JP7316858B2 - Systems for storing carbon dioxide, methods for improving water quality, and methods for producing fertilizers - Google Patents

Description

One embodiment of the present invention relates to a carbon dioxide storage system, a method for improving water quality, and a method for producing fertilizer.

The fixation and storage of carbon dioxide, which is a greenhouse gas, is an important issue in suppressing rapid environmental changes on a global scale caused by greenhouse gases. In Patent Document 1 and Non-Patent Document 1, by carbonizing organic matter including waste derived from plants and animals and using this as a material for soil improvement, atmospheric dioxide reduced and fixed by plants Techniques for storing carbon underground in the form of carbon have been disclosed.

JP-A-2007-75706

Akira Shibata, "Simple carbonization of biomass and carbon-storing vegetables COOL VEGETM for regional development", Journal of High Temperature Society, March 2011, Vol. 37, No. 2, p. 37-42

One of the objects of one of the embodiments of the present invention is to provide a carbon storage system capable of contributing to the suppression of global warming by storing atmospheric carbon dioxide in the ground as carbon. . Another object of one of the embodiments of the present invention is to provide a method for improving water quality using a porous material obtained from biomass. Another object of one of the embodiments of the present invention is to provide a method for producing fertilizer using a porous material obtained from biomass.

One embodiment of the present invention is a system for storing carbon dioxide. The system includes a first means of carbonizing biomass to produce a carbide and a carbonized gas, a second means of generating electricity using the carbonized gas, a third means of fixing metal on the carbonized material, and a A fourth means for causing the charcoal to adsorb at least one compound containing phosphorus, and a fifth means for producing a fertilizer from the charcoal to which the compound is adsorbed.

One embodiment of the invention is a method of improving water quality. This method includes carbonizing a first biomass to produce a carbide and a first dry distillation gas, immersing the carbide in a liquid containing a metal salt, and reducing the metal salt adsorbed on the carbide to obtain a metal-supported carbide. and immersing the metal-supported carbide in water containing at least one phosphorus-containing compound.

One embodiment of the present invention is a method of making fertilizer. This method includes carbonizing a first biomass to produce a carbide and a first dry distillation gas, immersing the carbide in a liquid containing a metal salt, and reducing the metal salt adsorbed on the carbide to obtain a metal-supported carbide. and immersing the metal-supported carbide in water containing at least one phosphorus-containing compound.

One embodiment of the present invention is a method of modifying soil. This method includes carbonizing a first biomass to produce a carbide and a first dry distillation gas, immersing the carbide in a liquid containing a metal salt, and reducing the metal salt adsorbed on the carbide to obtain a metal-supported carbide. , immersing the metal-supported carbide in water containing at least one phosphorus-containing compound, and spraying the water-immersed metal-supported carbide onto soil.

According to embodiments of the present invention, carbon dioxide in the atmosphere can be stored underground in the form of carbon, contributing to the suppression of the greenhouse effect. Alternatively, it can effectively improve the water quality of rivers, lakes, or seas. Alternatively, it becomes possible to produce a fertilizer effective for growing plants at low cost.

1 is a conceptual diagram of a carbon dioxide storage system that is one of the embodiments of the present invention; FIG. A system for manufacturing an adsorbent that constitutes a carbon dioxide storage system that is one embodiment of the present invention. 1 is a schematic cross-sectional view of a gasifier included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a gasifier included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a gasifier included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a heat exchanger included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a block diagram of a power generator included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of an immersion device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a drying device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a reduction device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a reduction device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a reduction device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. 1 is a schematic cross-sectional view of a reduction device included in a carbon dioxide storage system that is one embodiment of the present invention; FIG. A cartridge used in a water quality improvement method that is one embodiment of the present invention. The flowchart which shows the manufacturing method of the fertilizer which is one embodiment of this invention.

Hereinafter, each embodiment of the present invention will be described with reference to the drawings and the like. However, the present invention can be implemented in various aspects without departing from the gist thereof, and should not be construed as being limited to the description of the embodiments illustrated below.

In the drawings, in order to make the description clearer, the width, thickness, shape, etc. of each part may be schematically represented compared to the actual embodiment, but this is only an example and limits the interpretation of the present invention. not something to do. In this specification and each drawing, elements having the same functions as those described with respect to the previous drawings may be denoted by the same reference numerals, and redundant description may be omitted.

Hereinafter, in the present specification, biomass refers to a substance derived from living organisms, which is a kind of organic matter, and its metabolites. Examples of biomass include materials derived from trees. Specific examples include wood products such as plate-like or column-like wood, thinning wood, pruning waste wood, construction waste wood, powdered sawdust, and particle boats. There are no restrictions on the type of wood, and cedar, cypress, and bamboo may be used. Other examples of biomass include agricultural waste such as rice husks, bagasse, corn cobs and leaves, and agricultural by-products such as straw, straw, and hay. Other examples include plants used as raw materials for fibers such as hemp, flax, cotton, sisal, abaca, and palm hair. Alternatively, algae such as seaweed may be used. Other examples include food waste and silage obtained from animal manure.

1. Carbon Dioxide Storage System FIG. 1 is a conceptual diagram illustrating a system 100 for storing carbon dioxide in the atmosphere (Carbon-Soring System, hereinafter referred to as CS system), which is one embodiment of the present invention. In this CS system 100, plants create bioresources by reducing carbon dioxide through photosynthesis and fixing it as various organic substances. Biological resources are used not only as an energy source (food) for other organisms, but also as functional and structural materials such as fibers and wood for various purposes. The CS system 100 further carbonizes organic residues, by-products and metabolites, namely biomass, which are used in various ways, to produce adsorbents and dry distillation gas, and at the same time to create electrical energy. In addition, water quality improvement utilizing the adsorption capacity of compounds containing phosphorus and nitrogen (hereinafter also referred to as adsorbents) possessed by adsorbents, production of fertilizers using adsorbents with adsorbents adsorbed, and soil improvement using these fertilizers is done. By returning the sorbent to the ground as fertilizer, the carbon dioxide fixed by the plants is stored in the ground as carbon.

