 20% by mass or less, more preferably 15% by mass or less, even more preferably 10% by mass or less, and particularly preferably 0.1% by mass or more and 5% by mass or less. By reducing the concentration of hydrogen in the carbon monoxide-containing gas, it is possible to sufficiently suppress variations in the composition of the carbon monoxide-containing gas over time.

[0040] Furthermore, the nitrogen concentration in the carbon monoxide-containing gas supplied to the culture tank 2 is preferably 30% by volume or less, more preferably 1% to 25% by volume, and even more preferably 5% to 20% by volume. Because this carbon monoxide-containing gas is supplied to culture tank 2, hydrogen is less likely to reduce the activity of microorganisms (gas-utilizing bacteria). In other words, since hydrogen at a concentration suitable for use by microorganisms can be supplied, the microorganisms can work actively. Furthermore, the carbon monoxide-containing gas is sufficiently concentrated because carbon dioxide and nitrogen are mainly separated (removed) in the first PSA device 51, and carbon monoxide is selectively separated and recovered in the second PSA device 52. Therefore, the first valuable substance can be produced more efficiently in culture tank 2. Furthermore, since the overall volume of the raw material gas is reduced, the size of the piping, pumps, containers, etc., located in the pre-processing unit 5 and / or downstream thereof can also be reduced.

[0041] In culture tank 2, a first valuable substance, specifically a liquid containing the first valuable substance, is generated from carbon monoxide-containing gas using microorganisms (gas-utilizing bacteria or algae). A purification device 6 is connected to culture tank 2 via liquid line LL. This purification device 6 is a device that purifies a first valuable substance (organic substance) from a liquid containing valuable substances. Examples of such purification apparatus 6 include distillation apparatus, permeable vaporization membrane apparatus, zeolite dehydration membrane apparatus, organic membrane apparatus, apparatus for removing low-boiling-point substances with a boiling point lower than the first valuable substance, apparatus for removing high-boiling-point substances with a boiling point higher than the first valuable substance, and apparatus for removing ion exchange membrane. These apparatuses may be used individually or in combination of two or more types.

[0042] When using a distillation apparatus, for example, the temperature inside the distillation apparatus during the distillation of ethanol, which is the first valuable substance, is not particularly limited, but is preferably 100°C or lower, and more preferably 70°C to 95°C. By setting the temperature to this level, the separation of the required first valuable substance from other components, i.e., the distillation (purification) of the first valuable substance, can be performed more reliably. The pressure inside the distillation apparatus during the distillation of the first valuable substance may be atmospheric pressure, but it is preferably less than atmospheric pressure (reduced pressure distillation), and more preferably between 60 kPaA and 95 kPaA. By setting the pressure to this level, the separation efficiency of the first valuable substance can be improved, and consequently, the yield of the first valuable substance can be increased.

[0043] Furthermore, for example, the temperature inside the distillation apparatus during the distillation of acetic acid, the first valuable substance, is not particularly limited, but is preferably 95°C or higher, and more preferably 100°C to 150°C. The pressure inside the distillation apparatus during the distillation of the first valuable substance may be atmospheric pressure, but it is preferably less than atmospheric pressure (reduced pressure distillation), and more preferably between 60 kPaA and 95 kPaA. Setting the pressure to this level improves the separation efficiency of the first valuable substance and, consequently, the yield of the first valuable substance. In addition, azeotropes and the like may be added to the liquid containing the valuable substance. The yield of the first valuable substance (concentration of the first valuable substance in the purified product) is preferably 90% by mass or more, more preferably 99% by mass or more, and even more preferably 99.5% by mass or more.

[0044] The first valuable substance obtained in this way may include, for example, monools such as methanol and ethanol, diols such as 2,3-butanediol, acetic acid, lactic acid, isoprene, butadiene, and is preferably a monool or diol having 1 to 4 carbon atoms, and more preferably ethanol. Such first valuable substance can be used, for example, as a raw material for resin materials, rubber materials, etc., and can also be used as various solvents, disinfectants, or fuels. Furthermore, high-concentration ethanol can be used as fuel ethanol mixed with gasoline, etc., and can also be used as a raw material for cosmetics, beverages, chemicals, fuels (jet fuel), etc., and as an additive for food, etc., making it extremely versatile.

