Biomass solid fuel production system

Abstract

This disclosure describes a biomass solid fuel production system that enables efficient operation. [Solution] The biomass solid fuel production system comprises a fuel production facility for producing biomass solid fuel from biomass raw materials and a clinker production facility. The fuel production facility includes a heating device that heats biomass raw materials to produce biomass solid fuel, a combustion furnace that burns the pyrolysis gas generated by heating the biomass raw materials in the heating device to produce combustion gas, a first flow path, and a second flow path. The clinker production facility includes a raw material preparation unit that dries cement raw materials and a clinker production unit that generates clinker from the cement raw materials dried by the raw material preparation unit by burning fuel. The first flow path introduces high-temperature combustion gas discharged from the combustion furnace into the clinker production unit. The second flow path introduces low-temperature combustion gas discharged from the heating device after heating the biomass raw materials into the raw material preparation unit.

Description

Technical Field

[0001] The present disclosure relates to a manufacturing system for biomass solid fuel.

Background Art

[0002] Patent Document 1 discloses a manufacturing apparatus for biomass solid fuel (PBT (registered trademark): Pelletizing Before Torrefaction). The apparatus of Patent Document 1 includes an externally heated rotary kiln and a combustion furnace. The rotary kiln is configured to heat (low-temperature carbonize) a pellet-shaped biomass molded body (WP: White Pellet) input as a raw material to produce biomass solid fuel.

[0003] The rotary kiln includes a cylindrical main body into which the biomass molded body before heating is input from one end side and from which the biomass solid fuel after heating is discharged from the other end side, and a heating unit arranged to cover the outer peripheral portion of the cylindrical main body and configured to heat the biomass molded body flowing inside the cylindrical main body. The inside of the cylindrical main body is maintained in a low-oxygen atmosphere (reducing atmosphere) by supplying an inert gas. The pyrolysis gas (biogas) generated by heating the biomass molded body inside the cylindrical main body is supplied to the combustion furnace.

[0004] The combustion furnace is configured to burn the pyrolysis gas supplied from the rotary kiln to generate combustion gas and supply the combustion gas to the heating unit. That is, the pyrolysis gas generated by heating the biomass molded body in the rotary kiln is used as fuel for the combustion furnace, and the heat of the combustion gas generated by burning the pyrolysis gas in the combustion furnace is used for heating the biomass molded body in the rotary kiln, enabling the production of a self-sustaining type of biomass solid fuel.

Prior Art Documents

Patent Documents

[0005]

Patent Document 1

[0006] This disclosure describes a biomass solid fuel production system that enables efficient operation. [Means for solving the problem]

[0007] An example of a biomass solid fuel production system comprises a fuel production facility and a clinker production facility configured to produce biomass solid fuel from biomass raw materials. The fuel production facility includes a heating device configured to heat biomass raw materials to produce biomass solid fuel, a combustion furnace configured to burn the pyrolysis gas generated by heating the biomass raw materials in the heating device to produce combustion gas, a first flow path, and a second flow path. The clinker production facility includes a raw material preparation unit configured to dry cement raw materials, and a clinker production unit configured to produce clinker from the cement raw materials dried by the raw material preparation unit by combustion of fuel. The first flow path is configured to introduce high-temperature combustion gas discharged from the combustion furnace into the clinker production unit. The second flow path is configured to introduce low-temperature combustion gas discharged from the heating device after heating the biomass raw materials into the raw material preparation unit. [Effects of the Invention]

[0008] The biomass solid fuel production system described in this disclosure enables efficient operation. [Brief explanation of the drawing]

[0009] [Figure 1] Figure 1 is a schematic diagram illustrating an example (first example) of a biomass solid fuel production system. [Figure 2] Figure 2 is a schematic diagram illustrating another example (second example) of a biomass solid fuel production system. [Modes for carrying out the invention]

[0010] In the following descriptions, the same reference numeral will be used for identical elements or elements with the same function, and redundant explanations will be omitted. Furthermore, in this specification, when referring to the top, bottom, right, and left of a figure, the direction of the reference numeral in the figure will be used as the reference.

