Method for manufacturing regenerating adsorbents

Abstract

The present invention provides a method for producing a regenerated adsorbent that efficiently adsorbs impurities while effectively regenerating the adsorbent. [Solution] A method for manufacturing a regenerated adsorbent is provided, comprising: a preparation step of preparing a first gas containing exhaust gas, a second gas containing an inert gas, and an adsorbent filled in the container bodies of pressure swing adsorption type reaction vessels 40a and 40b having a gas inlet and outlet; an adsorption step of allowing the first gas to pass through the container body while pressurizing the inside of the container body to adsorb impurities in the first gas onto the adsorbent, thereby obtaining a third gas and a post-adsorption adsorbent; and a regeneration step of allowing the second gas to pass through the container body while depressurizing the inside of the container body to transfer impurities adsorbed on the post-adsorption adsorbent into the second gas, thereby obtaining a fourth gas and a regenerated adsorbent, wherein the temperature of the second gas in the regeneration step is higher than the temperature of the first gas in the adsorption step.

Description

[Technical Field]

[0001] This disclosure relates to a method for producing a regenerative adsorbent. [Background technology]

[0002] Conventionally, PSA (Polyseptic Tank Aqueduct) equipment has been used to remove impurities from mixed gases (see, for example, Patent Document 1). [Prior art documents] [Patent Documents]

[0003] [Patent Document 1] International Publication No. 2022 / 270439 [Overview of the project] [Problems that the invention aims to solve]

[0004] While efforts have been made to improve the efficiency of impurity removal in PSA devices, the regeneration efficiency of adsorbents has not been adequately studied.

[0005] In view of the above circumstances, this disclosure provides a method for producing a regenerated adsorbent that efficiently adsorbs impurities while effectively regenerating the adsorbent. [Means for solving the problem]

[0006] According to one aspect of the present invention, a method for producing a regenerated adsorbent is provided, comprising: a preparation step of preparing a first gas containing exhaust gas, a second gas containing an inert gas, and an adsorbent filled in the container body of a pressure swing adsorption type reaction vessel having a gas inlet and outlet; an adsorption step of allowing the first gas to pass through the container body while pressurizing the inside of the container body to adsorb impurities in the first gas onto the adsorbent, thereby obtaining a third gas and a post-adsorption adsorbent; and a regeneration step of allowing the second gas to pass through the container body while depressurizing the inside of the container body to transfer impurities adsorbed on the post-adsorption adsorbent into the second gas, thereby obtaining a fourth gas and a regenerated adsorbent, wherein the temperature of the second gas in the regeneration step is higher than the temperature of the first gas in the adsorption step.

[0007] According to this embodiment, it is possible to provide a method for producing a regenerated adsorbent that efficiently adsorbs impurities while effectively regenerating the adsorbent. [Brief explanation of the drawing]

[0008] [Figure 1] This is a schematic diagram showing the configuration of an organic substance manufacturing system. [Figure 2] This is a diagram illustrating the configuration of the separation device. [Figure 3] This figure shows an example of the shape of an adsorbent used in a separation device (Figures 3(A) to 3(B)). [Figure 4] This is a schematic diagram showing the external appearance of the separation device. [Figure 5] Figure 5(A) shows the internal structure of the container body during the adsorption of impurities, and Figure 5(B) shows the structure during the regeneration of the adsorbent. [Figure 6] Figure 6(A) shows an example of a flow straightening plate, and Figure 6(B) shows an example of a flow path modification mechanism. [Figure 7] This diagram shows the hardware configuration of the control mechanism 6. [Figure 8] This is a block diagram showing the functions realized by the processor and other components in an information processing device. [Figure 9]This is a graph showing how the adsorbent is regenerated. Mode for Carrying Out the Invention

[0009] Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings.

[0010] Incidentally, the program for implementing software appearing in one embodiment may be provided as a non-transitory computer-readable medium, may be provided so as to be downloadable from an external server, or may be provided such that the program is executed by an external computer to implement its functions in a client terminal (so-called cloud computing).

[0011] Furthermore, in various types of information processing according to one embodiment, an input and an output corresponding to the input can be implemented. Here, as long as an output can be obtained as a result of the input, the form of information referred to in such information processing (hereinafter referred to as reference information) is not limited. The reference information may be, for example, rule-based information such as a database, a lookup table, or a predetermined function (including determination expressions such as regression expressions constructed by statistical methods), may be a trained model in which the correlation between inputs and outputs is learned in advance, or may be generative AI such as a large language model or a visual language model that can output desired results by inputting a prompt.

[0012] Furthermore, in one embodiment, the term "unit" may include, for example, a combination of hardware resources implemented by circuits in a broad sense and software information processing that can be specifically realized by these hardware resources. Additionally, although various types of information are handled in one embodiment, these pieces of information are represented, for example, by physical values of signal values representing voltage and current, the level of a signal value as a binary bit aggregate composed of 0 or 1, or quantum superposition (so-called quantum bits), and communication and calculation can be performed on circuits in a broad sense.

[0013] Furthermore, a circuit in a broad sense is a circuit realized by combining at least a suitable combination of circuits, circuits, processors, and memory. The processor may be a general-purpose processor or a dedicated circuit. In other words, it includes application-specific integrated circuits (ASICs), programmable logic devices (for example, simple programmable logic devices (SPLDs), complex programmable logic devices (CPLDs), and field programmable gate arrays (FPGAs)), etc.

[0014] [Organic Substance Manufacturing System] First, an organic substance production system according to one embodiment will be described. Figure 1 is a schematic diagram showing the configuration of the organic substance production system. As will be explained in detail below, the organic substance production system is a system that can mainly produce organic substances from exhaust gas.

[0015] <Gasifier> The organic substance manufacturing system 100 shown in Figure 1 (hereinafter also simply referred to as "manufacturing system 100") comprises a gasifier (gas generation unit) 10 and an organic substance manufacturing apparatus 1 (hereinafter also simply referred to as "manufacturing apparatus 1") connected to the gasifier 10. In this specification, the upstream side with respect to the flow direction of gases and liquids will also be simply referred to as the "upstream side," and the downstream side will also be simply referred to as the "downstream side." In this embodiment, the gasifier 10 is not particularly limited, but examples include fluidized bed furnaces, kiln furnaces, shaft furnaces, etc. The gas generation unit may be a COx emission source of at least one business establishment selected from combustion furnaces (incinerators), paper mills, cement plants, thermal power plants, oil refineries, ethylene crackers, oil refineries, chemical plants, blast furnaces, converters, or electric furnaces in steel mills, in addition to the gasifier 10.

[0016] In each furnace, exhaust gas (raw material gas) containing carbon monoxide and carbon dioxide is generated during the combustion, melting, and refining of the contents. In the case of combustion furnaces or gasification furnaces at waste incineration plants, examples of contents (waste) include plastic waste, food waste, municipal waste (MSW), industrial waste, discarded tires, biomass waste, household waste (futons, paper products), building materials, etc. These wastes may consist of one type alone or two or more types. Furthermore, in the case of blast furnaces, converters, or electric arc furnaces in steel mills, exhaust gas is generated when, for example, iron ore is heated together with coke, limestone, etc. In the case of chemical plants, exhaust gas is generated when, for example, methane is steam reformed.

[0017] The carbon in exhaust gas derived from waste, etc., is different from the carbon in petroleum. 14 C, 13 The abundance of carbon isotopes such as ¹¹C (e.g., δ¹¹C) 14 C, δ 13 The C values ​​are different. Therefore, the abundance ratio of carbon isotopes contained in the organic substances produced by the manufacturing system 100 using exhaust gas as a raw material is also different from that of organic substances derived from petroleum. Consequently, even if the organic substances produced by the manufacturing system 100 are converted into other compounds and used, it is possible to determine (trace) that they originate from organic substances produced by the method described herein, which has a low environmental impact.

[0018] Exhaust gases typically contain carbon dioxide and carbon monoxide, as well as other gaseous components such as hydrogen, nitrogen, oxygen, water vapor, and methane. Exhaust gases may also contain other components such as soot, tar, nitrogen compounds, sulfur compounds, phosphorus compounds, and aromatic compounds. The exhaust gas may be produced as a gas containing 10% or more by volume by performing a heat treatment (commonly known as gasification) that causes incomplete combustion of the contents (carbon source) (i.e., by partially oxidizing the carbon source).

[0019] By using exhaust gas to produce valuable materials such as organic substances, carbon sources such as carbon dioxide that were previously emitted into the atmosphere can be effectively utilized, thereby reducing the burden on the environment. From the perspective of the carbon cycle, it is preferable to use exhaust gas generated in combustion furnaces or smelters. The gasifier 10 may have an oxygen generator that produces the oxygen necessary for combustion. Examples of oxygen generators include cryogenic separation devices that can compress, cool, and liquefy air from the atmosphere to extract liquid oxygen, liquid nitrogen, etc. The heat absorbed when the obtained liquid nitrogen vaporizes can be used, in particular, to cool the exhaust gas in the separation device 4 (described later). Furthermore, the nitrogen gas obtained when the liquid nitrogen vaporizes can be suitably used as a purge gas for various parts of the manufacturing system 100.

[0020] Furthermore, the gasifier 10 may have a reforming area inside or outside it for reforming the exhaust gas. The reforming area converts gases such as methane and ethane, as well as hydrocarbons such as char, tar, and dioxins contained in the exhaust gas, into carbon monoxide and hydrogen by, for example, holding the exhaust 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.

[0021] In the reforming area, a method may be employed in which hydrocarbons such as methane contained in the exhaust 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 nickel catalysts, nickel oxide catalysts, ruthenium catalysts, rhodium catalysts, palladium catalysts, and platinum catalysts. Here, the stable isotope ratio of carbon δ 13 C has δ under high-temperature combustion conditions. 13 The value of C tends to be high, and in incomplete combustion, δ 13 It is known that the C value tends to be low. Therefore, by providing a reforming area, the exhaust gas will have its own unique δ according to the combustion conditions. 13 It may have a C value. Therefore, even if the organic substance produced by the manufacturing system 100 is converted to another compound and used, it can be identified (trace) that it originates from the organic substance produced by the method of this disclosure, which has a low environmental impact.