[0045] The manufacturing apparatus 1 includes a synthesis unit (second valuable substance generation unit) 7 connected to the first PSA apparatus 51 via gas line GL2 and to the second PSA apparatus 52 via gas line GL3. In the synthesis unit 7, carbon dioxide separated in at least the first PSA unit 51 and hydrogen separated in the second PSA unit 52 are reacted using a catalyst to produce a second valuable product. The second valuable substance preferably contains at least one selected from the group consisting of amino acids, aliphatic hydrocarbons, alcohols, ketones, and carboxylic acids.

[0046] Examples of catalysts capable of producing amino acids as a second valuable substance include metalloporphyrin catalysts, metal-organic frameworks (MOFs), metal or alloy catalysts containing gold, copper, ruthenium, etc., microbial catalysts such as purple photosynthetic bacteria, and oxide-based ceramic catalysts containing cerium oxide and zirconium oxide. Examples of catalysts capable of producing aliphatic hydrocarbons as a second valuable material include metal or alloy catalysts containing copper, iron, etc., oxide catalysts containing cerium oxide, titanium oxide, etc., composite catalysts containing the above metal or alloy catalysts and the above oxide catalysts in any combination, metal complex catalysts containing ruthenium, etc., organic group modified zeolite catalysts, petroleum metabolic bacteria, and the like.

[0047] Examples of catalysts capable of producing alcohol as a second valuable substance include metal or alloy catalysts containing copper, silver, nickel, zinc, zirconium, etc., oxide catalysts containing zinc oxide, titanium oxide, etc., composite catalysts containing the above metal or alloy catalysts and the above oxide catalysts in any combination, carbon-supported catalysts in which metal nanoparticles are supported on a carbon material, and metal complex catalysts containing iridium, etc. Among these, palladium-molybdenum intermetallic compound catalysts are preferred as catalysts capable of producing methanol as a second valuable substance. Such catalysts can produce methanol from carbon dioxide and hydrogen at extremely low temperatures (room temperature).

[0048] Examples of catalysts capable of producing ketones as a second valuable substance include metal or alloy catalysts containing palladium, ruthenium, etc., oxide catalysts containing titanium dioxide, etc., and composite catalysts containing the above metal or alloy catalysts and the above oxide catalysts in any combination. Examples of catalysts capable of producing carboxylic acids as a second valuable substance include MOFs containing copper, zirconium, etc., metal or alloy catalysts containing palladium, ruthenium, rhodium, etc., oxide catalysts containing titanium dioxide, etc., composite catalysts containing the above metal or alloy catalysts and the above oxide catalysts in any combination, alkyllithium compounds, and the like.

[0049] Furthermore, removal sections 8 may be provided in the middle of gas lines GL2 and GL3, respectively. These removal sections 8 have the function of removing impurities contained in the gas separated (recovered) from the first PSA device 51 or the second PSA device 52 that reduce the reactivity of the catalyst. If the separated carbon dioxide or hydrogen is of high purity, the removal unit 8 does not need to be provided. Such impurities are not particularly limited, but include sulfur or sulfur compounds, chlorine or chlorine compounds, cyanide compounds, etc. Among these, it is preferable to remove sulfur compounds, especially hydrogen sulfide, as impurities. By removing hydrogen sulfide, it is possible to effectively prevent the catalyst from becoming extremely less reactive or deactivated.