A carbide is a porous material containing carbon as a main component, and a metal-supported carbide obtained by supporting a metal on this porous material functions as an adsorbent. Although the details will be described later, after the metal salt is adsorbed on the carbide to obtain the metal salt-supported carbide (precursor carbide), at least part of the supported metal salt is metal (zero-valent metal) An adsorbent is obtained by reduction to This adsorbent can adsorb compounds containing phosphorus and nitrogen, which are water pollutants in water areas such as rivers, lakes, and seas. In particular, iron-supported adsorbents are effective in adsorbing phosphorus-containing compounds. Examples of the phosphorus-containing compound include phosphoric acid, metal phosphates such as calcium, iron, aluminum, sodium, and potassium, metaphosphates, pyrophosphates, and organic phosphoric acids such as phosphate esters. be. Nitrogen-containing compounds include ammonia, ammonium chloride, ammonium sulfate, ammonium nitrate, amines, urea, nitrogen-containing heteroaromatic compounds, metal nitrates and nitrites, and the like.

The dry distillation gas generated during carbonization includes combustible or reducing gases such as hydrogen, carbon monoxide, methane, propane, and alkanes represented by butane. The CS system 100 utilizes both the combustibility and reducing power of the carbonization gas. As will be described later, the former combustible gas is used for power generation by burning, contributing to the creation of electrical energy. Furthermore, exhaust heat generated during power generation can be used for drying the precursor carbide. On the other hand, the latter high-temperature dry distillation gas is used for reduction of the metal salt supported on the precursor carbide. This makes it possible to efficiently convert the precursor carbide into an adsorbent.

The dry distillation gas immediately after gasification has a high temperature, and the dry distillation gas has a large thermal energy. In the CS system 100, this thermal energy is also used to produce adsorbents. That is, it is used for drying the precursor carbide and accelerating the reduction of the metal salt.

CS system 100 includes at least one of the following means.
(1) Generation of carbonized material and carbonized gas by carbonization of biomass (2) Power generation using carbonized gas (3) Generation of metal-supported carbide (adsorbent) by metal fixation on carbonized material (4) Absorption of adsorbed material by metal-supported carbide Adsorption (5) Production of fertilizer from a metal-supported compound that has adsorbed an adsorbent (6) Injection of fertilizer into soil Below, each means will be described.

1-1. Generation of Carbide and Dry Distillation Gas by Carbonization of Biomass A part of the configuration for realizing the CS system 100 is shown in FIG. A means for carbonizing biomass 102 to produce char and carbonization gas includes gasifier 110 and heat exchanger 150 .

(1) Gasifier The gasifier 110 carbonizes the biomass 102 under conditions of low oxygen concentration to produce dry distillation gas and carbonized matter 104 . There are no particular restrictions on the structure of the gasifier 110 . FIG. 3 shows a schematic cross-sectional view of an internal combustion gasifier as the gasifier 110 . The gasifier 110 shown here is just an example, and as will be described later, the carbonization furnace may be an external heat type, and its structure may be a batch type closed coal kiln, a continuous rotary kiln, or an oscillating gasification furnace. , a screw furnace, a fixed bed furnace (downdraft, updraft), etc. may be used. Either type has a flow path for introducing dry distillation gas generated by carbonization to a reduction device 220 (described later).

As shown in FIG. 3, the gasifier 110 has a rotary gasifier 114 having a cylindrical shape and a heating chamber 112 equipped with burners 120 that supply thermal energy for carbonizing the biomass 102 . It is provided so as to cover the gasification furnace 114 . The gasifier 110 may be provided with a hopper 124 for charging the biomass 102 to be carbonized and a screw feeder 126 positioned below the hopper 124 . Biomass 102 is continuously fed into gasifier 114 by screw feeder 126 .

The gasification furnace 114 exemplified here is a rotary kiln type gasification furnace, and the gasification furnace 114 and the heating chamber 112 are arranged from a horizontal plane so that the side where the biomass 102 is introduced is higher than the side where the carbide 104 is carried out. Inclined. Gasifier 114 is configured to rotate within heating chamber 112 by drive 116 . The drive unit 116 rotates the gasification furnace 114 about the central axis of the heating chamber 112 using, for example, chains, belts, and gears. The biomass 102 supplied to the gasification furnace 114 is transported from the hopper 124 side to the burner 120 side by the continuous rotation of the gasification furnace 114 . During that time, the biomass 102 is heated under conditions of low oxygen concentration, carbonization proceeds, and dry distillation gas is generated. The carbonization gas is taken out from the exhaust duct 128 via the first gas supply pipe 118 . The first gas supply pipe 118 functions as a flow path for introducing the dry distillation gas into the reduction device 220 . The resulting carbide 104 is carried out of the gasifier 110 from the bottom of the gasification furnace 114 via a rotary valve 122 for preventing gas leakage, and is subjected to subsequent immersion. Depending on the situation, the rotary valve 122 may be installed in two stages, upper and lower. In this case, the upper and lower rotary valves are alternately opened to discharge the carbide. Also, a mechanism capable of cooling the rotary valve 122 may be provided around the rotary valve 122 .

In order to maintain the temperature of the dry distillation gas, the first gas supply pipe 118 may be covered with heat retaining means 130 such as heat insulating material. Alternatively, the first gas supply pipe 118 may be provided with a heating device (not shown in FIG. 2) for heating the dry distillation gas generated by the gasifier 110 or for maintaining the temperature.

As an optional configuration, a mechanism for supplying oxygen to the carbonized gas to be produced may be provided. FIG. 3 shows an example in which an inlet 134 for introducing oxygen or air for this function is provided in the exhaust duct 128 via a valve 132 . By adding a small amount of oxygen to the carbonization gas, the temperature of the gasifier 110 can be controlled, typically increased, and the tar contained in the carbonization gas is burned to reduce the concentration of tar in the carbonization gas. can do. In addition, if the oxygen supply amount is too large, the biomass 102 will be burned and the carbide cannot be obtained, so it is preferable to control the oxygen supply amount. Also, although not shown, a reformer may be connected to the first gas supply pipe 118 as a tar separator to remove tar by a steam reforming reaction.

As another example of the gasifier 110, an external combustion gasifier is shown in FIG. As shown in FIG. 4, the external combustion gasifier 110 basically has a gasification furnace 114 and a heating chamber 112 surrounding the gasification furnace 114 . Heating chamber 112 is provided so as to form a space with gasification furnace 114 , and heat medium inlet 144 and heat medium outlet 146 connected to this space are provided in heating chamber 112 . An externally heated heat medium is introduced into this space via the former, and the heat medium is discharged from the latter. Thereby, the heated heat medium comes into contact with the outer wall of the gasification furnace 114, and the gasification furnace 114 is heated. As the heat medium, gas heated by an electric heater or the like may be used, or high-temperature gas obtained by burning fuel such as light oil, heavy oil, or carbide may be used. Alternatively, dry distillation gas generated by gasification may be used. When using such an external combustion gasifier 110, although an energy source for heating the heat medium is required, the carbide 104 can be obtained with a relatively high yield.