[0022] The synthesis gas (hereinafter also referred to as "exhaust gas") produced by the gasifier 10 is at a high temperature. The heat from this high-temperature exhaust gas may be used to generate steam from water. For example, a tank storing water may be installed in the middle of the gas line GL1 connected downstream of the gasifier 10, and steam may be generated by heat exchange between the exhaust gas and the water. Alternatively, a heat recovery device more suitable for recovering high-temperature heat, such as an economizer, may be installed near the gasifier 10 and near the gas line GL1, and steam may be generated by heat exchange with the exhaust gas using the heat recovery device. In this way, by efficiently recovering and utilizing the heat from the exhaust gas without waste, the environmental burden during the production of organic substances can be further reduced. It should be noted that the heat from the exhaust gas is not limited to these uses and can be utilized for various purposes. A manufacturing apparatus 1 is connected to the gasification furnace 10. This manufacturing apparatus 1 has a production unit (organic substance production unit) 2, and the gasification furnace 10 and the production unit 2 are connected by a gas line GL1.

[0023] The generation unit 2 generates a valuable substance mainly containing an organic substance (hereinafter, also simply referred to as "organic substance") from supplied exhaust gas (raw material gas). Specifically, an organic substance (carbon-based valuable substance) can be generated by causing molecules in the exhaust gas to act on a catalyst or the like. Examples of the organic substance include alcohols such as methanol and ethanol, organic acids such as acetic acid and formic acid, and SAF (Sustainable Aviation Fuel). For example, an organic substance is generated by adding hydrogen to carbon monoxide in the exhaust gas using a catalyst. Examples of the catalyst used herein include lithium (Li), sodium (Na), manganese (Mn), rhenium (Re), ruthenium (Ru), cobalt (Co), rhodium (Rh), nickel (Ni), palladium (Pd), and alloys obtained by combining elements belonging to different groups of the periodic table among the above. The catalyst is preferably a metal catalyst, but is not particularly limited. Since the organic substance generated in the generation unit 2 is generated using carbon derived from exhaust gas, it is different from organic substances derived from petroleum in 14 C, 13 the abundance ratio of carbon isotopes such as C (e.g., δ 14 C, δ 13 C values). Therefore, even when this organic substance is converted into a product such as another compound and used, it can be determined (traced) that it is derived from the organic substance generated by the method according to the present disclosure with low environmental load. Further, the valuable substance is not limited to organic substances, and may contain, for example, ammonia. When the valuable substance contains ammonia, in the generation unit 2, ammonia can be generated by, for example, causing nitrogen and hydrogen in the exhaust gas to act on a catalyst containing iron (Fe), ruthenium (Ru), or the like.

[0024] <Generation Unit> The production unit 2 may, in addition to or in addition to the reaction using a non-biocatalyst, produce the above-mentioned organic substances from molecules in the exhaust gas by the action of a biocatalyst such as gas-assimilating bacteria. Examples of gas-assimilating bacteria that can be used include Butyribacterium methylotrophicum, Clostridium autoethanogenum, Clostridium carboxidivorans, Clostridium ljungdahlii, Clostridium ragsdalei, Moorella, and Carboxydothermus. When microorganisms such as gas-utilizing bacteria are used as biocatalysts, the product contains 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 generated organic substance is converted into other compounds and used, it can be more easily identified (traceable) that it originated from the organic substance produced by the method of this disclosure, which has a low environmental impact.

[0025] Furthermore, multiple types of compounds may be produced by reacting multiple types of molecules in the exhaust gas with the catalyst. The raw materials such as hydrogen supplied to the production unit 2 may be contained in the exhaust gas, or they may be supplied separately from a hydrogen supply source (gas tank).

[0026] <Pre-processing> A pre-processing unit 5 is provided in the middle of the gas line GL1. The pre-processing unit 5 is provided to perform a process to remove impurities from the exhaust gas. The pre-processing unit 5 includes a filter device 3 and a separation device 4, which are provided in order from the gasification furnace 10 side (upstream side).

[0027] The filter device 3 is used to remove tar, soot, and fine particles smaller than the size of soot. This filter can be made up of, for example, a bag filter. The separation device 4 is a pressure swing adsorption (PSA) type device that removes (separates) impurities from the exhaust gas (first gas). Because the separation device 4 is a PSA type device, unlike other methods such as temperature swing adsorption (TSA), physical-temperature swing adsorption (PTSA), and chemical absorption, it does not require a large amount of heat or absorbent liquid, and therefore can remove impurities with relatively little energy.

[0028] In addition to the filter device 3 and separation device 4, the pre-processing unit 5 may also include, for example, a scrubber, a dehydration device (dehumidifier), a filter, an oxygenation device, an acetylene removal device, a dehydrogenation device, a TSA device, a PTSA device, a reduction device, an impurity removal device, etc. These can be used individually or in any combination.

[0029] Scrubbers can be used, for example, to remove pollutants (e.g., soot) and water-soluble substances contained in exhaust gas. In a scrubber, cleaning is performed by bringing a cleaning solution into contact with the object to be cleaned (wet cleaning method). An example of a wet cleaning 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.

[0030] A dewatering device (dehumidifier) ​​can be used, for example, to dewater exhaust gas whose water content has increased due to cleaning by a scrubber. This dewatering device (dehumidifier) ​​may be, for example, a cooling device that removes moisture by condensing the exhaust gas by cooling it, a device that removes moisture by passing the exhaust gas through a membrane separation device such as a membrane dryer, or a mist separator. Alternatively, it may be a device that adsorbs and removes moisture using adsorbents, moisture adsorbents such as alumina (Al2O3) and silica gel, moisture absorbents such as calcium chloride, or moisture absorbent liquids such as monoethylene glycol and diethylene glycol.

[0031] Filters are used to remove fine particles smaller than the size of soot. These filters can be, for example, bag filters. Deoxygenation devices can be 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.

[0032] A dehydrogenation apparatus is used to remove hydrogen and can consist of, for example, a separator containing a cylindrical separation membrane that selectively permeates and separates hydrogen. Examples of materials that make up such a separation membrane include metal materials, ceramic materials, and resin materials. 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 (Al2O3), and composite materials containing one or more of these (e.g., alumina-carbon materials). Examples of resin materials include polyamide, polyimide, and polysulfone.

[0033] A TSA device is a temperature swing adsorption type separator, while a PTSA device is a pressure and temperature swing adsorption type separator. These can be used, for example, to remove aromatic compounds, hydrogen cyanide, and the like.

[0034] The oxygen removed by the deoxygenation device may be configured to be supplied to the gasifier 10 in order to increase the heating temperature in the gasifier 10. This reduces the effort required to transport oxygen from another location to supply to the gasifier 10, and further reduces the environmental impact during the production of organic substances.

[0035] The reduction device can be configured to produce carbon monoxide from carbon dioxide using hydrogen, for example, through a reverse water-gas shift reaction or a chemical loop reaction mediated by a catalyst. The reduction device is, for example, a reaction apparatus filled with a catalyst. If the pre-treatment unit 5 has a dehydrogenation device, the reduction device is preferably configured to produce carbon monoxide from carbon dioxide using the hydrogen removed by the dehydrogenation device. This allows for the production of organic substances with a lower environmental impact compared to transporting hydrogen from another location. Furthermore, the hydrogen may be obtained by electrolysis of water using green electricity generated from natural energy sources such as wind, hydro, solar, and geothermal energy. This further reduces the environmental impact during the production of organic substances. When producing carbon monoxide from carbon dioxide in exhaust gas, the oxygen concentration inside the reduction device (i.e., under the reduction reaction environment) is preferably 1 volume percent or less. This prevents or suppresses the inhibition of the reduction reaction by oxygen. By incorporating a reduction device, the amount of carbon monoxide converted into organic substances can be increased, thereby improving the yield of organic substances.

[0036] The configuration of the reduction device is not limited to the above configuration, and for example, it may be configured to reduce carbon dioxide to carbon monoxide using a reducing agent. The reducing agent is not particularly limited as long as it can extract oxygen elements from carbon dioxide and reduce carbon dioxide. It is preferable that such a reducing agent contains a compound that has oxygen ion conductivity (a so-called oxygen carrier). As this oxygen carrier, for example, a metal oxide containing at least one metal element selected from Group 3 to Group 12 can be used. In addition, in the reducing agent, the oxygen carrier may be supported on a carrier such as a carbon material (graphite, graphene, etc.), zeolite, montmorillonite, SiO2, ZrO2, TiO2, V2O5, MgO, alumina (Al2O3), silica, etc.

[0037] In this case, the reducing agent in the oxidized state after reducing carbon dioxide can be reduced using a reducing gas containing, for example, at least one selected from hydrogen, hydrocarbons (e.g., methane, ethane, acetylene, etc.), and ammonia, which were removed in the pretreatment section 5. In this case, it is preferable that the reduction apparatus has two or more reactors filled with the reducing agent. This allows the carbon dioxide reduction reaction to be carried out by passing the exhaust gas through one reactor while the reduction reaction of the oxidized reducing agent is carried out by passing the reducing gas through the other reactor. As a result, an activated reducing agent is available in one of the reactors, and by passing the exhaust gas through while switching between reactors, the carbon dioxide reduction reaction can be carried out continuously by chemical looping. Furthermore, the reduction device can also be configured to reduce carbon dioxide to carbon monoxide through a reduction reaction of carbon dioxide using electrical energy.

[0038] The impurity removal device can remove impurities such as sulfur or sulfur compounds, chlorine or chlorine compounds, and cyanide compounds. An impurity removal device can be, for example, a reactor filled with a desulfurizing agent.