[0050] Such removal unit 8 can be composed of, for example, a reactor filled with a desulfurizing agent. Examples of desulfurizing agents include iron oxide-based desulfurizing agents, activated carbon-based desulfurizing agents, copper-zinc-based desulfurizing agents, copper-zinc-aluminum-based desulfurizing agents, and lime-based desulfurizing agents. Furthermore, by using an iron oxide-based desulfurizing agent, the iron sulfide produced by the reaction with hydrogen sulfide can react with oxygen, thus allowing oxygen to be removed from the gas passing through gas lines GL2 and GL3. Furthermore, after merging gas line GL2 and gas line GL3, a removal section 8 may be provided in the middle of the merged gas line.

[0051] Furthermore, a hydrogen separation device may be provided upstream or downstream of the removal section 8 of the gas line GL3. Preferably, this hydrogen separation device can consist of a separator containing a separation membrane that selectively permeates and separates hydrogen. Examples of materials that make up such a separation membrane include metal materials, ceramic materials, resin materials, and the like. Examples of metallic materials include Pd-Cu alloys, Pd-Ag alloys, vanadium alloys, and amorphous alloys such as La-Ni-Mg alloys. Examples of ceramic materials include titanium nitride, zeolite, silica (glass), alumina, and composite materials containing one or more of these (e.g., alumina-carbon materials). Examples of resin materials include polyamide, polyimide, and polysulfone.

[0052] The separation membrane is preferably made of a porous material having continuous pores (pores that penetrate the cylindrical wall) where adjacent pores communicate with each other. With a separation membrane of this configuration, hydrogen separation can be performed more smoothly and reliably. The porosity of the separation membrane is not particularly limited, but is preferably between 10% and 90%, and more preferably between 20% and 60%. This prevents an extreme decrease in the mechanical strength of the separation membrane while maintaining a sufficiently high hydrogen permeability. The shape of the separation membrane is not particularly limited and can be cylindrical, square, hexagonal, or other rectangular shapes. The average pore size of the separation membrane is preferably 500 pm or less, and more preferably 300 pm to 400 pm. This allows for a further improvement in hydrogen separation efficiency.

[0053] Next, the method of using the manufacturing system 100 of this embodiment (method of manufacturing valuable materials) will be described. [1] First, raw material gas is generated by burning a gasification raw material containing organic matter in a gasification furnace 10 (a step preceding the first step). [2] Next, the raw material gas (exhaust gas containing hydrogen, carbon monoxide, carbon dioxide, impurities and other gaseous components) discharged from the gasification furnace 10 is supplied to the pre-treatment unit 5. First, the dust removal device 54 removes at least one of solid impurities and water-soluble impurities (for example, soot, fine particles smaller than soot, water-soluble substances, etc.) from the raw material gas (first step).

[0054] [3] Next, the first PSA unit 51 removes gaseous impurities from the raw material gas after the first process (second process). That is, in this process [3] (second process), the removal of gaseous impurities is carried out using the first PSA unit 51.

[0055] Furthermore, it is preferable that impurities (such as water vapor, hydrogen sulfide, and carbon dioxide) are stored within the first PSA device 51 or removed using various adsorbents provided separately. Here, the adsorption performance of various adsorbents is shown in Table 1 below, indicating the percentage reduction in water vapor, hydrogen sulfide, and carbon dioxide content from the raw material gas used in this process [3] (in this case, the raw material gas after passing through the scrubber).

[0056] [Table 1]

[0057] Now, let's explain Table 1. Table 1 shows the degree to which each adsorbent adsorbs, in the order of water vapor / hydrogen sulfide / carbon dioxide. The criteria for each impurity, rated as "◎", "〇", "△", and "×", are as follows: [water vapor] ◎: The content was reduced by 95% to 100% compared to the raw material gas used in this process [3]. ○: The content was reduced by 80% to less than 95% from the raw material gas used in this process [3]. △: The content was reduced by 20% to less than 80% from the raw material gas used in this process [3]. ×: The content was reduced by less than 20% from the raw material gas used in this process [3].