As another example of the gasifier 110, a fixed-bed gasifier is shown in FIG. A gasification apparatus 110 shown in FIG. 5 has a continuous furnace type gasification furnace 114 , and a heater 121 for heating the gasification furnace 114 is provided around the gasification furnace 114 . A rotary valve 123 is provided above the gasification furnace 114 . Instead of the rotary valve 123, a screw feeder 126 (see FIGS. 3 and 4) may be provided. The introduction port 134 for introducing oxygen or air can be installed at any location, and is provided below the gasification furnace 114 in the example shown in FIG. The bottom of the gasifier 114 may be slanted (see dashed line in FIG. 5), and this structure allows the carbides 104 that form in the gasifier 114 to be collected at the bottom of the gasifier 114 .

Biomass 102 is introduced from hopper 124 into gasifier 114 , and oxygen or air is introduced into gasifier 114 from inlet 134 . The biomass 102 is carbonized by the heat from the heater 121 to produce dry distillation gas and porous carbonized matter 104 . A dry distillation gas is taken out from a first gas supply pipe 118 connected to the gasification furnace 114 and introduced into the heat exchanger 150 and/or the reduction device 220 . By using the gasifier 110 shown in FIG. 5, the tar content accompanying the carbonization gas can be reduced. If the inside of the gasification furnace 114 reaches a sufficient temperature during gasification, the heater 121 can be omitted.

(2) Heat Exchanger The heat exchanger 150 is connected to the first gas supply pipe 118 of the gasifier 110 and is provided to cool the high-temperature dry distillation gas and take out thermal energy. There are no restrictions on the type and structure of the heat exchanger 150, and various types such as plate type, shell-tube type, and fin-tube type can be applied. The heat exchanger 150 illustrated in FIG. 6 is a shell-and-tube heat exchanger. The heat exchanger 150 has an outer shell 152, and the outer shell 152 is provided with an inlet 154 and an outlet 156 for introducing and discharging the dry distillation gas, respectively. A flow path for the carbonization gas is formed in the outer shell 152 and connected to an inlet 154 and an outlet 156 . Fins 158 may be provided within the outer shell 152 to allow the heat transfer medium to efficiently contact the flow path.

The heat transfer medium may be gas such as air or nitrogen, water, alcohol such as ethylene glycol, silicone oil, or aromatic compound such as biphenyl or diphenyl ether. These heat transfer media are injected into the outer shell 152, heat exchanged with the dry distillation gas by contact with the flow path, are heated, and then taken out to the outside. When the heat transfer medium is gas such as air or nitrogen, the heat transfer medium heated by heat exchange can be introduced directly into the chamber 202 of the drying device 200 or the reduction furnace 222 of the reduction device 220 (described later). On the other hand, when the heat transfer medium is liquid, it is supplied to the drying device 200 and the reduction device 220 so as to circulate inside the tube heater 216 provided around the chamber 202 . When the heat transfer medium is a liquid, the heat exchanged liquid heat transfer medium is again heat-exchanged with a gas such as air or nitrogen in a heat exchanger different from the heat exchanger 150, and the heated gas is sent to the drying device. It can be introduced into the chamber 202 of 200 or the reduction furnace 222 of the reduction device 220 .

1-2. Power Generation Using Dry Distillation Gas As described above, in the CS system 100, the combustibility of the dry distillation gas is used to generate electrical energy. A means for generating electricity from the carbonized gas includes a power generator 170 (FIG. 2). There are no restrictions on the structure and type of the power generator 170, and a gas turbine type, gas engine type, or dual fuel engine type power generator can be used as appropriate. For example, in the case of a gas engine system, as shown in the block diagram of FIG. The generator 170 is configured by the generator 176 and the like. Electrical energy is output from transformer 176 . Optionally, the power plant 170 may include a cooler 178 for cooling the gas engine 172 to obtain thermal energy produced by the gas engine 172 . The heat energy obtained by the cooler 178 can be supplied to the drying device 200 or the reducing device 220 through a gaseous or liquid heat transfer medium. Although not shown, a compression device for compressing the dry distillation gas and supplying it to the gas engine 172 may be provided. Although the configuration in which the gas engine 172 and the generator 174 are separated has been described here, the power generator 170 may have a configuration in which the generator and the gas engine are integrated.

The means for generating electricity using the carbonized gas may further include a gas purifier 160, a gas holder 166, a heat exchanger 168, etc. (FIG. 2). There are no restrictions on the configuration of the gas purifier 160, and for example, it can include a steam concentrator 162, a dust filter 164, a scrubber (not shown), a desulfurizer, and the like. By appropriately providing these structures, ammonia, hydrogen cyanide, hydrochloric acid, dioxin, sulfur oxides, nitrogen oxides, hydrogen sulfide, dust, etc. contained in the dry distillation gas are removed. The gas holder 166 can be provided to store the dry distillation gas, and is configured using a variable volume type or constant volume type gas holder. The type and capacity of the gas holder 166 are appropriately selected according to the scale of the CS system 100 . The heat exchanger 168 has a function of cooling the dry distillation gas supplied to the power generator 170, and its structure can also be arbitrarily selected. For example, heat exchanger 168 may have the same or similar structure as heat exchanger 150 .

Flare stack 270 is provided to burn excess carbonization gas introduced into reduction device 220 . In the present system 100, the surplus dry distillation gas supplied to the reduction device 220 may be introduced into the power generation device 170 via the heat exchanger 168 and combusted to be reused for power generation (see FIG. 2). Since the dry distillation gas used for the reduction reaction of the metal salt accounts for several percent of the total, the excess dry distillation gas is introduced into the power generation device 170 via the heat exchanger 168 to efficiently use the thermal energy of the dry distillation gas. be able to. Furthermore, since the temperature of the gas discharged from the reduction device 220 is lowered, the load on the heat exchanger 168 can be reduced and the size of the heat exchanger 168 can be reduced.

1-3. Formation of Metal-Supported Carbide (Adsorbent) by Fixing Metal on Carbide In the CS system 100, a metal is fixed to the carbide produced by carbonization, thereby imparting the function of adsorbing compounds containing phosphorus and nitrogen to the carbide. Fixing of the metal is performed by allowing the carbide to adsorb the metal salt and reducing the supported metal salt to the metal. In the CS system 100, the reducing power and thermal energy of the dry distillation gas are used for reduction. The means for producing the sorbent includes a soaking device 180 and a reducing device 220, optionally further including a drying device 200 and a reducing gas source 250 (FIG. 2).