[0011] [Biomass Solid Fuel Production System] First, with reference to Figure 1, the configuration of the biomass solid fuel production system 1 (first example) will be described. The production system 1 is configured to produce biomass solid fuel BF from biomass raw material BM, and cement clinker MT4 (clinker) from cement raw material MT1. That is, as illustrated in Figure 1, the production system 1 comprises a fuel production facility 100 for producing biomass solid fuel BF, a clinker production facility 200 for producing cement clinker MT4, and a controller Ctr (control unit).

[0012] The biomass raw material BM used in manufacturing system 1 is not particularly limited. For example, the biomass raw material BM may be woody biomass or herbaceous biomass. Woody biomass may be obtained by crushing at least one of wood chips and waste wood. Woody biomass may be, for example, construction waste wood, forest residue, sawmill residue, palm kernel shells, rice husks, rice straw, wheat straw, animal feed, waste paper, etc., or crushed materials thereof. The biomass raw material BM used in manufacturing system 1 may be a biomass molded body that has been pressure-molded into a predetermined shape (e.g., pellet or briquette) by a molding machine (e.g., pelletizer or briquette machine).

[0013] The degree of carbonization of the biomass solid fuel BF produced in manufacturing system 1 is not particularly limited. In this document, "degree of carbonization" refers to the degree of carbonization of the biomass solid fuel, and can be evaluated by, for example, the solid (material) yield and the energy yield. The solid (material) yield is defined as the ratio of the amount of product produced to the amount of raw material supplied (solid (material) yield = amount of product produced / amount of raw material supplied × 100), and the lower the solid (material) yield, the more advanced the carbonization of the biomass solid fuel is considered to be. The energy yield is defined as the ratio of the calorific value of the product to the calorific value of the raw material (energy yield = calorific value of the product / calorific value of the raw material × 100), and the lower the energy yield, the more advanced the carbonization of the biomass solid fuel is considered to be. In this document, a "high" degree of carbonization refers to a solid (material) yield of 80% or less, or an energy yield of 90% or less. On the other hand, in this book, a "low" degree of carbide refers to a case where the solid (substance) yield is 85% or higher, or the energy yield is 95% or higher.

[0014] [Fuel production equipment 100] As illustrated in Figure 1, the fuel production facility 100 includes a heating device 110 and a combustion furnace 120.

[0015] The heating device 110 is configured to carbonize the biomass raw material BM by heating it with combustion gas CG supplied from the combustion furnace 120, thereby producing biomass solid fuel BF. The heating device 110 includes a cylindrical body 111, a girth gear 112, a plurality of tires 113, a plurality of support parts 114, a discharge part 115, and a heating part 116. The heating device 110 may be, for example, an externally heated rotary kiln.

[0016] The cylindrical body 111 is a long, roughly cylindrical object. The cylindrical body 111 includes one end 111a (inlet) into which the biomass raw material BM1 is fed, and the other end 111b (outlet) from which the biomass solid fuel BF is discharged. That is, the biomass raw material BM flows through the inside of the cylindrical body 111 from the one end 111a to the other end 111b. The cylindrical body 111 may be installed so that its longitudinal direction extends along the horizontal direction, or it may be installed so that its longitudinal direction is inclined with respect to the horizontal direction. In the latter case, the cylindrical body 111 may be installed so that it slopes downward from the one end 111a to the other end 111b.

[0017] The girth gear 112 is fixed to the outer surface of the cylindrical body 111 so as to extend along the circumferential direction of the cylindrical body 111. That is, the girth gear 112 has a substantially annular shape. The girth gear 112 has a gear shape with alternating bumps and grooves in its circumferential direction. The girth gear 112 meshes with a pinion gear (not shown), and rotates when a drive source (e.g., an electric motor) (not shown) rotates the pinion gear. As a result, the rotational force of the pinion gear is transmitted to the cylindrical body 111 via the girth gear 112. Consequently, the cylindrical body 111 rotates around a rotation axis that extends along its longitudinal direction.

[0018] The installation position of the girth gear 112 relative to the cylindrical body 111 is not particularly limited. As illustrated in Figure 1, the girth gear 112 may be located in the longitudinal direction of the cylindrical body 111, closer to one end 111a of the cylindrical body 111. Multiple girth gears 112 may be provided on the outer circumferential surface of the cylindrical body 111.