[0058] [Hydrogen sulfide] ◎: The content was reduced by 90% to 100% compared to the raw material gas used in this process [3]. ○: The content was reduced by 70% to less than 90% from the raw material gas used in this process [3]. △: The content was reduced by 20% to less than 70% from the raw material gas used in this process [3]. ×: The content was reduced by less than 20% from the raw material gas used in this process [3]. [carbon dioxide] ◎: The content was reduced by 60% to 100% compared to the raw material gas used in this process [3]. ○: The content was reduced by 40% to less than 60% from the raw material gas used in this process [3]. △: The content was reduced by 20% to less than 40% from the raw material gas used in this process [3]. ×: The content was reduced by less than 20% from the raw material gas used in this process [3]. Note that the content of each impurity is the value measured based on the amount of gaseous component according to the concentration standard.

[0059] The overall results column was evaluated based on the content of impurities (water vapor / hydrogen sulfide / carbon dioxide) in the raw material gas after the completion of this process [3], according to the following criteria. ◎: The content of all impurities was within the most preferable range. ○: The content of at least one impurity exceeded the most preferable range, but was within 15%. ×: The content of at least one impurity was above the most preferable range and also above 15%. Furthermore, the lifespan of the hydrogen sulfide adsorbent (second adsorbent) was evaluated according to the following criteria, with the first example set as 100%. ◎: Performance was maintained for over 90% of the days. ○: Performance was maintained for 80% to less than 90% of the days. ×: Performance could only be maintained for less than 80% of the days.

[0060] In the first example, the first adsorbent used was a zeolite with high water vapor removal performance as a water vapor remover. The second adsorbent used was a zeolite with high hydrogen sulfide removal performance as a hydrogen sulfide remover. The third adsorbent used was a zeolite with high carbon dioxide removal performance as a carbon dioxide remover. The fourth adsorbent used was a zeolite with high carbon dioxide removal performance as a carbon dioxide remover. The first adsorbent was able to remove mainly water vapor, and the raw gas that reached the second adsorbent contained very little water vapor. Therefore, although the water vapor removal rate of the second adsorbent was low, it was able to remove most of the remaining water vapor. Consequently, the raw gas that reached the third and fourth adsorbents contained very little water vapor. Furthermore, since a small amount of hydrogen sulfide was removed by the first adsorbent and sufficient hydrogen sulfide was removed by the second adsorbent, the amount of hydrogen sulfide contained in the raw gas reaching the third adsorbent was extremely small. Consequently, the hydrogen sulfide removal rate in the third adsorbent was extremely low. Furthermore, neither the first nor the second adsorbent adsorbed much carbon dioxide, the third adsorbent mainly adsorbed carbon dioxide, and the fourth adsorbent adsorbed some of the carbon dioxide that the third adsorbent was unable to adsorb.

[0061] In the second example, the configuration was the same as in the first example, except that alumina, which has high water vapor removal performance, was used as the first adsorbent for removing water vapor. The first adsorbent was able to remove mainly water vapor, and the raw gas that reached the second adsorbent contained very little water vapor. Therefore, although the water vapor removal rate of the second adsorbent was low, it was able to remove most of the remaining water vapor. Consequently, the raw gas that reached the third and fourth adsorbents contained very little water vapor. Furthermore, since a small amount of hydrogen sulfide was removed by the first adsorbent and sufficient hydrogen sulfide was removed by the second adsorbent, the amount of hydrogen sulfide contained in the raw gas reaching the third adsorbent was extremely small. Consequently, the hydrogen sulfide removal rate in the third adsorbent was extremely low. Furthermore, neither the first nor the second adsorbent adsorbed much carbon dioxide, while the third adsorbent primarily adsorbed carbon dioxide.