(1) Immersion Device The immersion device 180 has a function of causing the carbide 104 obtained by carbonization to adsorb a metal salt. There are no restrictions on the structure of the immersion device 180, and basically a tank 182 for storing a suspension or solution containing a metal salt used for immersion (hereinafter collectively referred to as a liquid containing a metal salt or an immersion liquid). (Fig. 8). A discharge port may be provided at the bottom of the tank 182, and the immersion liquid can be stored and discharged by opening and closing a valve 190 connected to the discharge port. Optionally, the tank 182 may further comprise an agitator 192 and a heater 196 for heating the immersion liquid. The immersion liquid is stirred by using the stirring device 192, and the concentration distribution of the metal salt in the immersion liquid can be reduced. Agitation of the immersion liquid may be performed by circulating the immersion liquid. The heater 196 has a heating element inside, and may be configured to be electrically heated, or has a tubular structure, and heat is supplied from the heat exchanger 150, 168, or the cooler 178 inside. The heat transfer medium may be configured to circulate. This makes it possible to effectively utilize the thermal energy of the dry distillation gas.

The immersion device 180 may further include a lid 184 having one or more through holes 186 therein. The through-hole 186 includes, for example, a gas source for introducing gas such as nitrogen, argon, and air, a decompression device for evacuating the inside of the tank 182, a pressurization device for pressurizing the inside of the tank 182, and a A pressure gauge, a thermometer, or the like for measuring pressure or temperature may be connected. Although not shown, the immersion device 180 may further include a cooling device for cooling the immersion liquid, an ultrasonic irradiation device, and the like. By irradiating the immersion liquid with ultrasonic waves from the ultrasonic irradiation device during immersion, the immersion liquid can be efficiently permeated into the pores of the carbide 104 .

Since the carbide 104 has a lower specific gravity than water, it floats on the immersion liquid. Therefore, a case 194 that can be accommodated in the tank 182 may be used in combination with the immersion device 180 . The case 194 is provided with a plurality of openings and is constructed of material and structure such that it has a higher specific gravity than the immersion liquid. The plurality of openings are set so that the mesh size is smaller than that of the carbide 104 . This not only prevents the carbides 104 from floating on the immersion liquid and making it impossible to sufficiently contact the immersion liquid, but also allows the immersed carbides 104 to be easily recovered, and furthermore, the carbides 104 can be removed from the case 194 . can be prevented from leaking out. Separation of the carbide 104 and the immersion liquid is performed by a dehydrator or the like installed after the immersion device 180 . As the dehydrator, for example, a conventionally known dehydrator such as a centrifugal dehydrator can be appropriately used.

(2) Drying Device The drying device 200 is a device having a function of drying the precursor carbide 106, and its structure is not restricted. For example, as shown in FIG. 9, the drying apparatus 200 includes a chamber 202 containing the precursor carbide 106 , and the chamber 202 is provided with one or more gas inlets 206 and gas outlets 210 .

The drying of the precursor carbide 106 may utilize the thermal energy of the dry distillation gas. In this case, the gas supply port 206 is connected to the heat exchanger 150 and/or the heat exchanger 168 to introduce a gaseous heat transfer medium heated by the dry distillation gas into the chamber 202 . The heat transfer medium flow rate is controlled using valve 208 . Alternatively, a tube heater 216 for circulating a separately heated heat transfer medium or a heat transfer medium supplied from the heat exchangers 150, 168 or the like may be provided outside or inside the chamber 202. FIG. FIG. 9 shows an example in which the tube heater 216 is installed outside the chamber 202 . In this case, in the heat exchangers 150 and 168, not only a gaseous heat transfer medium but also a liquid heat transfer medium can be used. As a result, the thermal energy of the high-temperature dry distillation gas generated in the gasification device 110 can be supplied to the drying device 200, contributing to a reduction in the manufacturing cost of the adsorbent. The CS system 100 may be configured to supply the heat energy obtained by the cooler 178 to the drying device 200 via a heat transfer medium.

Optionally, the drying apparatus 200 may include a separator 214 to prevent contact between the bottom of the chamber 202 and the precursor charcoal 106, a lid 204, or a drain (not shown). One or more through holes 212 may be provided in the lid 204 . For example, a thermometer or a pressure gauge may be installed in the through-hole 212 , and a decompression device for promoting drying may be connected to the chamber 202 through the through-hole 212 .

(3) Reduction Device The reduction device 220 has a function of reducing the metal salt supported on the precursor carbide 106 to metal. The structure of the reduction device 220 is also not particularly limited, and for example, a continuous furnace structure schematically shown in FIG. 10 can be adopted. The reduction apparatus 220 shown here includes a reduction furnace 222, a heater 228 for heating the reduction furnace 222, and a first gas supply pipe for introducing the dry distillation gas supplied from the gasifier 110 into the reduction furnace 222. 118, as well as a valve 234 for controlling the flow of reducing gas. The first gas supply pipe 118 may be directly extended from the gasifier 110 and connected to the reduction furnace 222, or the gasifier 110 and the reduction furnace 222 may be connected via another gas supply pipe. good. By connecting the reducing furnace 222 and the gasifier 110 through the first gas supply pipe 118, the thermal energy and reducing power of the high-temperature dry distillation gas generated in the gasifier 110 are provided to the reducing device 220. , and the reduction reaction in the reduction furnace 222 can be accelerated. As an optional configuration, a heater 246 for heating the dry distillation gas may be provided so as to cover the first gas supply pipe 118 .

The reducing furnace 222 may be provided with a rotary valve 226 and a hopper 224 for charging the precursor carbide 106 . A rotary valve 230 can be provided at the bottom of the reduction furnace 222 for removing the resulting adsorbent. Also, each of the rotary valves 226, 230 may be configured with two rotary valves to have a two-stage configuration. By providing the two rotary valves 226 and 230, it is possible to prevent leakage of the dry distillation gas introduced into the reducing furnace 222, and to reduce the metal salt safely. Moreover, by installing these, the precursor carbide 106 can be continuously put into the reduction furnace 222 and the adsorbent obtained by the reduction can be taken out. The bottom of the reduction furnace 222 may be slanted (see dashed line in FIG. 10) and this structure allows the adsorbent to collect at the bottom of the reduction furnace 222 . The reducing furnace 222 is further provided with a gas collecting pipe 244 , and the dry distillation gas that has reacted with the precursor carbide 106 or excess dry distillation gas is discharged through the gas collecting pipe 244 .