[0039] <Purification equipment> Furthermore, the generation unit 2 is connected to a purification device (organic substance purification unit) 6 via a liquid line LL. The purification device 7 is a device that purifies organic substances from an organic substance-containing liquid. Examples of such purification apparatus 7 include distillation apparatuses, permeable vaporization membranes, zeolite dehydration membranes, organic membranes, low-boiling-point substances with a boiling point lower than that of organic substances, high-boiling-point substances with a boiling point higher than that of organic substances, and ion exchange membranes. These apparatuses may be used individually or in combination of two or more types.

[0040] When using a distillation apparatus, the temperature inside the distillation apparatus during the distillation of organic substances (e.g., ethanol) is not particularly limited, but is preferably 100°C or lower, and more preferably 70°C to 95°C. Setting the temperature to this level ensures more reliable separation of the required organic substances from other components, i.e., distillation (purification) of the organic substances. Furthermore, if the gasification furnace 10 has an oxygen generator and liquid nitrogen can be obtained, it is preferable to utilize the endothermic heat generated when the liquid nitrogen vaporizes when condensing the distilled organic substances. This shortens the time required to produce organic substances without consuming additional energy such as electricity. In addition, when storing the obtained high-concentration organic substances, it is preferable to fill the tanks or other containers storing the organic substances with nitrogen gas remaining after the liquid nitrogen has vaporized. This allows for effective utilization of the generated liquid nitrogen, prevents quality deterioration due to oxidation of the organic substances, and prevents fires caused by the influx of oxygen.

[0041] The pressure inside the distillation apparatus during the distillation of organic substances may be atmospheric pressure, but it is preferable to be below 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 organic substances and, consequently, the yield of organic substances. The concentration of organic substances 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.

[0042] Examples of organic substances obtained in this way include monools such as methanol and ethanol, diols such as 2,3-butanediol, organic acids such as acetic acid and lactic acid, isoprene, butadiene, ammonia, and SAF (Sustainable Aviation Fuel). Such organic substances can be used, for example, as raw materials 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.

[0043] [Details of the separation device] The separation device 4 of the preprocessing unit 5 will be described in more detail below with reference to Figures 2 to 8. <Overview of the separation device> As shown in Figure 2, the separation device 4 has, for example, two reaction vessels 40 (reaction vessel 40a and reaction vessel 40b) through which exhaust gas passes and from which impurities are adsorbed and removed. Figure 2 is a diagram showing an overview of the configuration of the separation device. Reaction vessels 40a and 40b are filled with porous materials such as activated carbon, zeolite, silica gel, molecular sieves, and metal-organic frameworks (MOFs) as adsorbents. By setting the type of adsorbent and the size of the pores, it is possible to select compounds that can be adsorbed and removed. In Figure 2, the adsorbents are indicated by shading.

[0044] Examples of impurities adsorbed and removed by the separation device 4 include water (H2O), carbon dioxide (CO2), hydrogen sulfide (H2S), nitrogen (N2), acetylene (C2H2), BTEX (benzene (C6H6), toluene (C6H5CH3), ethylbenzene (C6H5(CH2CH3)), xylene (C6H4(CH3)2), 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 an extreme decrease in catalyst reactivity or deactivation in the production section 2 downstream of the separation device 4.

[0045] When adsorbing and removing two or more compounds in the separation apparatus 4, multiple reaction vessels 40 (multiple sets of reaction vessels 40a and reaction vessel 40b) filled with adsorbents of different types and pore sizes may be used, or a single reaction vessel 40 (one set of reaction vessels 40a and reaction vessel 40b) filled with adsorbents of different types and pore sizes may be used. In this way, by removing impurities from the exhaust gas (first gas), the volume of exhaust gas (third gas) to be treated downstream can be reduced, thus enabling miniaturization of the generation unit 2 located downstream. Furthermore, it is possible to prevent impurities from adversely affecting the generation of organic substances in the generation unit 2.

[0046] As shown in Figure 2, when the pressure inside the reaction vessel 40a is increased and exhaust gas (first gas) is passed through the reaction vessel 40a as indicated by the solid black arrow, the exhaust gas (first gas) comes into contact with the adsorbent. As a result, impurities are adsorbed onto the adsorbent, and exhaust gas from which impurities have been removed (third gas) and post-adsorption adsorbent with adsorbed impurities are obtained. At this time, when the pressure inside the reaction vessel 40b is decreased and an inert gas (second gas), such as nitrogen (N2), hydrogen (H2), argon (Ar), or helium (He), is passed through as indicated by the solid white arrow, the impurities adsorbed on the adsorbent migrate into the inert gas (second gas). As a result, inert gas containing impurities (off gas, fourth gas) and regenerated adsorbent from which impurities have been released are obtained.

[0047] After a certain period of time, impurities are adsorbed onto most of the adsorption sites of the adsorbent in reaction vessel 40a, causing the adsorbent's capacity to adsorb impurities to saturate. At that point, as shown by the black dotted arrow in Figure 2, the exhaust gas is passed through reaction vessel 40b instead of reaction vessel 40a. As described above, impurities have already detached from the adsorbent in reaction vessel 40b. Therefore, the impurities in the exhaust gas are adsorbed onto the adsorbent in reaction vessel 40b. Simultaneously, by lowering the pressure in reaction vessel 40a and passing an inert gas through reaction vessel 40a as shown by the white dotted arrow in Figure 2, the impurities adsorbed onto the adsorbent can be detached and recovered.

[0048] The relationship between the direction in which the exhaust gas (first gas and third gas) and the inert gas (second gas and fourth gas) pass through the reaction vessel 40 is not particularly limited, but it is preferable that they pass in opposite directions as shown in Figure 2. According to the inventors' studies, the adsorbent on the exhaust gas inlet side (lower side in Figure 2) tends to adsorb many impurities. Therefore, by passing the inert gas in the opposite direction, the off-gas (fourth gas), which has a relatively high impurity concentration, after the lower adsorbent has been regenerated, can be quickly discharged from the outlet side (lower side in Figure 2). In other words, it is possible to prevent the off-gas, which has a relatively high impurity concentration, from coming into contact with the adsorbent on the exhaust gas outlet side (upper side), which has relatively less adsorption of impurities. Therefore, the removal of impurities adsorbed on the adsorbent by the inert gas can be performed more efficiently, and the amount of inert gas used can be reduced.

[0049] In Figure 2, the exhaust gas (first gas), indicated by the black arrow, is supplied to the reaction vessel 40 (reaction vessel 40a or reaction vessel 40b). Preferably, the temperature of the inert gas (second gas) supplied to the reaction vessel 40 when the adsorbent is regenerated is higher than the temperature of the exhaust gas (first gas) when impurities are adsorbed onto the adsorbent. This allows for smooth operation of both the exothermic phenomenon of adsorption of impurities and the endothermic phenomenon of detachment of impurities. In particular, by sufficiently raising the temperature of the inert gas when impurities are detached and the adsorbent is regenerated, the adsorbent can be sufficiently regenerated even when a small amount of inert gas is used. Therefore, inert gas can be saved, and thus the environmental burden during the production of organic substances can be further reduced.

[0050] In the past, when considering purification technologies such as exhaust gas purification, the focus has tended to be on the efficiency of adsorption, and the regeneration of adsorbents has not been adequately considered. On the other hand, as described in this disclosure, by raising the inert gas to a moderately high temperature during adsorbent regeneration, the adsorbent can be efficiently and sufficiently regenerated, as shown in Figure 9. Figure 9 is a graph showing the regeneration of the adsorbent. The vertical axis of the graph in Figure 9 shows the relative amount of hydrogen sulfide, with the amount of hydrogen sulfide (volume %) in the inlet exhaust gas (first gas) before impurities are removed set to 100%. Each plot in the graph in Figure 9 shows the value of the amount of hydrogen sulfide (volume %) in the outlet exhaust gas (third gas) when the exhaust gas (first gas) is supplied to the reaction vessel to attempt to remove impurities. At the left end of the graph, the amount of hydrogen sulfide in the outlet exhaust gas (third gas) was equal to the amount of hydrogen sulfide in the inlet exhaust gas (first gas). This indicates that the adsorbent has reached the end of its lifespan and needs to be replaced. Previously, to reach this point, both exhaust gas (first gas) and nitrogen gas (second gas), which acted as an inert gas, were passed through the reaction vessel at intervals of 10 to 20 minutes, while maintaining a temperature of approximately 20°C or lower.

[0051] From the state at the left end of the graph, it was found that when the gas supply to the reaction vessel was carried out in the same manner as described above, except that the temperature of the exhaust gas (first gas) was set to approximately 70°C to 90°C and the temperature of the inert gas (second gas) was set to approximately 20°C to 90°C, the amount of hydrogen sulfide in the exhaust gas (third gas) at the outlet side was greatly reduced, as shown in Figure 9, and the adsorbent was regenerated. In other words, by not lowering the temperature of the exhaust gas (first gas) too much, the activity of the adsorbent that had been lost can be regenerated. On the other hand, without reducing the adsorption capacity of the adsorbent to the state shown on the far left of Figure 9, as long as the adsorption capacity of the adsorbent is maintained, the temperature of the inert gas (second gas) can be made higher than the temperature of the exhaust gas (first gas). This allows for efficient adsorption of impurities onto the adsorbent and regeneration of the adsorbent through the release of impurities. In other words, a balance between adsorption and regeneration can be maintained, making it possible to preserve the activity of the adsorbent over a long period of time. This allows the adsorbent to be used for a long period of time, reducing the environmental burden during the production of organic substances. Furthermore, there is no need to use large amounts of inert gas for the regeneration of the adsorbent. In addition, the burden of monitoring the degradation of the adsorbent (i.e., monitoring the degree of purification of the exhaust gas) and replacing degraded adsorbents can be reduced.