[0019] The plurality of tires 113 are each fixed to the outer peripheral surface of the cylindrical main body 111 so as to extend along the circumferential direction of the cylindrical main body 111. That is, the plurality of tires 113 each exhibit a substantially annular shape. Each tire 113 is supported by a support portion 114 (for example, a support roller). That is, the outer peripheral surface of the tire 113 is in direct contact with the outer peripheral surface of the support portion 114. Therefore, the outer peripheral surface of the tire 113 and the outer peripheral surface of the support portion 114 may be smoothed for reducing frictional resistance.

[0020] The plurality of tires 113 may be arranged at predetermined intervals in the longitudinal direction of the cylindrical main body 111. As illustrated in FIG. 1, the heating device 110 may include two tires 113 and two support portions 114 that support each tire 113. In this case, one tire 113 may be located near one end portion 111a of the cylindrical main body 111, and the other tire 113 may be located near the other end portion 111b of the cylindrical main body 111.

[0021] The discharge portion 115 is connected to the other end portion 111b of the cylindrical main body 111 and forms a discharge space connected to the internal space of the cylindrical main body 111. The discharge portion 115 receives the biomass solid fuel BF discharged from the other end portion 111b of the cylindrical main body 111 and discharges the biomass solid fuel BF from a discharge port provided at the lower end portion. The discharge portion 115 receives the pyrolysis gas PG generated by heating the biomass raw material BM in the cylindrical main body 111 and discharges the pyrolysis gas PG toward the combustion furnace 120 through a pipe D1 from an exhaust port provided at the upper end portion.

[0022] The heating portion 116 is arranged so as to cover the outer peripheral portion of the cylindrical main body 111 and has a cylindrical shape as a whole. The heating portion 116 may be arranged at the central portion in the extending direction of the cylindrical main body 111. As illustrated in FIG. 1, the heating portion 116 may extend along the extending direction of the cylindrical main body 111 between the two tires 113.

[0023] The heating unit 116 is connected to the combustion furnace 120 by the pipe D2. Therefore, high-temperature combustion gas CG (high-temperature combustion gas CGa) discharged from the combustion furnace 120 is introduced into the heating unit 116 through the pipe D2. That is, the heating unit 116 is configured to indirectly heat the biomass raw material BM flowing inside the cylindrical main body 111 by heating the outer wall (outer surface) of the cylindrical main body 111 with the high-temperature combustion gas CGa. The temperature of the high-temperature combustion gas CGa may be, for example, about 1000°C.

[0024] The heating unit 116 may heat the biomass raw material BM to about 240°C to 700°C in a low-oxygen atmosphere (for example, the oxygen concentration inside the cylindrical main body 111 is 10% or less). When the biomass raw material BM inside the cylindrical main body 111 is heated by the heating unit 116, pyrolysis gas PG is generated from the biomass raw material BM, and the biomass raw material BM is carbonized into a carbide. The pyrolysis gas PG is a mixed gas of gaseous organic components and water vapor.

[0025] When the high-temperature combustion gas CGa introduced into the heating unit 116 heats the outer wall (outer surface) of the cylindrical main body 111, the temperature of the high-temperature combustion gas CGa decreases and becomes low-temperature combustion gas CG (low-temperature combustion gas CGb). The temperature of the low-temperature combustion gas CGb may be, for example, about 300°C. The low-temperature combustion gas CGb may be exhausted to the outside of the system (for example, the atmosphere) through the pipe D3 connected to the heating unit 116 by the blower F. The blower F is controlled based on a control signal from the controller Ctr. Thereby, the operation (driving or stopping) of the blower F and the adjustment of the blowing flow rate by the blower F are performed. The blower F may be, for example, an induced draft fan. Also, a dust collector (for example, a cyclone) configured to collect dust contained in the low-temperature combustion gas CGb may be provided between the blower F and the heating unit 116 in the pipe D3.

[0026] A valve V is provided on the upstream side of the blower F in the pipe D3. The valve V is controlled based on a control signal from the controller Ctr and is configured to adjust the opening degree by opening and closing the pipe D3 before and after the valve V.