[0062] In the third example, the configuration was the same as in the first example, except that the first adsorbent was a different zeolite from the first example, which had high water vapor removal performance and also possessed some hydrogen sulfide removal performance, and the fourth adsorbent was not used. The first adsorbent was able to remove mainly water vapor, and the raw gas that reached the second adsorbent contained very little water vapor. Therefore, although the water vapor removal rate of the second adsorbent was low, it was able to remove most of the remaining water vapor. Consequently, the raw gas that reached the third and fourth adsorbents contained very little water vapor. Furthermore, since a small amount of hydrogen sulfide was removed by the first adsorbent and sufficient hydrogen sulfide was removed by the second adsorbent, the amount of hydrogen sulfide contained in the raw gas reaching the third adsorbent was extremely small. Consequently, the hydrogen sulfide removal rate in the third adsorbent was extremely low. Furthermore, neither the first nor the second adsorbent adsorbed much carbon dioxide, while the third adsorbent primarily adsorbed carbon dioxide.

[0063] In the fourth example, the configuration was the same as in the first example, except that the first adsorbent was a different zeolite from the first example, which had high water vapor removal performance and some hydrogen sulfide removal performance, and the third adsorbent had low carbon dioxide removal performance. The first adsorbent was able to remove mainly water vapor, and the raw gas that reached the second adsorbent contained very little water vapor. Therefore, although the water vapor removal rate of the second adsorbent was low, it was able to remove most of the remaining water vapor. Consequently, the raw gas that reached the third and fourth adsorbents contained very little water vapor. Furthermore, since a small amount of hydrogen sulfide was removed by the first adsorbent and hydrogen sulfide was removed by the second adsorbent, the amount of hydrogen sulfide contained in the raw gas reaching the third adsorbent was extremely small. Consequently, the hydrogen sulfide removal rate by the third adsorbent was extremely low. Furthermore, neither the first nor the second adsorbent adsorbed much carbon dioxide, the third adsorbent mainly adsorbed carbon dioxide, and the fourth adsorbent adsorbed the carbon dioxide that the third adsorbent was unable to adsorb.

[0064] In the fifth example, the configuration was the same as in the first example, except that the first and fourth adsorbents were omitted. It was found that using only the second and third adsorbents tended to reduce the rate of impurity removal. Furthermore, it was found that the lifespan of the hydrogen sulfide removal agent (the second adsorbent) also tends to be shortened. Therefore, Table 1 shows that it is preferable to use the first adsorbent.

[0065] [4] Next, in the second PSA apparatus 52, carbon monoxide-containing gas is separated and recovered from the raw material gas after the second process (third process). That is, in this process [4] (third process), the separation of carbon monoxide-containing gas is performed using the second PSA apparatus 52. With this method, the amount of carbon monoxide-containing gas to be recovered can be easily changed by controlling the pressure of the second PSA apparatus 52. In addition, it is easier to increase the concentration of carbon monoxide in the carbon monoxide-containing gas compared to when carbon monoxide is produced using a catalyst or when gases other than carbon monoxide are separated from the raw material gas after the second process. Furthermore, in the pre-treatment stage 5, for example, oxygen, acetylene, aromatic compounds other than BTEX, etc., may be removed from the raw material gas.

[0066] [5] Subsequently, the carbon monoxide-containing gas (the raw material gas that has passed through the pretreatment section 5) is supplied to the culture tank 2. In the culture tank 2, a first valuable substance, specifically a valuable substance-containing liquid containing the first valuable substance, is produced from the carbon monoxide-containing gas (fourth step). That is, in this step [5] (fourth step), the first valuable substance is produced using microorganisms. In this way, the carbon monoxide-containing gas obtained by selectively separating carbon monoxide from the raw material gas can be prevented or suppressed from having variations in the concentration of hydrogen it contains, i.e., variations in the gas composition. Therefore, the amount of the first valuable substance produced can be predicted without separately confirming the composition of the carbon monoxide-containing gas. The concentrations of each gas component contained in the carbon monoxide-containing gas are preferably adjusted to the above range. When a series of steps in the method for producing a valuable product are considered as one cycle and multiple cycles are repeated, it is preferable that the concentrations are adjusted to the above range in each cycle.