[0052] More specifically, the temperature difference between the exhaust gas (first gas) used for adsorbing impurities and the inert gas (second gas) used for regenerating the adsorbent is preferably 15°C or more, more preferably 20°C or more, and even more preferably 30°C or more. By setting such a sufficient temperature difference, both the adsorption of impurities and the regeneration of the adsorbent can be carried out efficiently. It is particularly preferable to ensure this temperature difference by sufficiently heating the inert gas (second gas). This allows the adsorbent to be used for a long period of time. Furthermore, as the degree of adsorption degradation progresses, it is preferable to increase the temperature difference between the exhaust gas used for adsorption of impurities (first gas) and the inert gas used for regenerating the adsorbent (second gas). By controlling it in this way, the environmental impact during the production of organic substances can be minimized. In other words, while the adsorbent is not degraded, the temperature difference is kept small to reduce energy consumption, and as the adsorbent degrades, the temperature difference is increased, allowing the adsorbent to be used for a longer period of time.

[0053] The separation device 4 is not limited to two reaction vessels 40; it may have one, but it is preferable to have two or more. This allows the adsorbent to be regenerated in another reaction vessel while the exhaust gas is being passed through one reaction vessel to adsorb impurities. As a result, a regenerated adsorbent from which impurities have been released is available in one of the reaction vessels, and by passing the exhaust gas through the reaction vessels while switching between them, impurities can be continuously adsorbed and removed from the exhaust gas.

[0054] The PSA reaction vessel 40 can be filled with granular (for example, spherical or cylindrical) adsorbent. Figure 3 shows an example of the shape of the adsorbent used in the separation device (Figures 3(A) to 3(B)). Among the granular adsorbents, an adsorbent with a cross-section like three columnar particles arranged side by side (i.e., a clover-shaped cross-section), as shown in Figure 3(A), is preferred. In this case, there are many gaps through which the exhaust gas can pass, so it is possible to prevent or suppress an unnecessary increase in the packing density of the adsorbent. Therefore, the exhaust gas can pass smoothly through the reaction vessel 40, and pressure loss can be easily reduced. Alternatively, instead of filling the reaction vessel 40 with granular adsorbent, the adsorbent may be molded into a molded body having a number of partitioned small spaces 53, as shown in Figure 3(B), and then filled into the vessel. The number of small spaces 53 should be formed to partition the internal space of the reaction vessel 40 in a direction perpendicular to the direction in which the exhaust gas passes through the reaction vessel 40. In other words, the shape of the partition wall 52 that partitions each small space 53 of the molded body should be an elongated cylindrical shape along the direction in which the exhaust gas passes. With this configuration, turbulence of the exhaust gas streamline passing through each small space 53 can be more effectively prevented, and thus pressure loss can be further reduced.

[0055] Reducing the pressure loss of exhaust gas allows the exhaust gas to flow at a relatively low pressure, enabling the production of organic substances with less energy consumption. Furthermore, because the exhaust gas flows at a low velocity, sufficient contact opportunities between the exhaust gas and the adsorbent are easily ensured. This means that impurities are more readily adsorbed by the adsorbent, improving the efficiency of exhaust gas purification.

[0056] When enlarging the reaction vessel 40, it is necessary to design it to withstand the pressure changes (increasing and decreasing pressure) of the PSA method, which limits the radial enlargement. Therefore, when enlarging the reaction vessel 40, it is manufactured to have an elongated shape. Consequently, in order to allow the exhaust gas to pass smoothly through the reaction vessel 40, it is necessary to supply the exhaust gas at a certain high pressure and high flow rate. In this case, when a large number of small spaces 53 are formed, the exhaust gas can be preferentially passed through the small spaces 53 compared to when granular adsorbent is filled. Therefore, it is less likely that high-velocity exhaust gas will pass through the spaces between the particles, preventing the adsorbent from adsorbing impurities. Furthermore, as mentioned above, when numerous small spaces 53 are formed, the pressure loss is less compared to when granular adsorbent is filled, allowing the exhaust gas to pass through at a relatively low pressure and low flow rate. Therefore, in this case, even if the reaction vessel 40 is enlarged, the exhaust gas can still pass through at a relatively low pressure and low flow rate.

[0057] Furthermore, the cross-sectional shape of the partition wall 52 along the orthogonal direction may be circular or elliptical as shown in Figure 3(C), or it may be a polygonal shape such as a square, rectangle, parallelogram, trapezoid, triangle, or hexagon as shown in Figure 3(B). In particular, when this cross-sectional shape is polygonal, it is easier to arrange multiple small spaces 53 closely together, which makes it easier to increase the contact area between the exhaust gas and the adsorbent. The cross-sectional shape of the partition wall 52 along the perpendicular direction is particularly preferably hexagonal. In this case, the cross-sectional shape can be described as honeycomb-shaped. With this configuration, multiple small spaces 53 can be arranged regularly and densely, thereby further improving the adsorption efficiency of impurities. In addition, because the corners of the partition wall 52 are obtuse, sufficient space can be secured even at the corner portions. As a result, the exhaust gas is less likely to be compressed, and the pressure loss can be significantly reduced. Consequently, the exhaust gas can be flowed at a lower pressure and lower flow rate, and an increase in the effects described above can be expected.

[0058] The impurities separated by the separation device 4 are preferably reused in various parts of the manufacturing device 1. For example, if the impurities are nitrogen, they may be used to clean various parts of the system, such as the separation device 4, the piping of the gas analysis equipment, and the equipment in the gasification furnace process; they may be used to seal the generated organic material to prevent oxidation; or they may be filled into cylinders and shipped. By reusing the impurities in this way, the environmental burden on the manufacturing device 1 when producing organic material can be further reduced.

[0059] <Configuration of the separation device> The configuration of the separation apparatus 4 will be described in more detail with reference to Figure 4, etc. Figure 4 is a schematic diagram showing the external appearance of the separation apparatus. As shown in Figure 4, in addition to the reaction vessel 40, the separation apparatus 4 further includes a cooling mechanism 42, an inert gas supply unit 43, a heating mechanism 44, and a control mechanism 6. The separation apparatus 4 also includes gas lines GL41, GL42, GL43, and GL44.

[0060] (Gas line) Gas line GL41 connects gas line GL1, which extends from the filter device 3, to the lower port 407 of the reaction vessel 40. Along gas line GL41, from the upstream side, are a cooling mechanism 42, an air supply pump P1, and a valve V1. Gas line GL42 connects gas line GL1 to the upper port 408 of the reaction vessel 40. Along gas line GL42 is a valve V2. With this configuration, exhaust gas (first gas and third gas) can be passed from the filter device 3 to the generation unit 2 via the reaction vessel 40. When supplying exhaust gas to the reaction vessel 40, the lower port 407 functions as the gas inlet and the upper port 408 functions as the gas outlet.

[0061] Gas line GL43 connects the inert gas supply unit 43 to the upper port 408 of the reaction vessel 40. A heating mechanism 44 and a valve V3 are provided along gas line GL43, starting from the upstream side. Gas line GL44 extends downstream from the lower port 407 of the reaction vessel 40. A valve V4 and a depressurizing pump P2 are provided along gas line GL44, starting from the upstream side. This configuration allows the inert gas (second gas) to pass through the reaction vessel 40. When supplying the inert gas to the reaction vessel 40, the upper port 408 functions as the gas inlet and the lower port 407 functions as the gas outlet.

[0062] The cooling mechanism 42 cools the exhaust gas (first gas) from the filter device 3 to the separation device 4 via gas lines GL1 and GL41. The configuration of the cooling mechanism 42 is not particularly limited as long as it can cool the exhaust gas, but examples include showering the outside of gas line GL41 with a fluid such as water or air, or blowing it with a blower, flowing fluid through an annular member such as a pipe or hose wrapped around gas line GL41, or filling a box-shaped member through which gas line GL41 passes with fluid. When the cooling mechanism 42 cools the exhaust gas, it is preferable to use a heat exchanger such as a heat pump. This allows the heat generated during cooling to be used in parts of the manufacturing system 100 that require heat, such as the heating mechanism 44, further reducing the environmental burden during the production of organic substances.

[0063] The cooling mechanism 42 preferably cools the temperature of the exhaust gas (first gas) to approximately -5°C to 40°C, more preferably to approximately 0°C to 35°C, and even more preferably to approximately 5°C to 30°C. By sufficiently cooling the exhaust gas in this way, the adsorption and removal of impurities in the reaction vessel 40 is carried out smoothly, and the purification efficiency of the exhaust gas (first gas and second gas) is improved. Furthermore, by not overcooling the exhaust gas, the energy consumption related to cooling can be reduced, thereby reducing the environmental burden during the production of organic substances. In addition, since it is possible to prevent overcooling of the reaction vessel 40, it is possible to avoid a decrease in the regeneration efficiency of the adsorbent when an inert gas is supplied to the reaction vessel 40.

[0064] When valves V1 and V2 are open, cooled exhaust gas (first gas) is supplied into the reaction vessel 40 via the lower port 407. At this time, valves V3 and V4 are closed. The gas pump P1 supplies the exhaust gas while pressurizing the reaction vessel 40. This allows the exhaust gas to come into contact with the adsorbent packed in the reaction vessel 40, and impurities are adsorbed and removed. The exhaust gas from which impurities have been removed (third gas) passes sequentially through gas lines GL42 and GL1 via the upper port 408 and is supplied to the generation unit 2.