[0027] As illustrated in Figure 1, the downstream end of pipe D2 may be connected to the other end 111b of the cylindrical body 111 within the heating section 116. The upstream end of pipe D3 may be connected to the one end 111a of the cylindrical body 111 within the heating section 116. In this case, the high-temperature combustion gas CGa introduced into the heating section 116 from pipe D2 heats the outer wall (outer surface) of the cylindrical body 111, flows towards the one end 111a of the cylindrical body 111 within the heating section 116, and becomes low-temperature combustion gas CGb. Subsequently, the low-temperature combustion gas CGb is discharged from the heating section 116 to the outside of the system through pipe D3. Thus, the heating device 110 illustrated in Figure 1 is a counter-flow type in which the flow direction of the biomass raw material BM flowing inside the cylindrical body 111 and the flow direction of the high-temperature combustion gas CGa flowing inside the heating section 116 are opposite. The heating device 110 may also be a parallel flow type in which these flow directions are the same.

[0028] From the middle of pipe D3 (upstream of valve V), pipe D4 branches off and extends. The downstream end of pipe D4 is connected to the raw material preparation section 201 (described later) of the clinker manufacturing equipment 200. More specifically, the downstream end of pipe D4 branches off toward each of the devices constituting the raw material preparation section 201 and is connected to each of the devices constituting the raw material preparation section 201. Therefore, the low-temperature combustion gas CGb discharged from the heating section 116 can be introduced into each of the devices constituting the raw material preparation section 201 through pipes D3 and D4. In other words, a part of pipe D3 (the portion of pipe D3 from the upstream end to the branching point) and pipe D4 constitute a flow path (second flow path) for introducing the low-temperature combustion gas CGb into the raw material preparation section 201. Note that pipe D4 does not necessarily have to branch off from pipe D3. In other words, the upstream end of pipe D4 may be connected to the heating section 116.

[0029] The combustion furnace 120 is configured to produce combustion gas CG by burning the pyrolysis gas PG generated by heating the biomass raw material BM in the heating device 110. In the combustion furnace 120, at least one of the pyrolysis gas PG1 supplied through piping D1 and fuel supplied from an external source (e.g., liquefied petroleum gas (LPG)) is mixed with air (oxygen-containing gas) supplied from an external source and burned at a high temperature. The pyrolysis gas PG is completely combusted. The high-temperature combustion gas CGa produced by the combustion is supplied to the heating section 116 through piping D2.

[0030] From the middle of pipe D2, pipe D5 (the first flow path) branches off and extends. The downstream end of pipe D5 is connected to the clinker production section 202 (described later) of the clinker production equipment 200. More specifically, the downstream end of pipe D5 branches off towards each of the devices that make up the clinker production section 202 and is connected to each of those devices. Therefore, the high-temperature combustion gas CGa discharged from the combustion furnace 120 can be introduced into each of the devices that make up the clinker production section 202 through pipes D2 and D5. In other words, a part of pipe D2 (the portion of pipe D2 from the upstream end to the branching point) and pipe D5 constitute a flow path (the first flow path) for introducing the high-temperature combustion gas CGa into the clinker production section 202. Note that pipe D5 does not necessarily have to branch off from pipe D2. In other words, the upstream end of pipe D5 may be connected to the combustion furnace 120.

[0031] [Clinker manufacturing equipment 200] The clinker manufacturing equipment 200 includes a raw material preparation unit 201 and a clinker production unit 202. The raw material preparation unit 201 is configured to prepare cement raw materials (e.g., drying, crushing, mixing, etc.). The clinker production unit 202 is configured to produce clinker from the cement raw materials prepared by the raw material preparation unit 201 by burning fuel.

[0032] In the example in Figure 1, the clinker manufacturing equipment 200 includes a raw material storage area 210, a dryer 220, a raw material crusher 230, a silo 240, an SP (suspension preheater) 250, a kiln 260, a clinker cooler 270, a power generator 280, and a dust collector 290. In the example in Figure 1, the raw material preparation section 201 may include a dryer 220 and a raw material crusher 230. In the example in Figure 1, the clinker generation section 202 may include a calcination furnace 252 (described later) for the SP 250, a rising duct 253 (described later) for the SP 250, and a kiln 260.