The reducing device 220 may further have a second gas supply pipe 240 for separately supplying reducing gas. A reducing gas source 250 is connected to the second gas supply pipe 240 ( FIG. 2 ), and the flow rate of the reducing gas is controlled by a valve 242 . As a result, for example, when the amount of reducing gas generated in the gasifier 110 is insufficient, or even when the gasifier 110 is not in operation, a sufficient amount of reducing gas is supplied into the reducing device 220 to produce precursors. A reduction treatment can be performed on the carbide 106 . The reducing gas supplied from the reducing gas source 250 may be hydrogen, carbon monoxide, alkane, or a mixture thereof. Alternatively, the reducing gas may be mixed with an inert gas such as nitrogen or argon. Alternatively, the precursor carbide 106 may be heat treated in an oxygen-free or inert gas atmosphere. Due to the heat treatment, carbon, oxygen, hydrogen, or sulfur contained in the precursor carbide 106 reacts to form a reducing gas. The reducing gas reduces the precursor carbide 106 .

The reduction device 220 may further include a third gas supply pipe 236 connected to a gas replacement device (not shown) for replacing the atmosphere (gas) in the reduction furnace 222 . Since the dry distillation gas contains combustible gases such as hydrogen and alkanes and toxic gases such as carbon monoxide, air, nitrogen, or rare gas ( Helium, argon, etc.) can be supplied to discharge the residual dry distillation gas from the reduction furnace 222 . A gas source (not shown) such as air, nitrogen, or argon is connected to the gas replacement device. Alternatively, the gas replacement device may be a fan or compressor for introducing outside air. Furthermore, the first gas supply pipe 118, the second gas supply pipe 240, and the third gas supply pipe 236 are not connected to the reduction furnace 222 independently, but are connected to the reduction furnace 222 as a single supply pipe. I don't mind. In this case, these gas supply pipes are connected outside the reduction furnace 222, and the supply of these gases is controlled by switching valves.

Although not shown, the CS system 100 is provided outside the reducing furnace 222 to heat the reducing furnace 222 by providing a tube heater for circulating the heat transfer medium supplied from the heat exchanger 150 or the like, similar to the drying apparatus 200. may be configured. This also makes it possible to utilize the thermal energy of the dry distillation gas for the reduction of the precursor carbide 106 via the heat transfer medium.

The reductor 220 need not be continuous and may be batchwise. For example, as shown in FIG. 11, instead of the rotary valve 226, an opening/closing door 223 is provided at the opening of the reducing furnace 222. Using this, the precursor carbide 106 is introduced into the reducing furnace 222, and the generated adsorbent is taken out. good too. Although not shown, a plurality of openings may be provided, and the charging of the precursor carbide 106 and the taking out of the adsorbent may be performed via different openings. Further, in the example shown in FIG. 11, the reducing apparatus 220 is configured such that the precursor carbide 106 is introduced from above the reducing furnace 222 through the opening. Device 220 may be configured.

Alternatively, as shown in FIG. 12, the reduction device 220 may be a rotary kiln type reduction device. That is, the reduction apparatus 220 includes a rotary reducing furnace 222 having a cylindrical shape and a heating chamber 221 covering the reducing furnace 222, and the reducing furnace 222 may be configured to rotate within the heating chamber 221 by a drive unit 232. good. The temperature inside the reduction furnace 222 is controlled by a burner 231 provided in the heating chamber 221 . The dry distillation gas is supplied from the gasification furnace 114 through the first gas supply pipe 118 . The reductor 220 may also be configured to receive a supply of reducing gas from a reducing gas source 250 . The heating chamber 221 is provided with a gas collection tube 244 through which gas generated after the precursor carbide 106 reacts with the dry distillation gas or excess dry distillation gas is discharged.

The precursor carbide 106 supplied to the reducing furnace 222 through the screw feeder 225 is transported from the hopper 224 side to the burner 231 side by the continuous rotation of the reducing furnace 222 . In the atmosphere of the dry distillation gas, the precursor carbide 106 is heated by the heat of the burner 231, thereby reducing the metal salt supported on the precursor carbide 106 and generating an adsorbent.

Alternatively, as shown in FIG. 13, an external combustion reducing device 220 can be used. The external combustion type reduction device 220 shown in FIG. 13 has a reduction furnace 222 rotated by a drive unit 232 and a heating chamber 221 covering it. A space is formed between the reduction furnace 222 and the heating chamber 221 , and a heat medium inlet 227 and a heat medium outlet 229 are provided in the space in the heating chamber 221 . The heating of the reducing furnace 222 may be performed in the same manner as the external combustion gasifier 110 described above, or alternatively, the dry distillation gas may be introduced inside the reducing furnace 222 and between the heating chamber 221 and the reducing furnace 222. good too. In the latter case, the dry distillation gas is introduced from the first gas supply pipe 118 and/or the heat medium inlet 227, respectively.

As will be described later, in the system 100, the dry distillation gas that has been used for reduction processing in the reduction device 220 can be introduced into the power generation device 170 to generate power. In order to generate power using the gas, it is necessary to cool the dry distillation gas to about 50° C. in the heat exchanger 168 . Since the temperature of the dry distillation gas introduced between the heating chamber 221 and the reduction furnace 222 is lowered, by introducing the gas discharged from the heat medium discharge port 229 into the heat exchanger 168, the heat exchanger 168 This is preferable because it can reduce the load on That is, one of the advantages of the system 100 is that the reduction device 220 can be used like a heat exchanger.

Note that drying and reduction of precursor carbide 106 may be performed in reduction device 220 without providing drying device 200 in CS system 100 .

Thus, in the CS system 100, the thermal energy and reducing power of the dry distillation gas are effectively used to generate the adsorbent. This contributes to low cost manufacture of the adsorbent.

1-4. Adsorption of Adsorbent by Metal-Supported Carbide The means for adsorbing an adsorbate by metal-supported carbide, ie, an adsorbent, is not limited, but one example is a cartridge 260 that can be filled with an adsorbent. A cartridge 260 shown in FIG. 14A has a housing 262 that can be filled with the adsorbent 108, and the housing 262 is connected to an inlet 264 and an outlet 266 that connect the space inside the housing 262 to the outside. . Water containing adsorbents (hereinafter referred to as treated water) is injected from the inlet 264 using a pump (not shown) or the like. In this process, the treated water comes into contact with the adsorbent 108, and the adsorbent is adsorbed by the metal fixed to the adsorbent 108. Although not shown, filters may be provided between housing 262 and inlet 264 and between housing 262 and outlet 266 . This can prevent contamination by foreign matter and outflow of the adsorbent 108 .