[0065] The inert gas supply unit 43 supplies inert gas. The heating mechanism 44 heats the inert gas from the inert gas supply unit 43 to the reaction vessel 40 via the gas line GL43. The configuration of the inert gas supply unit 43 is not particularly limited as long as it can heat the inert gas, but examples include a configuration in which a high-temperature fluid such as hot water or high-temperature air is showered or blown onto the outside of the gas line GL43 by a shower or blower, a configuration in which a high-temperature fluid is flowed through an annular member wrapped around the gas line GL43, or a configuration in which a box-shaped member through which the gas line GL43 passes is filled with a high-temperature fluid. When the heating mechanism 44 heats the inert gas, it is preferable to use a heat exchanger such as a heat pump. This allows the cold air generated during heating to be used in parts of the manufacturing system 100 that require cold air, such as the cooling mechanism 42, further reducing the environmental burden during the production of organic substances.

[0066] The heating mechanism 44 preferably heats the inert gas (second gas) to a temperature of approximately 30°C to 300°C, more preferably to 40°C to 200°C, and even more preferably to 50°C to 140°C. By sufficiently heating the inert gas in this way, impurity removal and the production of regenerated adsorbent can be smoothly carried out in the reaction vessel 40. In other words, the regeneration efficiency of the adsorbent is improved. Furthermore, by not overheating the inert gas, the energy consumption for heating can be reduced, thereby reducing the environmental burden during the production of organic substances. In addition, since it is possible to prevent overheating of the reaction vessel 40, a decrease in the purification efficiency of the exhaust gas when exhaust gas is supplied to the reaction vessel 40 can be avoided. In particular, by setting the heating temperature of the inert gas to approximately 300°C or lower, changes in the crystal structure of the adsorbent can be prevented or suppressed, and the adsorbent can be efficiently regenerated while aiming for long-term use.

[0067] When valves V3 and V4 are open, heated inert gas (second gas) is supplied into the reaction vessel 40 via the upper port 408. At this time, valves V1 and V2 are closed. A depressurizing pump P2 located on the lower port 407 (outlet) side reduces the pressure inside the reaction vessel 40, thereby introducing the inert gas into the reaction vessel 40. As a result, the inert gas comes into contact with the adsorbent packed inside the reaction vessel 40, causing impurities to migrate from the adsorbent to the inert gas, thus regenerating the adsorbent. The inert gas containing impurities (fourth gas) passes through the gas line GL44 via the lower port 407 and is recovered as off-gas.

[0068] (Reaction vessel) The reaction vessel 40 has a lower port 407, an upper port 408, a vessel body 401, and a monitoring auxiliary mechanism 402. As described above, the lower port 407 and the upper port 408 are inlets or outlets for exhaust gas and inert gas. The vessel body 401 is filled with an adsorbent, and impurities are adsorbed and the adsorbent is regenerated as the exhaust gas and inert gas pass through it. The monitoring auxiliary mechanism 402 is provided to monitor the degree of deterioration of the adsorbent filled in the vessel body 401.

[0069] • Container body The container body 401 will be described with further reference to Figure 5. Figure 5 shows the internal structure of the container body, specifically the state during impurity adsorption (Figure 5(A)) and the state during adsorption regeneration (Figure 5(B)). The black arrows in Figure 5(A) schematically indicate the direction of passage of the exhaust gas (first gas or third gas), and the white arrows in Figure 5(B) schematically indicate the direction of passage of the inert gas. As shown in Figures 5(A) and 5(B), the container body 401 includes at least one rectifier plate 404 and a flow path changing mechanism 405 provided on the inlet side (lower port 407 side and upper port 408 side) of the rectifier plate 404. The constituent materials forming the container body 401 can be appropriately selected depending on the type of adsorbent or impurities, the degree of pressurization, etc., but for example, stainless steel such as SUS316L, low-alloy carbon steel such as ASTM A516 Gr.70, and high-performance alloy steel such as Inconel 625 can be used as the main components.

[0070] It is preferable that the inner wall portion (inner surface) 406 surrounding the internal space of the container body 401 be coated. This prevents impurities such as soot in the exhaust gas (first gas) from directly adhering to the container body 401 itself, thereby reducing damage to the container body 401 (inner wall portion 406) and preventing interference from impurities accumulated in the passing gas. The coating materials are preferably highly corrosion-resistant substances such as ceramics like aluminum nitride (AlN), silicon nitride (Si3N4), beryllium oxide (BeO), silicon carbide (SiC), and aluminum oxide (Al2O3), resins like polytetrafluoroethylene (PTFE), polyimide (PI), polyphenylene sulfide (PPS), and polyetheretherketone (PEEK), or mixtures thereof. This prevents or suppresses damage to the container body 401 even if each gas or impurity contains corrosive substances such as hydrogen sulfide. As a result, the container body 401 can be used for a long period of time, further reducing the environmental burden during the production of organic substances.

[0071] The coating's constituent materials have a thermal expansion coefficient of 2.2 × 10⁻⁶ between 0°C and 100°C. -6 / ℃ or higher 22×10 -6 It is preferable that the temperature be around / ℃ or lower, 5.5 × 10 -6 / ℃ or higher 18×10 -6It is more preferable that the thermal expansion coefficient be around / °C or lower. By using a constituent material having such a thermal expansion coefficient as a coating, the thermal expansion coefficient of the coating tends to be similar to that of the constituent material of the container body 401. Therefore, even when cooled exhaust gas or heated inert gas passes through the container body 401, the difference in the degree of deformation due to heat can be kept small, and the peeling of the coating from the inner wall portion 406 of the container body 401 can be prevented or suppressed. In other words, the ratio of the thermal expansion coefficient of the coating applied to the inner wall portion 406 to the thermal expansion coefficient of the constituent material forming the container body 401 is preferably 0.1 or more and 2 or less, and more preferably 0.3 or more and 2 or less.

[0072] The container body 401 has a containment space 403 filled with an adsorbent (not shown). The amount of adsorbent to be filled into the containment space 403 (the adsorbent containment space within the container body) is 300 kg / m³. 3 More than 900kg / m 3 It is preferable that it be approximately 330 kg / m 3 More than 700kg / m 3 It is more preferable that the packing density is within the following range. By keeping the packing density from being too large, sufficient volume can be provided for the pores of the adsorbent and the spaces between the adsorbents, preventing or suppressing excessive obstruction of gas passage. Furthermore, a moderately large packing density allows for sufficient adsorption and removal of impurities in the exhaust gas by the adsorbent.

[0073] Furthermore, it is preferable that multiple containment spaces 403 be provided, as shown in Figures 5(A) and 5(B). By dividing the containment space 403 into multiple sections in this way, if the degree of adsorption differs depending on the vertical position of the container body 401, it becomes easier to replace the adsorbent at each location. For example, if the adsorbent in the containment space 403 on the lowermost port 407 side is significantly degraded, but the adsorbent in the other containment spaces 403 is not degraded, only the adsorbent in the containment space 403 on the lowermost port 407 side can be replaced. This minimizes the amount of adsorbent that needs to be replaced, thereby reducing the amount of adsorbent used.

[0074] ·Rectifier plate In the examples shown in Figures 5(A) and 5(B), multiple rectifier plates 404 are provided. However, as mentioned above, there may be only one rectifier plate 404. The rectifier plates 404 are arranged at intervals along the direction of gas passage, so as to divide the internal space of the container body 401 substantially perpendicular to the direction of gas (exhaust gas and inert gas) passage. That is, the rectifier plates 404 are provided substantially horizontally, defining the containment space 403 inside the container body 401. In other words, in this embodiment, the rectifier plate 404 has both the function of a rectifier plate and the function of a partition wall. By providing the rectifier plate 404 substantially perpendicular to the direction of gas passage, the gas can be reliably allowed to pass through the rectifier plate 404.

[0075] It is preferable that the rectifier plate 404 is fixed and supported so as to be in contact with multiple locations on the inner wall portion 406 that defines the adsorbent containment space 403. In this case, the load of the rectifier plate 404 (or the rectifier plate 404 and the adsorbent) can be shared at multiple locations between the rectifier plate 404 and the inner wall portion 406. In other words, it is possible to prevent excessively large loads from being placed on specific locations and improve the durability of the rectifier plate 404 and the container body 401. In particular, it is preferable that the multiple locations on the containment space 403 that support the rectifier plate 404 are positioned approximately point-symmetric with respect to the center of the containment space 403 when viewed from above. This makes it easier to distribute the load on the rectifier plate 404 and the inner wall portion 406, and further improves the durability of the rectifier plate 404 and the container body 401.

[0076] As shown in Figure 6(A), the rectifier plate 404 has through holes 4041 and plate-shaped portions 4042. Figure 6 shows an example of a rectifier plate (Figure 6(A)) and an example of a flow path changing mechanism (Figure 6(B)). The through holes 4041 penetrate the rectifier plate 404 in its thickness direction (direction of gas passage) and are provided in multiple locations in the in-plane direction of the rectifier plate 404. The plate-shaped portions 4042 are provided to obstruct the passage of gas. With this configuration, when gas passing through the container body 401 reaches the rectifier plate 404, it is blocked by the plate-shaped portions 4042 and distributed to each of the through holes 4041. This spreads the gas radially (width direction and depth direction) of the container body 401, allowing the gas to reach the adsorbent packed in that radial direction, thereby preventing or suppressing excessive deterioration of the adsorbent at specific locations. Furthermore, by preventing turbulence in the gas flow direction, the energy required for pressurizing the exhaust gas by the air supply pump P1 and for depressurizing the inert gas by the depressurization pump P2 can be reduced.

[0077] The diameter of the through-hole 4041 is preferably smaller than that of the adsorbent. This prevents the adsorbent from mixing between the containment spaces 403 separated by the rectifier plate 404. Therefore, as described above, only the adsorbent that has deteriorated the most can be replaced. Furthermore, the ratio of the total area of ​​the through-holes 4041 to the total area of ​​the rectifier plate 404 (or the radial area of ​​the container body 401) (in other words, the opening ratio of the rectifier plate 404) is preferably 20% to 70%, and more preferably 30% to 60%. This prevents excessive obstruction of the gas flow while appropriately regulating the flow direction.