[0033] The raw material storage area 210 is configured to store cement raw materials MT1. Cement raw materials MT1 are a mixture of, for example, limestone, coal ash, silica, clay, iron oxide raw materials, waste, etc., and are in size from a few centimeters to more than ten centimeters.

[0034] The dryer 220 is configured to dry the cement raw material MT1 introduced from the raw material storage area 210 by supplying hot air (for example, around 400°C). The cement raw material MT1 dried by the dryer 220 becomes the dried raw material MT2.

[0035] Exhaust gas G2 from the power generator 280 is introduced into the dryer 220 and used to dry the cement raw material MT1. Low-temperature combustion gas CGb discharged from the heating section 116 is introduced into the dryer 220 through pipes D3 and D4 and can also be used to dry the cement raw material MT1.

[0036] Meanwhile, the exhaust gas G3 from the dryer 220 is introduced into the dust collector 20. The temperature of the exhaust gas G3 when it is introduced into the dust collector 290 is, for example, about 90°C. Note that the clinker manufacturing facility 200 does not necessarily have to be equipped with a dryer 220. In this case, the cement raw material MT1 from the raw material storage area 210 is introduced into the raw material crusher 230.

[0037] The raw material pulverizer 230 is configured to pulverize the dried raw material MT2 introduced from the dryer 220. Examples of raw material pulverizers 230 include vertical mills and ball mills. The dried raw material MT2 is pulverized by the raw material pulverizer 230 into granules of 300 μm or less to become granular raw material MT3.

[0038] Exhaust gas G2 from the power generation device 280 is introduced into the raw material crusher 230 and used to dry the dried raw material MT2. Low-temperature combustion gas CGb discharged from the heating unit 116 is also introduced into the raw material crusher 230 through pipes D3 and D4 and may be used to dry the dried raw material MT2. That is, when the dried raw material MT2 is crushed in the raw material crusher 230, the dried raw material MT2 comes into contact with at least one of the exhaust gas G2 from the power generation device 280 and the low-temperature combustion gas CGb from the heating unit 116, and is further dried. Alternatively, the raw material crusher 230 may directly introduce the cement raw material MT1 and perform drying and crushing simultaneously.

[0039] Subsequently, the granular raw material MT3 is introduced into silo 240. Meanwhile, the exhaust gas G4 from the raw material crusher 230 is introduced into dust collector 290. The temperature of the exhaust gas G4 when it is introduced into dust collector 290 is, for example, around 90°C.

[0040] Silo 240 is configured to temporarily store granular raw material MT3 from the raw material crusher 230. Silo 240 is configured to supply the granular raw material MT3 to SP250 in a timely manner.

[0041] SP250 is a device for preheating granular raw material MT3 in kiln 260 to improve the calcination efficiency of the raw material. SP250 includes multiple stages (for example, about 4 to 5 stages) of cyclones 251 (separators) and a calcination furnace 252. The granular raw material MT3, which is fed into the cyclone 251 located at the top of the SP250 tower, moves downward while sequentially passing through each stage of cyclones 251 and calcination furnace 252.

[0042] Exhaust gas from kiln 260 is introduced from the bottom of the SP250 tower. The exhaust gas and granular raw material MT3 are sequentially heat-exchanged in the cyclones 251 at each stage, and the granular raw material MT3 is preheated to, for example, about 900°C to become preheated raw material. The preheated raw material generated in SP250 is discharged from the cyclone 251 located at the bottom of the tower and introduced into kiln 260. Meanwhile, exhaust gas G1 from SP250 is discharged from the cyclone 251 located at the top of the SP250 tower and supplied to the power generation device 280 by an induced draft fan (not shown). The exhaust gas G1 is, for example, about 400°C.