[0067] Here, the temperature at which the valuable substance-containing liquid is produced in the culture tank (valuable substance production section) 2 is preferably 25°C or higher and 50°C or lower, more preferably 30°C or higher and 45°C or lower, and even more preferably 35°C or higher and 40°C or lower. When generating a liquid containing valuable substances in culture tank 2, the nitrogen removed (separated) by the first PSA device 51 may be used to fill culture tank 2. In this case, the concentration of oxygen contained in the space within culture tank 2 can be relatively reduced, preventing or mitigating adverse effects of oxygen on microorganisms (gas-utilizing bacteria or algae).

[0068] [6] Next, the valuable substance-containing liquid produced in the culture tank 2 is supplied to the purification device 6 via the liquid line LL. In the purification device 6, the first valuable substance contained in the valuable substance-containing liquid is purified, and a purified product containing the first valuable substance at a high concentration is obtained. [7] Meanwhile, the gas containing carbon dioxide and other substances separated in the first PSA unit 51 is supplied to the synthesis unit 7 via the gas line GL2. In addition, the gas mainly containing hydrogen separated in the second PSA unit 52 is supplied to the synthesis unit 7 via the gas line GL3. At this time, the gas flowing through gas lines GL2 and GL3 passes through the removal section 8, thereby removing sulfur compounds (especially hydrogen sulfide), and thus preventing or suppressing a decrease in the activity of the catalyst in the synthesis section 7.

[0069] In the synthesis section (second valuable product production section) 7, at least hydrogen and carbon dioxide separated from the raw material gas are reacted using a catalyst to produce a second valuable product (a step after the third step). The second valuable substance preferably contains at least one selected from the group consisting of carbon monoxide, amino acids, alkanes, alkenes, alcohols, ketones, and carboxylic acids. Furthermore, other valuable substances may be synthesized from carbon monoxide in the synthesis section 7. For example, when producing methanol as a second valuable product, if a palladium-molybdenum intermetallic compound catalyst is used as the catalyst, methanol can be efficiently produced from carbon dioxide and hydrogen under pressurized conditions (e.g., around 0.9 MPa) and at room temperature (e.g., around 25°C).

[0070] Such second valuable material can be used, for example, as a raw material for resin materials, rubber materials, cosmetics, beverages, etc., or as an additive for food products, etc. With the above configuration, the separated carbon dioxide can be converted into the second valuable material, thus enabling the effective utilization of carbon dioxide. Furthermore, the raw material gas supplied to the above process [2] (first process) may be produced by introducing a substance containing a second valuable substance into a gas generation unit (for example, a gasification furnace 10) and burning this substance in the gas generation unit. Examples of the substance containing the second valuable substance include the above-mentioned resin material, rubber material, cosmetics, beverages, food, etc.

[0071] Furthermore, the raw material gas supplied to the above process [2] (first process) may be produced by feeding waste containing a second valuable material into a gas generation unit (for example, a gasification furnace 10) and burning the waste in the gas generation unit. Examples of waste containing a second valuable material include waste from articles made of the above-mentioned resin material and rubber material, as well as waste from cosmetics, beverages, and food products. Furthermore, the second valuable material obtained in step [7] may be used as fuel for combustion in step [1].

[0072] Furthermore, if the gas generation unit (e.g., gasification furnace 10) becomes inoperable due to some influence, it will be difficult to continuously supply the raw material gas to the valuable material generation unit (e.g., culture tank 2), which may cause the microorganisms to die. In this case, it is advisable to incompletely combust the second valuable material (e.g., methanol) to provide a source of carbon monoxide for the microorganisms. The source of hydrogen for the microorganisms may be, for example, hydrogen separated in the second PSA device 52, or hydrogen prepared separately. As described above, by increasing the recycling efficiency of the second valuable material itself, carbon dioxide can be utilized more effectively.

[0073] If heating is required for the reaction in step [7] above, this reaction may be carried out using the heat generated during the combustion in step [1] above. In this case, the heat generated by combustion can be effectively utilized without being wasted. For example, gas lines GL2 and GL3 can be placed close to gas line GL1 near the outlet of the gasifier 10, and heat exchange can be performed between the high-temperature raw material gas discharged from the gasifier 10 and the gas flowing through gas lines GL2 and GL3. In this case, the reaction in step [7] is appropriately set according to the type of catalyst, but is preferably carried out at a temperature of 50°C or higher, more preferably at a temperature of 70°C or higher, and even more preferably at a temperature of 90°C to 150°C. This makes it easier to increase the yield of the second valuable product.