The treated water may be prepared by dissolving the adsorbent in water, but water existing in rivers, lakes, or seas, water in septic tanks, and water subjected to advanced treatment at sewage treatment plants can be used as treated water. can be used. These treated waters may be injected from the inlet 264, and the cartridge 260 may be installed in rivers, lakes, the sea, septic tanks, and advanced treatment tanks. In this case, as shown in FIG. 14B, a cartridge 260 having a mesh-like housing 262 may be used. Although the size of the mesh is not limited to the following, it is preferably 0.1 mm or more and 50 mm or less, more preferably 0.5 mm or more and 20 mm or less. The inlet 264 and the outlet 266 may not be provided in the mesh-like housing 262 . Since the adsorbent 108 has a lower specific gravity than water, if the housing 262 does not have sufficient weight, a weight 268 may be connected to the housing 262 for securely placing the housing 262 in the treated water. Although not shown, instead of the weight 268, the housing 262 may be provided with an anchor for fixing to the river bottom, lake bottom, septic tank, or advanced treatment tank. By filling the cartridge 260 with the adsorbent and bringing the treated water into contact with the adsorbent, the adsorbent can be easily handled and the adsorption treatment can be performed continuously.

Rivers, lakes, and seas contain various substances that cause water pollution, and typical examples thereof are compounds containing phosphorus and nitrogen. Since the adsorbent produced by the CS system 100 has a high adsorption capacity for these compounds, it is possible to effectively remove water pollutants from water in rivers, lakes, seas, septic tanks, and advanced treatment tanks. can be done. Therefore, the CS system 100 can contribute to environmental conservation through water quality improvement.

1-5. Production of Fertilizers from Metal-Supported Compounds with Adsorbed Adsorbents Compounds containing phosphorus and nitrogen, which are adsorbents, can act as nutrients to promote the growth of a variety of plants. Can be used as fertilizer. In order to effectively exhibit the function as a fertilizer, pulverizers and mixers are used as means for producing fertilizer from this adsorbent.

There are no restrictions on the structure or type of crusher, and examples include crushers such as vibration mills, jet mills, ball mills, roller mills, rod mills, hammer mills, impact mills, rotary mills, pin mills, pin-disk mills, and planetary mills. . Crushing the adsorbent with a crusher increases the surface area, thereby promoting the dissociation of the adsorbent from the adsorbent.

The means for producing fertilizer from the sorbent may further comprise a classifier for matching the particle size of the crushed sorbent to the fertilizer application. There are no restrictions on the structure or type of the classifier, and either a dry classifier or a wet classifier may be employed. Classifiers include airflow classifiers, gravity field classifiers, inertial force field classifiers, centrifugal force field classifiers, and the like.

The means for producing fertilizer may further include a mixer for mixing with other fertilizer ingredients. There are no restrictions on the structure or type of mixer, and a free-fall mixer, forced mixer, Y-branch mixer, agitator mixer, paddle mixer, or the like can be arbitrarily selected.

1-6. Putting Fertilizer into the Soil There are no restrictions on the means of putting the fertilizer into the soil. Also, there is no restriction on the application method, and either a row-type spreader or a full-surface application spreader may be employed. Fertilizer is preferably spread within 30 cm from the surface of the soil.

As described above, in the CS system 100 of the present embodiment, carbon dioxide in the atmosphere is fixed by photosynthesis of plants to form organic substances, and biomass generated by their utilization and metabolism is carbonized. Carbonization converts most of the organic matter into carbide, ie carbon. Since this char is eventually returned to the ground, carbon dioxide is stored in the ground as carbon. Through this series of processes, the CS system 100 contributes to the reduction of carbon dioxide in the atmosphere.

Furthermore, since carbonized matter can be used as an adsorbent capable of adsorbing water pollutants, the CS system 100 is a system that contributes to environmental conservation through water quality improvement. Also, electrical energy is created from the dry distillation gas produced by the carbonization of the biomass during the production of the adsorbent. Therefore, it can be said that this CS system 100 simultaneously contributes to the creation of renewable energy. In addition, the adsorbent that adsorbs water pollutants also functions as a fertilizer for promoting the growth of plants in the ground, so the CS system 100 is a system that can contribute to the development of agriculture and forestry.

2. Method for Manufacturing Adsorbent in CS System In this section, a method for manufacturing an adsorbent in the CS system 100 will be specifically described.

2-1. Carbonization First, biomass 102 is placed in gasifier 110 using hopper 124 and screw feeder 126 (FIGS. 3, 4, and 5). In the gasifier 114, the burner 120 or a heated heat medium is used to heat the gasifier 114 in the absence of oxygen or in the presence of a low concentration of oxygen. The oxygen concentration may be 1% or less, and the heating temperature is appropriately selected within the range of 400°C to 1300°C. Oxygen may be introduced from the inlet 134 as needed. By carbonization, the carbide 104 is produced as a porous material in which pores of various sizes are formed in which pores due to the structure of the biomass 102 and pores generated by desorption of the dry distillation gas are intricately mixed. At the same time, hot (700° C. to 1300° C.) carbonization gas is produced. All or part of the dry distillation gas is introduced into the heat exchanger 150, cooled, and supplied to the power generator 170 via the gas purifier 160 and the like (see FIG. 2). This creates electrical energy. It should be noted that the heat generated in the heat exchangers 150, 168 may be used to dry the biomass 102 prior to carbonization of the biomass 102. This allows the biomass 102 to be carbonized with less energy in the gasifier 110 . The biomass used in this batch is hereinafter referred to as first biomass 102-1.

2-2. Soaking and Drying The carbide 104 obtained by carbonizing the first biomass 102-1 is subjected to a soaking treatment in the soaking device 180. FIG. Metal salts contained in the immersion liquid include sulfates, nitrates, and hydrochlorides of iron, nickel, cobalt, vanadium, manganese, magnesium, and calcium. Sulfates, nitrates and hydrochlorides of are preferred. Specific examples include ferrous sulfate, ferric sulfate, ferrous nitrate, ferric nitrate, ferrous chloride, and ferric chloride. Also, a polyferric sulfate solution can be used. The concentration of the metal salt in the immersion liquid can be, for example, 1% or more and 80% or less by weight, or 15% or more and 60% or less by weight. As a solvent for the immersion liquid, water and alcohol can be used, but water is preferable because it is low in toxicity, non-flammable and inexpensive. The temperature of the immersion liquid during immersion may be adjusted to 0°C to 150°C, 0°C to 100°C, 0°C to 90°C, or 0°C to 70°C. Note that the immersion liquid may be replaced for each batch, or may be replaced for each of a plurality of batches. That is, the dipping liquid may be reused in multiple batches.