[0043] The calcination furnace 252 is located between the lowest cyclone 251 and the kiln 260. The calcination furnace 252 is configured to calcine preheated raw materials by burning fuel supplied from a supply unit (not shown) (e.g., coal such as pulverized coal, coke, etc.). This improves the production volume and calcination efficiency of the preheated raw materials. The calcination furnace 252 is connected to the kiln end 262 (described later) of the kiln 260 via a rising duct 253. Therefore, exhaust gas from the kiln 260 is introduced into the calcination furnace 252 via the rising duct 253.

[0044] The kiln 260 includes a main body 261, a kiln end 262, and a burner 263. The main body 261 is configured to fire preheated raw materials at high temperatures to produce cement clinker MT4. The kiln 260 may be, for example, a rotary kiln extending horizontally.

[0045] The maximum temperature of the main body 261 typically exceeds 2000°C. Therefore, in the main body 261, the preheated raw materials are heated to, for example, about 1450°C. The exhaust gas generated inside the main body 261 during firing is introduced into the SP250. The temperature of the exhaust gas when it is introduced into the SP250 is, for example, about 900°C to 1250°C. This exhaust gas contains carbon dioxide. On the other hand, the cement clinker MT4 produced by firing in the main body 261 is discharged into the clinker cooler 270, which is connected to the front part 264 (downstream end) of the main body 261 (kiln 260). The temperature of the cement clinker MT4 discharged into the clinker cooler 270 is, for example, about 1000°C.

[0046] The kiln end 262 connects the rising duct 253 of the SP250 to the main body 261, and is configured to introduce the preheated raw material, which has been preheated in the SP250, into the main body 261. In other words, the kiln end 262 constitutes the upstream end of the kiln 260 into which the preheated raw material is introduced.

[0047] The burner 263 is provided on the main body 261 so as to extend horizontally along the front part 264 of the main body 261. The burner 263 is configured to burn fuel supplied from a supply unit (not shown) (for example, coal such as pulverized coal, coke, etc.) and form a flame inside the main body 261. Inside the main body 261, the preheated raw material is scorched by the flame of the burner 263.

[0048] The clinker cooler 270 is connected to the front section 264 of the main body 261, and the cement clinker MT4 obtained by firing the preheated raw materials in the main body 261 is introduced into it. The clinker cooler 270 is configured to cool the cement clinker MT4 with a cooling gas (e.g., air).

[0049] The cement clinker MT4 cooled by the clinker cooler 270 is discharged from an outlet 271 located at the lower part of the downstream end of the clinker cooler 270. The cement clinker MT4 discharged from the outlet 271 may be stored in a storage unit (e.g., a silo) not shown. At least a portion of the cooling gas used to cool the cement clinker MT4 in the clinker cooler 270 is introduced into a dust collector 272 located at the upper part of the downstream end of the clinker cooler 270.

[0050] The dust collector 272 is configured to separate fine particles accompanying the cooling gas from the cooling gas. The dust collector 272 may be, for example, an electrostatic precipitator or a bag filter. The cooling gas after passing through the dust collector 272 may be exhausted to the outside of the clinker manufacturing facility 200 (for example, into the atmosphere) as exhaust gas from the clinker manufacturing facility 200.

[0051] The power generator 280 is configured to generate electricity by driving a power turbine with steam produced by heat exchange with exhaust gas G1. Therefore, a portion of the heat from the exhaust gas G1 is recovered as electrical energy in the power generator 280. The exhaust gas G2 from the power generator 280 is introduced into the raw material preparation unit 201 (at least one of the dryer 220 and the raw material crusher 230). The power generator 280 may also be positioned between the SP250 and the induced draft fan, and the exhaust gas G2 from the power generator 280 may be introduced into the raw material preparation unit 201 by the induced draft fan.

[0052] The dust collector 290 is configured to separate granular materials (powder or particles) contained in the exhaust gases G3 and G4 from the gas. The dust collector 290 may be, for example, an electrostatic precipitator or a bag filter. The exhaust gas after passing through the dust collector 290 may be exhausted to the outside of the clinker manufacturing facility 200 (for example, into the atmosphere).

[0053] [Effect] As shown in the above example, high-temperature combustion gas CGa and low-temperature combustion gas CGb, which are combustion gases CG at different temperatures, are introduced into the clinker production facility 200 to supply destinations suitable for their respective temperatures. Therefore, the combustion gas CG generated in the combustion furnace 120 is effectively utilized. Consequently, the biomass solid fuel production system 1 can be operated efficiently.