[0078] Furthermore, the external shape of the through-hole 4041 in plan view is not limited to a circular shape as shown in Figure 6(A), but may be a polygonal shape such as an ellipse, triangle, rectangle, or hexagon, or it may be an irregular shape such as a star or a four-pointed star. Furthermore, two or more rectifier plates 404 may be provided between the accommodation spaces 403. In this case, rectifier plates 404 with different shapes, total number of plate-like portions 4042, and planar area of ​​the plate-like portions 4042 may be used. Moreover, the number of accommodation spaces 403 formed by the rectifier plates 404 is not limited to three as shown in Figure 5, but may be two or fewer, or four or more.

[0079] • Flow path change mechanism As shown in Figures 5(A) and 5(B), the flow path changing mechanism 405 changes the gas flow path on the inlet side (lower port 407 or upper port 408) of the container body 401. More specifically, as shown in Figure 6(B), the flow path changing mechanism 405 comprises a shielding portion 4051 and a leg portion 4052. Figure 6(B) illustrates the flow path changing mechanism 405 on the lower port 407 side. The leg portion 4052 fixes the flow path changing mechanism 405 to the inner wall portion 406 of the container body 401. The shielding portion 4051 is provided in an in-plane direction (approximately horizontal direction) perpendicular to the gas passage direction and shields the exhaust gas that reaches the inside of the container body 401 from the inlet (lower port 407). The exhaust gas that hits the lower surface of the shielding portion 4051 changes its flow path to the radially outward side of the container body 401, and the exhaust gas spreads radially. Next, the spread exhaust gas passes through the rectifier plate 404 and comes into contact with the adsorbent. In this way, by providing the flow path changing mechanism 405, the gas that has reached the container body 401 from a relatively narrow inlet is spread radially through the container body 401, allowing the gas to come into relatively uniform contact with the adsorbent located from the radial center to the edges.

[0080] Figure 6(B) shows an example where the flow path modification mechanism 405 also functions as a leg for the rectifier plate 404. This allows the lowest (lower port 407) rectifier plate 404, which bears the greatest weight load, to be supported from below. Therefore, it is possible to prevent or suppress the rectifier plate 404 from falling off the inner wall 406 of the container body 401. In addition, the uppermost (upper port 408) rectifier plate 404 (see Figures 5(A) and 5(B)) can be supported by the ceiling of the container body 401 via the rectifier plate 404 above it, thereby reducing the weight load on the lowest rectifier plate 404.

[0081] Furthermore, the flow path changing mechanism is not limited to the shape shown in Figure 6(B), as long as it can change the gas flow path and spread it throughout the entire internal space (container space 403) of the container body 401, as described above. For example, the flow path changing mechanism 405 may consist only of a shielding portion 4051 connected to the rectifier plate 404, or the leg portion 4052 may be connected to the side of the container body 401.

[0082] ·Monitoring aid mechanism The monitoring assistance mechanism 402 shown in Figure 4 is provided for monitoring the adsorbent contained in the container body 401. The monitoring assistance mechanism 402 has a window portion 402a, an upper sampling portion 402b, a lower sampling portion 402c, an intermediate temperature measuring portion 402d, an upper temperature measuring portion 402e, and a lower temperature measuring portion 402f. The window 402a is configured to allow the color of the adsorbent to be visually inspected. The window 402a may be, for example, a transparent glass window or a camera installed inside the container body 401. The position where the window 402a is located is not particularly limited, but it is preferable to provide one for each storage space 403 (see Figures 5(A) and 5(B)), as shown in Figure 4. This allows the color of the adsorbent to be checked for each storage space 403. The degree of deterioration can be determined according to the color of the adsorbent, and the adsorbent can be replaced for each storage space 403.

[0083] The upper sampling section 402b and the lower sampling section 402c are provided near the gas inlet and outlet of the container body 401, and are configured to collect exhaust gas (first gas or third gas), inert gas (second gas), or off gas (fourth gas). The upper sampling section 402b and the lower sampling section 402c may be sampling ports such as valves, or they may be gas chromatography devices that collect and analyze gas from the container body 401 or the lower port 407 or upper port 408. This makes it possible to compare the gas composition near the inlet and near the outlet, thereby confirming the degree of deterioration of the entire adsorbent contained in the container body 401. The intermediate temperature measuring section 402d, the upper temperature measuring section 402e, and the lower temperature measuring section 402f are each configured to contact the adsorbent or gas inside the container body 401, and to measure the temperature of the adsorbent or gas in the central, upper, and lower parts of the container body 401. The intermediate temperature measuring section 402d, the upper temperature measuring section 402e, and the lower temperature measuring section 402f are, for example, thermocouples. When the adsorbent deteriorates, the amount of heat generated during adsorption and the amount of heat absorbed during regeneration may decrease, so the deterioration state can be confirmed by measuring the temperature.

[0084] In this way, by providing the monitoring assistance mechanism 402, parameters that may change as the adsorbent deteriorates (hereinafter also referred to as "information regarding the adsorbent") can be obtained. The information regarding the adsorbent preferably includes at least one of the following: a) the color of the adsorbent, b) the chemical composition of the exhaust gas (third gas) on the outlet (upper port 408) side, c) the chemical composition of the off-gas (fourth gas) on the outlet (lower port 407) side, d) the average temperature inside the container body 401 when adsorbing impurities from the exhaust gas (first gas) (adsorption process), e) the average temperature inside the container body 401 when regenerating the adsorbent (regeneration process), f) the temperature difference of the adsorbent between the inlet (lower port 407) side and the outlet (upper port 408) side when adsorbing impurities from the exhaust gas (first gas) (adsorption process), and g) the temperature difference of the adsorbent between the inlet (upper port 408) side and the outlet (lower port 407) side when regenerating the adsorbent (regeneration process). According to the inventors' research, at least one of a to g changes as the adsorbent deteriorates. Therefore, with this configuration, the degree of deterioration of the adsorbent can be determined, and the temperature difference between the exhaust gas (first gas) and the inert gas (second gas) supplied to the reaction vessel 40 can be appropriately controlled.

[0085] (Control mechanism) Hardware configuration The control mechanism 6 acquires information about the adsorbent via the monitoring assistance mechanism 402 and controls the cooling mechanism 42 and the heating mechanism 44 based on the information about the adsorbent. The control mechanism 6 comprises a sensor unit 60, a cooling control unit 62, and a heating control unit 61. The sensor unit 60 includes a communication unit 601, a storage unit 602, a processor 603, and an acquisition unit 605, and these components are electrically connected within the sensor unit 60 via a communication bus 604. Figure 7 shows the hardware configuration of the control mechanism 6.

[0086] The acquisition unit 605 is configured to acquire information about the adsorbent. The acquisition unit 605 includes, for example, a camera that acquires information about the color of the adsorbent through the window 402a, a sensor or communication device that acquires information about the chemical composition of the gas through the upper sampling unit 402b and the lower sampling unit 402c, and wires that acquire information about the temperature of the adsorbent or the inside of the container body 401 from the intermediate temperature measuring unit 402d, the upper temperature measuring unit 402e, and the lower temperature measuring unit 402f. The acquisition unit 605 acquires various types of information based on control signals from the processor 603.

[0087] The communication unit 601 is configured to transmit various electrical signals from the sensor unit 60 to external components. The communication unit 601 is also configured to receive various electrical signals from external components to the communication unit 601. The communication unit 601 preferably uses wired communication methods such as USB, IEEE1394, Thunderbolt®, and wired LAN network communication, but may also include wireless LAN network communication, mobile communication such as 3G / LTE / 5G, and Bluetooth® communication as needed. In other words, it is more preferable to implement it as a collection of these multiple communication methods. Specifically, the communication unit 601 transmits control signals from the processor 603 to the heating control unit 61 and the cooling control unit 62.

[0088] The storage unit 602 stores various types of information as defined above. This can be implemented, for example, as a storage device such as a solid-state drive (SSD) that stores various programs related to the acquisition unit 605 executed by the processor 603, or as memory such as random access memory (RAM) that stores temporarily necessary information (arguments, arrays, etc.) related to program calculations. The storage unit 602 stores various programs and variables related to the acquisition unit 605 executed by the processor 603. In particular, the memory unit 602 stores information about the adsorbent acquired by the acquisition unit 605. The memory unit 602 also stores reference information regarding the relationship between the information about the adsorbent and the temperature that the exhaust gas or inert gas should have in the container body 401 (i.e., the temperature set in the cooling mechanism 42 or heating mechanism 44). The reference information may include, for example, a table for determining the set temperature of the cooling mechanism 42 or heating mechanism 44 based on information about the adsorbent, a conditional expression for uniquely calculating the set temperature based on information about the adsorbent, or a trained machine learning model that determines the degree of deterioration of the adsorbent and outputs the set temperature by inputting information about the adsorbent.

[0089] The processor 603 is, for example, a central processing unit (CPU) not shown. The processor 603 realizes various functions related to the acquisition unit 605 by reading a predetermined program stored in the storage unit 602. That is, information processing by software stored in the storage unit 602 is concretely realized by the processor 603, which is an example of hardware, and can be executed as each functional unit included in the processor 603. Note that the processor 603 is not limited to a single unit, and may be implemented with multiple processors 603 for each function, or a combination thereof. Specifically, the processor 603 controls the measurement interval of various information by the acquisition unit 605 (for example, every 10 minutes, every hour, every day, every week, etc.), communication via the communication unit 601, digitization of various information output from the acquisition unit 605, and storage of the digitized information in the storage unit 602. Furthermore, the processor 603 is configured to determine the degree of degradation of the adsorbent based on information about the adsorbent. It is also configured to determine the temperatures of the cooling mechanism 42 and the heating mechanism 44 that should be set based on the degree of degradation of the adsorbent.