The immersion may be performed after cooling the carbide 104 to room temperature, or may be performed while the temperature is high. For example, the immersion temperature is preferably 0° C. to 150° C., 0° C. to 100° C., 0° C. to 90° C., or 0° C. to 70° C. The immersion time can be selected arbitrarily, and is preferably 1 minute or more. The immersion may be performed while applying ultrasonic waves to the immersion liquid. The immersion may be carried out under normal pressure, or may be carried out while reducing pressure or pressure, or may be carried out after pressure reduction, followed by immersion. For example, the pressure in the chamber 202 is -0.1 MPa or more and 0.9 MPa or less, -0.1 MPa or more and 0.4 MPa or less, or -0.1 MPa or more and 0.1 MPa or less in gauge pressure (pressure difference with respect to atmospheric pressure). do it. Moreover, when pressurizing after decompression, it can be carried out at a gauge pressure of 0 MPa or more and 0.9 MPa or less, or 0 MPa or more and 0.4 MPa or less as a gauge pressure with the atmospheric pressure being zero. By the above process, the metal salt is adsorbed on the pore walls and surface of the carbide 104, and the precursor carbide 106 is obtained.

By repeating the immersion of the carbide 104, the metal salt concentration gradually decreases. Therefore, the immersion liquid after immersion may be concentrated. At this time, the heat transfer medium supplied from the heat exchangers 150 and 168 may be used as the heat energy required for concentration. In this case, for example, the biomass (second biomass) 102-2 is carbonized in a different batch than the carbonization of the first biomass 102-1. The thermal energy of the dry distillation gas (second dry distillation gas) generated by the carbonization of the second biomass 102-2 is used to heat the heat transfer medium in the heat exchanger 150, and the heated heat transfer medium is transferred to the heater 196. The immersion liquid is heated and concentrated by circulating it to

Precursor carbide 106 is then dried using drying apparatus 200 . Drying may be performed at room temperature, but the chamber 202 may be set to an arbitrary temperature. For example, heating to a temperature selected from the range of 50° C. to 250° C. or 60° C. to 200° C. may be used. When heating, external energy may be used, or the heat transfer medium heated by the second dry distillation gas in the heat exchanger 150 may be circulated through the tube heater 216 . Thereby, the thermal energy of the second dry distillation gas can be efficiently used.

2-3. Reduction The dried precursor carbide 106 is subjected to a reduction treatment in a reduction device 220 to reduce the metal salt to metal to obtain an adsorbent. Reduction is performed by heating the reduction furnace 222 using the heater 228 and supplying a reducing gas. At this time, part of the dry distillation gas generated in the gasifier 110 can be used. Specifically, the valve 234 is opened to introduce the second dry distillation gas into the reduction furnace 222 from the first gas supply pipe 118 . At this time, the heat energy of the heat transfer medium obtained by the heat exchangers 150 and 168 may be used to heat the reduction furnace 222 . The introduction amount of the dry distillation gas and the heater 228 are adjusted so that the temperature of the reduction furnace 222 is 200° C. or higher and 1200° C. or lower, 400° C. or higher and 1200° C. or lower, or 600° C. or higher and 900° C. or lower. If the amount of the dry distillation gas is insufficient, the reducing gas may be separately introduced from the reducing gas source 250 .

Reduction can be monitored and controlled using the concentration of reducing gas in the exhaust gas from gas collection tube 244 . Specifically, when the concentration of the reducing gas in the exhaust gas is low, it may be determined that it is necessary to increase the introduction amount of the dry distillation gas or to introduce the reducing gas from the reducing gas source 250 . Alternatively, it may be determined that the reduction is completed when the concentration of the reducing gas becomes constant. By this reduction treatment, at least part of the metal salt in the precursor carbide 106 is reduced to become a zero-valent metal, and an adsorbent is obtained.

When the precursor carbide 106 is dried using the reduction device 220 , an inert gas is introduced into the reduction furnace 222 to dry the precursor carbide 106 . Alternatively, the screw feeder 225 side of the reducing furnace 222 may be the drying area and the burner 231 side may be the reducing area, and the drying process and the reducing process may be performed simultaneously in the reducing device 220 . Furthermore, two reducing devices 220 may be connected in series, one reducing device 220 performing the drying process, and the other reducing device 220 performing the reducing process.

When the precursor carbide 106 is reduced in an inert gas atmosphere or an atmosphere with a low oxygen concentration, the counter ion of the metal salt in the precursor carbide 106 reacts with the carbon constituting the precursor carbide 106 by heating. As a result, carbon monoxide or hydrogen is produced. For example, in the case of precursor carbide 106 containing iron sulfate, sulfurous acid gas generated by heating reacts with carbon in precursor carbide 106 to produce carbon monoxide and sulfur trioxide. Alternatively, the oxygen and carbon in the precursor carbide 106 react to form carbon monoxide. Alternatively, the water contained in the precursor carbide 106 is thermally decomposed to produce methane and hydrogen. Carbon monoxide, sulfur dioxide, sulfur trioxide, methane, or hydrogen may be used to reduce the precursor carbide 106 . However, if the precursor carbide 106 is reduced in the presence of sulfur oxide gas, by-products may be generated. The reduction treatment may be performed after replacing the inside of the furnace 222 with an inert gas.

3. Water Quality Improvement Method Using CS System In this section, a water quality improvement method in the CS system 100 will be described. Water quality improvement may be performed by filling the housing 262 of the cartridge 260 with an adsorbent and injecting treated water from the inlet 264 or immersing the treated water in the treated water. In the former case, it is preferable to pour the treated water through a filter to remove foreign matters. The total phosphorus concentration in the treated water is preferably 0.1 mg/L or more and 5000 mg/L or less. The total phosphorus concentration is an index indicating the total amount of compounds containing phosphorus contained in the treated water, and can be measured by the potassium peroxodisulfate decomposition method, the nitric acid-perchloric acid decomposition method, or the nitric acid-sulfuric acid decomposition method. can. There is no particular need to control the temperature of the treated water when the treated water is brought into contact with the adsorbent. Also, the treatment time may be appropriately set according to the concentration of the adsorbent in the treated water.

4. Fertilizer Production Method Using CS System In this section, a fertilizer production method in the CS system 100 will be described. An example of a method for producing fertilizer is shown in the flow chart of FIG. First, an adsorbent is produced according to the method described above, and an adsorbent is adsorbed. After that, pulverization is performed according to the application of the fertilizer. For example, the adsorbent may be pulverized so that the average particle size is 10 mm or less, 1 mm or more and 10 mm or less. Classification may be performed as necessary.