[0054] As shown in the above example, the high-temperature combustion gas CGa is introduced into the clinker manufacturing equipment 200 through pipes D2 and D5. Therefore, for example, if the temperature in the heating device 110 rises excessively, the high-temperature combustion gas CGa can be released into the clinker manufacturing equipment 200 through pipes D2 and D5, thereby protecting the heating device 110 and enhancing the overall safety of the manufacturing system 1.

[0055] As shown in the above example, since high-temperature combustion gas CGa is used for calcination or firing of the cement raw material MT1, the amount of external fuel used for calcination or firing of the cement raw material MT1 is reduced. Therefore, it becomes possible to reduce the manufacturing cost of cement clinker MT4.

[0056] As shown in the above example, since low-temperature combustion gas CGb is used to dry the cement raw material MT1, the amount of external fuel used to dry the cement raw material MT1 is reduced. Therefore, it becomes possible to reduce the manufacturing cost of cement clinker MT4.

[0057] Based on the above examples, the biomass raw material BM can be a molded body formed by pressurizing powdered biomass into a predetermined shape. In this case, the handling of the biomass raw material BM becomes easier.

[0058] [Differentiation] The disclosures herein should be considered in all respects to be illustrative and not restrictive. Various omissions, substitutions, and modifications may be made to the above examples without departing from the claims and the gist thereof.

[0059] (1) As illustrated in Figure 2, another example of manufacturing system 1 (the second example) differs from manufacturing system 1 in the first example mainly in that the fuel manufacturing equipment 100 further includes a classifier 130 and a crusher 140.

[0060] The classifier 130 is controlled based on a control signal from the controller Ctr and is configured to sieve the biomass solid fuel BF discharged from the discharge port of the discharge section 115 into sieved material with a particle size larger than a predetermined size and unsieved material. The classifier 130 may be, for example, a vibrating screen. The sieved material (biomass solid fuel BF with a relatively large particle size) may be shipped externally as a product, for example. The unsieved material (biomass solid fuel BF with a relatively small particle size) is transported to the crusher 140.

[0061] The crusher 140 is controlled based on a control signal from the controller Ctr and is configured to crush the sieved material separated in the classifier 130 into a fine powder. The crusher 140 may be, for example, a vertical mill. The fine biomass solid fuel BF produced by the crusher 140 may be transported to other equipment for use as a thermal energy source. Other equipment may be, for example, the clinker production section 202 of the clinker production equipment 200 (for example, at least one of the calcination furnace 252 and the kiln 260 (burner 263)).

[0062] The finely powdered biomass solid fuel BF produced by the crusher 140 may be used as a secondary raw material in other devices. The finely powdered biomass solid fuel BF used as a secondary raw material in other devices may exhibit functions such as a combustion aid, chlorine immobilizer, crushing aid, and anti-fusing agent. By introducing an anti-fusing agent into the clinker production unit 202, it is possible to suppress the fusion of molten plastics and the adhesion of molten plastics to the clinker production equipment 200 (for example, inside the calcination furnace 252, inside the kiln 260, etc.). By introducing a chlorine immobilizer into the clinker production unit 202, chlorine generated from chlorine-containing materials can be immobilized.

[0063] Furthermore, the crusher 140 may be supplied with the sieved material (biomass solid fuel BF with relatively small particle size) that has been classified by the classifier 130, as well as coal supplied from an external source. In this case, the crusher 140 may produce fine fuel by crushing the sieved material and coal while mixing them together, and then transport the fine fuel to another device.

[0064] In the second example illustrated in Figure 2, the finely powdered biomass solid fuel BF, crushed by the crusher 140, is supplied to the clinker production unit 202 as a thermal energy source, thereby reducing the amount of external fuel used by the clinker production unit 202. As a result, the manufacturing cost of cement clinker MT4 can be reduced.