[0074] Furthermore, if the amount of hydrogen separated by the second PSA device 52 becomes excessive, this hydrogen may be stored, for example. Also, if the amount of hydrogen separated by the second PSA device 52 becomes excessive, while the amount of hydrogen introduced into the culture tank 2 is insufficient, the separated hydrogen may be introduced into the culture tank 2. Similarly, the carbon dioxide separated in the first PSA device 51 may be stored, or, if necessary, introduced into the culture tank 2.

[0075] Furthermore, the manufacturing system 100 described above may generate predictive information based on the composition of the raw material gas produced in the gasifier 10 and a pre-set trained model. The predictive information is information regarding the amount of the first valuable substance produced. Here, the trained model is a model that has been trained to output predictive information based on the composition of the raw material gas produced in the gasifier 10. The trained model may be constructed using learning methods such as supervised learning, unsupervised learning, or self-supervised learning. Furthermore, the trained model may include general-purpose natural language processing models, such as Large Language Models (LLMs), which have been trained on a vast amount of data, as an artificial intelligence.

[0076] The functions of the manufacturing system 100 described above are performed by the computer and processor provided within the manufacturing system 100. Furthermore, the manufacturing system 100 may be connected to an external computer via the Internet. In this case, the manufacturing system 100 may send data to the external computer to generate a trained model or output predictive information from the trained model. Furthermore, they may be provided in the following embodiments.

[0077] (1) A method for producing a valuable substance, comprising: a first step of removing at least one of solid impurities and water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide and impurities; a second step of removing gaseous impurities from the raw material gas after the first step; a third step of separating and recovering a carbon monoxide-containing gas containing carbon monoxide from the raw material gas after the second step; and a fourth step of producing the valuable substance from the carbon monoxide-containing gas.

[0078] (2) A method for producing a valuable substance as described in (1) above, further comprising a step of generating the raw material gas by burning a gasification raw material containing organic matter prior to the first step.

[0079] (3) A method for producing a valuable substance as described in (1) or (2) above, wherein in the second step, the removal of the gaseous impurity is performed using a PSA apparatus.

[0080] (4) A method for producing a valuable substance according to any one of (1) to (3) above, wherein in the third step, the separation of the carbon monoxide-containing gas is performed using a PSA apparatus.

[0081] (5) A method for producing a valuable substance according to any one of (1) to (4) above, wherein the concentration of hydrogen contained in the carbon monoxide-containing gas is 20% by mass or less.

[0082] (6) A method for producing a valuable substance according to any one of (1) to (5) above, wherein in the fourth step, the production of the valuable substance is carried out using microorganisms.

[0083] (7) A method for producing a valuable substance according to any one of (1) to (6) above, further comprising the step of reacting at least the hydrogen separated from the raw material gas and the carbon dioxide using a catalyst after the third step to produce a second valuable substance.

[0084] (8) A method for producing a valuable substance as described in (7) above, wherein the second valuable substance comprises at least one selected from the group consisting of carbon monoxide, amino acids, alkanes, alkenes, alcohols, ketones, and carboxylic acids.

[0085] (9) A valuable material manufacturing apparatus comprising: a first impurity removal unit that removes at least one of solid impurities and water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide and impurities; a second impurity removal unit that removes gaseous impurities from the raw material gas after it has passed through the first impurity removal unit; a recovery unit that separates and recovers a carbon monoxide-containing gas containing carbon monoxide from the raw material gas after it has passed through the second impurity removal unit; and a valuable material production unit that generates the valuable material from the carbon monoxide-containing gas.