The pulverized adsorbent may be appropriately mixed with other fertilizer components. Fertilizer components include one or more selected from nitrogen, potassium, calcium, magnesium, manganese, silicic acid, and boron, and specific materials include oil cake, fragrant chicken manure, fish meal, bone meal, rice bran, bat guano, and pokashi. Fertilizer, plant ash, lime, chemical fertilizers and the like are exemplified. A fertilizer can be manufactured by the above process.

As described above, in the CS system 100, the reducing power and thermal energy of the dry distillation gas are used to produce the adsorbent, and the adsorbent adsorbs the adsorbent to produce fertilizer. Thus, CS system 100 can provide fertilizer at low cost.

Each of the embodiments described above as embodiments of the present invention can be implemented in combination as appropriate as long as they do not contradict each other. Appropriate additions, deletions, or design changes made by those skilled in the art based on each embodiment are also included in the scope of the present invention as long as they have the gist of the present invention.

Even if there are other actions and effects different from the actions and effects brought about by each of the above-described embodiments, those that are obvious from the description of the present specification or those that can be easily predicted by those skilled in the art are of course the present invention. is understood to be brought about by

100: CS system, 102: biomass, 102-1: first biomass, 102-2: second biomass, 104: carbide, 106: precursor carbide, 108: adsorbent, 110: gasifier, 112: heating chamber, 114: gasification furnace, 116: drive unit, 118: first gas supply pipe, 120: burner, 121: heater, 122: rotary valve, 123: rotary valve, 124: hopper, 126: screw feeder, 128: exhaust duct, 130: heat retaining means, 132: valve, 134: inlet, 144: heat medium inlet, 146: heat medium outlet, 150: heat exchanger, 152: outer shell, 154: inlet, 156: Outlet, 158: Fins, 160: Gas purifier, 162: Water vapor concentrator, 164: Dust filter, 166: Gas holder, 168: Heat exchanger, 170: Power generator, 172: Gas engine, 174: Generator, 176: Transformer, 178: Cooler, 180: Immersion device, 182: Tank, 184: Lid, 186: Through hole, 190: Valve, 192: Stirring device, 194: Case, 196: Heater, 200: Drying device, 202: Chamber, 204: Lid, 206: Gas supply port, 208: Valve, 210: Gas outlet, 212: Through hole, 214: Separator, 216: Tube heater, 220: Reduction device, 221: Heating chamber, 222: Reduction furnace , 223: Open/close door, 224: Hopper, 225: Screw feeder, 226: Rotary valve, 227: Heat medium inlet, 228: Heater, 229: Heat medium outlet, 230: Rotary valve, 231: Burner, 232: Drive Section, 234: Valve, 236: Third Gas Supply Pipe, 240: Second Gas Supply Pipe, 242: Valve, 244: Gas Collection Pipe, 246: Heater, 250: Reducing Gas Source, 260: Cartridge, 262: housing, 264: inlet, 266: outlet, 268: weight, 270: flare stack

Claims (23)

a first means for carbonizing biomass to produce a carbonized product and a carbonization gas, comprising a gasifier comprising a carbonization furnace ;
A second means for generating electricity using the dry distillation gas,
a third means for fixing a metal on said carbide, comprising an immersion device for adsorbing a metal salt on said carbide and a reducing device for reducing said adsorbed metal salt to metal;
a fourth means for causing the metal-immobilized carbide to adsorb at least one compound containing phosphorus, and a fifth means for producing a fertilizer from the carbide to which the compound is adsorbed,
The reduction device is a system for storing carbon dioxide, wherein the carbon dioxide gas is introduced from the gasification device . 2. The system of claim 1, further comprising sixth means for applying said fertilizer to soil. 2. The system of claim 1, wherein the biomass is a material comprising lignocellulose. 2. The system of claim 1, wherein said second means includes a gas engine and a generator connected to said gas engine. 2. The system of claim 1, wherein said fifth means includes a crusher. 6. The system of Claim 5, wherein said fifth means further comprises a mixer. carbonizing biomass to produce char and carbonization gas;
immersing the carbide in a liquid containing a metal salt;
reducing the metal salt adsorbed on the carbide to produce a metal-supported carbide; and immersing the metal-supported carbide in water containing at least one compound containing phosphorus;
The method of improving water quality , wherein the reduction includes contacting the carbonized material with the dry distillation gas . 8. The method of claim 7 , wherein said biomass is a material comprising lignocellulose. 8. The method according to claim 7 , wherein said metal salt is a metal salt selected from iron, aluminum, magnesium and calcium. 8. The method of claim 7 , wherein the metal salt is an iron salt. 8. The method of claim 7 , wherein the total phosphorus concentration of the phosphorus compounds in the water is 0.1 mg/L or more and 5000 mg/L or less. 8. The method of claim 7 , further comprising drying the char soaked in the liquid at a temperature between 30[deg.]C and 200[deg.]C. further comprising drying the carbide immersed in the liquid at a temperature of 30° C. or more and 200° C. or less;
11. The method according to claim 10, wherein said drying is performed using thermal energy of said carbonization gas. carbonizing biomass to produce char and carbonization gas;
immersing the carbide in a liquid containing a metal salt;
reducing the metal salt adsorbed on the carbide to produce a metal-supported carbide; and immersing the metal-supported carbide in water containing at least one compound containing phosphorus;
The method of producing a fertilizer , wherein the reduction includes contacting the carbonized material with the carbonization gas . 15. The method of claim 14 , further comprising cracking the water-soaked char. 15. The method of claim 14 , wherein said biomass is a material comprising lignocellulose. 15. The method of claim 14 , wherein the metal salt is a metal salt selected from iron, aluminum, magnesium, calcium. 15. The method of claim 14 , wherein said metal salt is an iron salt. 15. The method of claim 14 , wherein the total phosphorus concentration of phosphorus compounds in the water is 0.1 mg/L or more and 5000 mg/L or less. 15. The method of claim 14 , further comprising drying the char soaked in the liquid at a temperature between 0<0>C and 100<0>C. further comprising drying the carbide immersed in the liquid at a temperature of 30° C. or more and 200° C. or less;
15. The method according to claim 14 , wherein said drying is performed using thermal energy of said carbonization gas. 16. The method according to claim 15 , wherein the crushing is performed so that the average particle size of the carbide is 1 mm or more and 10 mm or less. 15. The method of claim 14 , further comprising mixing said carbide with a material containing elements selected from nitrogen, potassium, calcium, magnesium, manganese, silicic acid, and boron.

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