[0090] Furthermore, the heating control unit 61 includes a communication unit 611, a storage unit 612, and a processor 613, and these components are electrically connected within the heating control unit 61 via a communication bus 614. The cooling control unit 62 includes a communication unit 621, a storage unit 622, and a processor 623, and these components are electrically connected within the cooling control unit 62 via a communication bus 624. The communication unit 611 and the communication unit 621 receive, for example, control signals from the sensor unit 60. The storage unit 612 and the storage unit 622 store, for example, control signals from the sensor unit 60. The processor 613 and the processor 623 control the temperatures of the cooling mechanism 42 and the heating mechanism 44, respectively, based on, for example, the control signals from the sensor unit 60. The basic configuration of the communication unit 611 and 621, the storage unit 612 and 622, and the processors 613 and 623 is the same as that described for the communication unit 601, the storage unit 602, and the processor 603.

[0091] • Processor functional configuration Next, the functional configuration of the processor 603 of the sensor unit 60 will be described. As mentioned above, the information processing by the software stored in the memory unit 602 is specifically realized by the processor 603, which is an example of hardware, and can be executed as each functional unit included in the processor 603. Figure 8 is a block diagram showing the functions realized by the processor and other components in the information processing device. Specifically, the processor 603 includes an acquisition unit 6031, an input processing unit 6032, and an output unit 6033.

[0092] The acquisition unit 6031 is configured to acquire various information that has been acquired from an external source via the communication unit 601 or the acquisition unit 605, or that has been previously stored in the storage unit 602. For example, the acquisition unit 6031 acquires various information stored in the storage unit 602, namely information related to the adsorbent acquired by the acquisition unit 605, reference information, and so on. The input processing unit 6032 is configured to input information about the adsorbent acquired by the acquisition unit 6031 into the reference information stored in the storage unit 602. The output unit 6033 is configured to output various types of information. Specifically, the output unit 6033 can output the degree of deterioration of the adsorbent determined based on the reference information, or the set temperature of the cooling mechanism 42 or the heating mechanism 44.

[0093] As described above, the separation device 4 allows for appropriate setting of the temperature of the exhaust gas (first gas) when adsorbing and removing impurities with the adsorbent, and the temperature of the inert gas (second gas) used to detach and recover impurities from the adsorbent and regenerate the adsorbent. This balances the adsorption and regeneration of the adsorbent, allowing for sufficient purification of the exhaust gas while extending the lifespan of the adsorbent. Furthermore, the amount of inert gas (first gas) used to regenerate the adsorbent can be kept to a minimum. Furthermore, with the manufacturing apparatus 1 and manufacturing system 100 having such a separation device 4, impurities can be sufficiently removed from the exhaust gas before organic substances are produced in the production unit 2. As a result, the production unit 2 can be miniaturized, and the catalyst, energy, etc., consumed in the production unit 2 can be reduced. Therefore, it is possible to reduce the environmental impact during the production of organic materials and improve the life cycle assessment (LCA) of organic materials.

[0094] [Methods for producing organic substances] Next, we will explain the method for producing organic substances (the method for producing regenerative adsorbents). [1] First, exhaust gas containing carbon monoxide, carbon dioxide, and hydrogen is supplied from the gasifier 10 (see Figure 1). If the manufacturing device 1 has a reduction device, the exhaust gas is mixed with hydrogen in the reduction device. As a result, at least a portion of the carbon dioxide in the exhaust gas is reduced to produce carbon monoxide.

[0095] [2] Next, the exhaust gas is supplied to the pre-processing unit 5 (preparation step to prepare the first gas containing the exhaust gas). After soot and other particles are removed from the exhaust gas in the filter device 3 of the pre-processing unit 5, the exhaust gas is supplied to the separation device 4. At this time, an inert gas (a second gas containing the inert gas) is supplied to the inert gas supply unit 43 (see Figure 3), and an adsorbent is pre-filled in the container body 401 of the pressure swing adsorption type reaction vessel 40, which has a gas inlet and outlet (preparation step). The filled adsorbent may be unused adsorbent or recycled adsorbent obtained by regenerating used adsorbent.

[0096] The exhaust gas is supplied to gas line GL41, which is connected to gas line GL1, and cooled by cooling mechanism 42. The temperature at which the exhaust gas should be cooled is set by control mechanism 6 based on information about the adsorbent and reference information. It is also preferable to use the heat generated during cooling for heating mechanisms 44 and other parts that require heat. The cooled exhaust gas (first gas) is supplied by the air pump P1, pressurizing the inside of the container body 401 as it passes through the container body 401. At this time, valves V1 and V2 are open, while valves V3 and V4 are closed. As a result, impurities in the exhaust gas (first gas) are adsorbed onto the adsorbent inside the container body 401, yielding exhaust gas from which impurities have been removed (third gas) and adsorbent that has adsorbed impurities (post-adsorption adsorbent) (adsorption step). The exhaust gas (third gas), from which impurities have been removed, is supplied to the generation unit 2 by passing through the upper port 408, gas line GL42, and gas line GL1. Furthermore, the exhaust gas (first gas and third gas) may be collected at the inlet (lower port 407) and outlet (upper port 408) sides of the container body 401 by the lower sampling section 402c and the upper sampling section 402b, and acquired by the sensor section 60 of the control mechanism 6 as information regarding the adsorbent.

[0097] When the adsorption efficiency of the adsorbent decreases or is expected to decrease, valves V1 and V2 are closed, and valves V3 and V4 are opened. Then, inert gas is supplied from the inert gas supply unit 43 to the gas line GL43 and heated by the heating mechanism 44. The temperature at which the inert gas should be heated is set by the control mechanism 6 based on information about the adsorbent and reference information. The heated inert gas (second gas) is depressurized by the depressurizing pump P2, causing it to pass through the container body 401 while reducing the pressure inside the container body 401. This transfers impurities adsorbed on the adsorbent to the inert gas (second gas), resulting in the production of off-gas (fourth gas) and regenerated adsorbent (regenerated adsorbent) (regeneration process). As described above, it is preferable that the temperature of the inert gas (second gas) in the regeneration process is higher than the temperature of the exhaust gas (first gas) in the adsorption process. It is preferable that the off-gas be classified according to the type of impurity and then used in various parts of the manufacturing system 100 or manufacturing apparatus 1, or filled into containers and shipped. Furthermore, the inert gas (second gas) and off-gas (fourth gas) may be collected by the upper sampling section 402b and the lower sampling section 402c at the inlet (upper port 408) and outlet (lower port 407) sides of the container body 401, and acquired by the sensor section 60 of the control mechanism 6 as information regarding the adsorbent. Furthermore, the adsorption of impurities by the adsorbent and the regeneration of the adsorbent by the inert gas are preferably carried out simultaneously in different reaction vessels 40 (for example, reaction vessel 40a and reaction vessel 40b), as explained with reference to Figure 2, thereby enabling continuous adsorption and regeneration.

[0098] [3] The exhaust gas (third gas) that has passed through the pre-processing unit 5 is supplied to the generation unit 2. In the generation unit 2, an organic substance-containing liquid mainly containing organic substances generated from the exhaust gas is obtained. If the organic substance generated in the generation unit 2 is a gas, the generated organic substance can be cooled to produce an organic substance-containing liquid. [4] The organic substance-containing liquid produced in the generation unit 2 is supplied to the purification unit 7 via the liquid line LL. In the purification unit 7, the organic substance contained in the organic substance-containing liquid is purified, and a purified product containing organic substance at a high concentration is obtained.

[0099] According to the method for producing organic substances (method for producing regenerated adsorbents) described above, impurities can be sufficiently removed from the exhaust gas before the organic substance is produced in the production unit 2. Therefore, the production unit 2 can be miniaturized, and the catalyst, energy, etc., consumed in the production unit 2 can be reduced. Furthermore, the energy required for regenerating the adsorbent can be minimized, extending its lifespan. Therefore, the environmental impact during the production of organic materials can be reduced, and the life cycle assessment (LCA) of organic materials can be improved.

[0100] [Differentiation] The following describes modifications of the embodiments described above. Note that the embodiments described above and the following descriptions are interchangeable. The valuable materials produced by the manufacturing system 100 or manufacturing apparatus 1 do not have to be organic substances. For example, the final products may be carbon monoxide itself, metal carbonyl compounds (e.g., Fe(CO)5 or Ni(CO)4), or inorganic substances such as calcium hydroxide.

[0101] The cooling mechanism 42 and heating mechanism 44 of the separation device 4 do not need to adjust the temperature of the exhaust gas (first gas) and inert gas (second gas) before they pass through the reaction vessel 40; it is sufficient if they can adjust the temperature of the exhaust gas (first gas) and inert gas (second gas) as they pass through the reaction vessel 40. For example, at least one of the cooling mechanism 42 and the heating mechanism 44 may adjust the temperature of the reaction vessel 40 itself, rather than the gas line GL41 or gas line GL43. Furthermore, in the separation device 4, it is sufficient to set the temperature relationship between the exhaust gas (first gas) and the inert gas (second gas) as described above. For example, the cooling mechanism 42 may be omitted, and only the heating mechanism 44 may be provided. In this case, the regeneration of the adsorbent is more likely to be prioritized, so the adsorbent can be used for a longer period of time.

[0102] The monitoring assistance mechanism 402 of the reaction vessel 40 does not need to include all of the window section 402a to the lower temperature measuring section 402f; it is sufficient to have any one of them. The monitoring assistance mechanism 402 should be configured so that information regarding the adsorbent can be appropriately set according to parameters such as the adsorbent, impurities, and exhaust gas composition, and the necessary information regarding the adsorbent can be obtained. The directions in which the exhaust gas (first gas) and the inert gas (second gas) pass may be the same or different, or they may be in opposite directions to those shown in Figures 2 and 4. In other words, the inlet for the inert gas may be the lower port 407 and the inlet for the exhaust gas may be the upper port 408.