[0086] (10) A valuable material manufacturing system comprising a gas generation unit that generates a raw material gas containing hydrogen, carbon monoxide, carbon dioxide and impurities, and a valuable material manufacturing apparatus as described in (9) above. Of course, this is not always the case.

[0087] As previously described, various embodiments of the present invention have been explained, but these are merely examples and do not limit the scope of the invention in any way. These novel embodiments can be implemented in various other forms, and various omissions, substitutions, and modifications can be made without departing from the spirit of the invention. These embodiments and their variations are included in the scope and spirit of the invention, as well as in the claims of the invention and its equivalents.

[0088] For example, the manufacturing system and the manufacturing apparatus for valuable materials may each have other optional additional configurations compared to the above embodiment, may be replaced with any configuration that performs a similar function, and some configurations may be omitted. Furthermore, in the above embodiment, carbon dioxide and hydrogen were separated from the raw material gas using different devices, but carbon dioxide and hydrogen may be separated from the raw material gas using the same device. [Explanation of Symbols]

[0089] 100: Manufacturing systems for valuable goods 10: Gasifier 1: Equipment for manufacturing valuable materials 2:Culture tank 5: Pre-processing section 51: First PSA device 52: Second PSA device 54: Dust removal equipment 6: Purification equipment 7: Synthesis section 8:Removal part GL1: Gas line GL2: Gas line GL3: Gas line LL: Liquid line

Claims

1. A method for manufacturing valuable materials, A first step of removing at least one of the solid impurities and the water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide, and impurities, A second step of removing the gaseous impurities from the raw material gas after the first step, A third step involves separating and recovering the carbon monoxide-containing gas, including the carbon monoxide, from the raw material gas after the second step, A method for producing a valuable substance, comprising a fourth step of producing the valuable substance from the carbon monoxide-containing gas.

2. In the method for producing a valuable substance according to claim 1, Furthermore, a method for producing a valuable substance, comprising a step of generating the raw material gas by burning a gasification raw material containing organic matter prior to the first step.

3. In the method for producing a valuable substance according to claim 1, A method for producing a valuable substance, wherein in the second step, the removal of the gaseous impurities is performed using a PSA apparatus.

4. In the method for producing a valuable substance according to claim 1, A method for producing valuable materials, wherein in the third step, the separation of the carbon monoxide-containing gas is performed using a PSA apparatus.

5. In the method for producing a valuable substance according to claim 1, A method for producing a valuable substance, wherein the concentration of hydrogen contained in the carbon monoxide-containing gas is 20% by mass or less.

6. In the method for producing a valuable substance according to claim 1, A method for producing a valuable substance, wherein in the fourth step, the production of the valuable substance is carried out using microorganisms.

7. In the method for producing a valuable substance according to claim 1, A method for producing a valuable substance, further comprising the step of reacting at least the hydrogen and carbon dioxide separated from the raw material gas using a catalyst after the third step to produce a second valuable substance.

8. In the method for producing a valuable substance according to claim 7, A method for producing a valuable substance, wherein the second valuable substance comprises at least one selected from the group consisting of carbon monoxide, amino acids, alkanes, alkenes, alcohols, ketones, and carboxylic acids.

9. A manufacturing apparatus for valuable materials, A first impurity removal unit removes at least one of the solid impurities and the water-soluble impurities from a raw material gas containing hydrogen, carbon monoxide, carbon dioxide, and impurities. A second impurity removal unit removes the gaseous impurities from the raw material gas after it has passed through the first impurity removal unit, A recovery unit separates and recovers the carbon monoxide-containing gas, including the carbon monoxide, from the raw material gas after it has passed through the second impurity removal unit, A valuable material manufacturing apparatus comprising a valuable material production unit that produces the valuable material from the carbon monoxide-containing gas.

10. A manufacturing system for valuable goods, A gas generation unit that generates a raw material gas containing hydrogen, carbon monoxide, carbon dioxide, and impurities, A system for manufacturing valuable materials, comprising the manufacturing apparatus for valuable materials described in claim 9.

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