[0103] The control mechanism 6 may also be configured to further control the timing of adsorption and regeneration. For example, if it is determined that the degree of deterioration of the adsorbent has progressed based on information about the adsorbent and reference information, the control mechanism 6 may be configured to set a longer regeneration (supply of inert gas) time. The control mechanism 6 may be partially or entirely omitted. That is, in the method for producing organic substances (regenerative adsorbents), steps such as obtaining information about the adsorbent and setting the temperature of the cooling mechanism 42 or heating mechanism 44 may be performed manually.

[0104] The product may be provided in any of the following embodiments.

[0105] (1) A method for producing a regenerated adsorbent, comprising: a preparation step of preparing a first gas containing exhaust gas, a second gas containing an inert gas, and an adsorbent filled in the container body of a pressure swing adsorption type reaction vessel having a gas inlet and outlet; an adsorption step of passing the first gas through the container body while pressurizing the inside of the container body to adsorb impurities in the first gas onto the adsorbent to obtain a third gas and a post-adsorption adsorbent; and a regeneration step of passing the second gas through the container body while depressurizing the inside of the container body to transfer the impurities adsorbed on the post-adsorption adsorbent into the second gas to obtain a fourth gas and a regenerated adsorbent, wherein the temperature of the second gas in the regeneration step is higher than the temperature of the first gas in the adsorption step.

[0106] (2) A method for producing a regenerated adsorbent as described in (1) above, wherein the preparation step further involves cooling the first gas.

[0107] (3) A method for producing a regenerated adsorbent as described in (1) or (2) above, wherein the difference between the temperature of the first gas in the adsorption step and the temperature of the second gas in the regeneration step is 15°C or more.

[0108] (4) A method for producing a regenerated adsorbent according to any one of (1) to (3) above, wherein the temperature of the first gas in the adsorption step is -5°C or more and 40°C or less, and the temperature of the second gas in the regeneration step is 30°C or more and 500°C or less.

[0109] (5) A method for producing a regenerated adsorbent according to any one of (1) to (4) above, wherein the container body is provided with at least one rectifier plate inside it.

[0110] (6) A method for manufacturing a regenerative adsorbent as described in (5) above, wherein the rectifier plate is installed so as to divide the internal space of the container body substantially perpendicular to the direction of gas passage.

[0111] (7) A method for producing a regenerated adsorbent according to (5) or (6) above, wherein the at least one rectifier plate is a plurality of rectifier plates, and the rectifier plates are arranged at intervals along the direction of gas passage.

[0112] (8) A method for producing a regenerated adsorbent according to any one of (5) to (7) above, wherein the container body is further provided with a flow path changing mechanism on the inlet side of the rectifier plate.

[0113] (9) A method for producing a regenerated adsorbent according to any one of (1) to (8) above, wherein the container body is coated on its inner surface, and the ratio of the thermal expansion coefficient of the coating to the thermal expansion coefficient of the constituent material forming the container body is 0.1 or more and 2 or less.

[0114] (10) In the method for producing a regenerated adsorbent described in any one of (1) to (9) above, the amount of adsorbent to be filled into the adsorbent containment space in the container body is 300 kg / m 3 More than 900kg / m 3 The method for producing a regenerative adsorbent is as follows.

[0115] (11) A method for producing a regenerated adsorbent according to any one of (1) to (10) above, wherein the difference between the temperature of the first gas in the adsorption step and the temperature of the second gas in the regeneration step is increased as the degree of deterioration of the adsorbent progresses.

[0116] (12) A method for producing a regenerated adsorbent as described in (11) above, wherein the degree of deterioration of the adsorbent is determined based on at least one of the following: a) the color of the adsorbent, b) the chemical composition of the third gas, c) the chemical composition of the fourth gas, d) the average temperature inside the container body during the adsorption step, e) the average temperature inside the container body during the regeneration step, f) the temperature difference of the adsorbent between the inlet side and the outlet side during the adsorption step, and g) the temperature difference of the adsorbent between the inlet side and the outlet side during the regeneration step.

[0117] (13) A method for producing a regenerated adsorbent as described in (12) above, wherein the degree of degradation of the adsorbent is determined based on at least one of the above and a trained model, and the trained model is a model that has been pre-trained on the relationship between the degree of degradation and at least one of the above. Of course, this is not always the case.

[0118] As previously stated, various embodiments relating to this disclosure have been described, but these are presented as examples only and do not limit the scope of the invention in any way. The 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. Such 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.

[0119] For example, the organic material manufacturing system and organic material manufacturing apparatus of the present disclosure may each have any other additional configurations, may be replaced with any configurations that perform similar functions, and some configurations may be omitted. Furthermore, the method for producing organic substances (method for producing regenerated adsorbent) of the present disclosure may have any additional steps compared to the above embodiment, may be replaced by any steps that perform similar functions, and some steps may be omitted. [Explanation of Symbols]

[0120] 1: Manufacturing equipment 10: Gasification furnace 100: Manufacturing System 2: Generation part 7: Purification equipment 5: Pre-processing section 52: Bulkhead 53: Small space 3: Filter device 4: Separation device 40: Reaction vessel 40a: Reaction vessel 40b: Reaction vessel 401: Container body 402: Monitoring support mechanism 402a: Window section 402b: Upper sampling section 402c:Lower sampling part 402d: Intermediate temperature sensor 402e: Upper temperature sensor 402f: Lower temperature measuring section 403: Containment Space 404: Rectifier plate 4041: Through hole 4042: Plate-like part 405: Flow path change mechanism 4051: Shielding part 4052: Legs 406: Interior wall section 407: Lower port 408: Upper port 42: Cooling mechanism 43: Inert gas supply unit 44:Heating mechanism 6: Control mechanism 60: Sensor unit 601: Communications Department 602: Storage section 603: Processor 6031: Acquisition Department 6032: Input Processing Unit 6033: Output section 604: Communications bus 605: Acquisition Department 61: Heating control unit 611: Communications Department 612: Storage section 613: Processor 614: Communications bus 62: Cooling Control Unit 621: Communications Department 622: Storage section 623: Processor 624: Communications bus GL1: Gas line GL41: Gas line GL42: Gas line GL43: Gas line GL44: Gas line LL: Liquid line P1: Air supply pump P2: Pressure reducing pump PSA: See above V1: Valve V2: Valve V3: Valve V4: Valve

Claims

1. A method for producing a regenerating adsorbent, The process involves preparing a first gas containing exhaust gas, a second gas containing an inert gas, and an adsorbent which is a porous material filled into the container body of a pressure swing adsorption type reaction vessel having a gas inlet and outlet, and also a preparation step of cooling the first gas. An adsorption step is performed by pressurizing the inside of the container body and passing the first gas through the container body, thereby adsorbing impurities in the first gas onto the adsorbent, to obtain a third gas and a post-adsorption adsorbent. The process includes a regeneration step in which the second gas is passed through the container body while the pressure inside the container body is reduced, thereby transferring the impurities adsorbed on the adsorbent after adsorption into the second gas, and obtaining a fourth gas and a regenerated adsorbent. The temperature of the second gas in the regeneration process is higher than the temperature of the first gas in the adsorption process. As the degree of deterioration of the adsorbent progresses, the difference between the temperature of the first gas in the adsorption process and the temperature of the second gas in the regeneration process is increased. A method for producing a regenerated adsorbent.

2. In the method for producing a regenerative adsorbent according to claim 1, The difference between the temperature of the first gas in the adsorption step and the temperature of the second gas in the regeneration step is 15°C or more. A method for producing a regenerated adsorbent.

3. In the method for producing a regenerative adsorbent according to claim 1, The temperature of the first gas in the adsorption step is between -5°C and 40°C. The temperature of the second gas in the regeneration process is 30°C or higher and 500°C or lower. A method for producing a regenerative adsorbent.

4. In the method for producing a regenerative adsorbent according to claim 1, The container body is provided with at least one rectifier plate inside. A method for producing a regenerative adsorbent.

5. In the method for producing a regenerating adsorbent according to claim 4, The rectifier plate is installed so as to divide the internal space of the container body substantially perpendicular to the direction of gas passage. A method for producing a regenerated adsorbent.

6. In the method for producing a regenerating adsorbent according to claim 4, The aforementioned at least one rectifier plate is a plurality of rectifier plates, The rectifier plates are arranged at intervals along the direction of gas passage. A method for producing a regenerated adsorbent.

7. In a method for producing a regenerated adsorbent according to any one of claims 4 to 6, The container body is further provided with a flow path modification mechanism on the inlet side of the rectifier plate. A method for producing a regenerated adsorbent.

8. In the method for producing a regenerative adsorbent according to claim 1, The container body has a coating applied to its inner surface. The ratio of the thermal expansion coefficient of the coating to the thermal expansion coefficient of the constituent material forming the container body is 0.1 or more and 2 or less. A method for producing a regenerated adsorbent.

9. In the method for producing a regenerative adsorbent according to claim 1, The amount of adsorbent to be filled into the adsorbent containment space within the container body is 300 kg / m³. ３ More than 900kg / m ３ The following is: A method for producing a regenerated adsorbent.

10. In the method for producing a regenerative adsorbent according to claim 1, The degree of deterioration of the adsorbent is determined based on at least one of the following: a) the color of the adsorbent, b) the chemical composition of the third gas, c) the chemical composition of the fourth gas, d) the average temperature inside the container body during the adsorption process, e) the average temperature inside the container body during the regeneration process, f) the temperature difference of the adsorbent between the inlet and outlet sides during the adsorption process, and g) the temperature difference of the adsorbent between the inlet and outlet sides during the regeneration process. A method for producing a regenerated adsorbent.

11. In the method for producing a regenerated adsorbent according to claim 10, The degree of degradation of the adsorbent is determined based on at least one of the trained models. The aforementioned trained model is a model that has been pre-trained on the relationship between the degree of degradation and at least one of the aforementioned factors. A method for producing a regenerated adsorbent.

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