[0065] In the second example illustrated in Figure 2, the biomass solid fuel BF produced in the heating device 110 is classified by the classifier 130 into sieved material with a particle size larger than a predetermined size and unsieved material. As a result, the sieved material (biomass solid fuel BF with a relatively large particle size) can be shipped externally as a product, while the unsieved material (biomass solid fuel BF with a relatively small particle size) that may not be suitable as a product can be effectively utilized for the production of cement clinker MT4.

[0066] (2) The low-temperature combustion gas CGb discharged from the heating section 116 may be introduced into at least one of the devices constituting the raw material preparation section 201. The low-temperature combustion gas CGb discharged from the heating section 116 may be introduced into at least two of the devices constituting the raw material preparation section 201 (for example, the dryer 220 and the raw material grinder 230) through physically independent and separate piping.

[0067] (3) The high-temperature combustion gas CGa discharged from the combustion furnace 120 may be introduced into at least one of the devices constituting the clinker generation unit 202. The high-temperature combustion gas CGa discharged from the combustion furnace 120 may be introduced into at least two of the devices constituting the clinker generation unit 202 (at least two of the calcination furnace 252, rising duct 253, and kiln 260) through physically independent and separate piping.

[0068] (4) The high-temperature combustion gas CGa discharged from the combustion furnace 120 or the low-temperature combustion gas CGb discharged from the heating section 116 may be used in other devices of the clinker manufacturing facility 200. Such other devices may be, for example, a finishing mill configured to pulverize the cement clinker MT4 produced in the clinker manufacturing facility 200. In this case, the heat from the high-temperature combustion gas CGa or the low-temperature combustion gas CGb makes it possible to ensure the semi-hydrated ratio of the gypsum that is fed into the finishing mill together with the cement clinker MT4. Such other devices may be, for example, a supply system for heavy oil used as fuel in the calcination furnace 252 or the kiln 260. In this case, the heat from the high-temperature combustion gas CGa or the low-temperature combustion gas CGb makes it possible to ensure the fluidity of the heavy oil.

[0069] [Other examples] Example 1. An example of a biomass solid fuel production system comprises a fuel production facility configured to produce biomass solid fuel from biomass raw materials, and a clinker production facility. The fuel production facility includes a heating device configured to heat biomass raw materials to produce biomass solid fuel, a combustion furnace configured to burn the pyrolysis gas generated by heating the biomass raw materials in the heating device to produce combustion gas, a first flow path, and a second flow path. The clinker production facility includes a raw material preparation unit configured to dry cement raw materials, and a clinker production unit configured to produce clinker from the cement raw materials dried by the raw material preparation unit by combustion of fuel. The first flow path is configured to introduce high-temperature combustion gas discharged from the combustion furnace into the clinker production unit. The second flow path is configured to introduce low-temperature combustion gas discharged from the heating device after heating the biomass raw materials into the raw material preparation unit.

[0070] In this case, high-temperature and low-temperature combustion gases, which are combustion gases at different temperatures, are introduced into the clinker production facility to supply gases appropriate to their respective temperatures. Therefore, the combustion gases generated in the combustion furnace are effectively utilized. Consequently, the biomass solid fuel production system can be operated efficiently.

[0071] In this case, the high-temperature combustion gas is introduced into the clinker manufacturing equipment through the first flow path. Therefore, for example, if the temperature in the heating device rises excessively, the high-temperature combustion gas can be released into the clinker manufacturing equipment through the first flow path, thereby protecting the heating device and enhancing the overall safety of the manufacturing system.

[0072] Example 2. The system of Example 1 may further include a crusher configured to crush the biomass solid fuel produced by the heating device and supply it to the clinker production unit. In this case, the finely powdered biomass solid fuel crushed by the crusher is supplied to the clinker production unit as a thermal energy source, thus reducing the amount of external fuel used in the clinker production unit. Therefore, it becomes possible to reduce the production cost of clinker.

[0073] Example 3. In the system of Example 2, the crusher may be a vertical mill.

[0074] Example 4. In the system of Example 2 or Example 3, the crusher may be configured to crush the biomass solid fuel produced by the heating device and the coal while mixing them together.

[0075] Example 5. Any of the systems in Examples 2 to 4 may further include a classifier configured to separate the biomass solid fuel produced by the heating device into sieved material (larger than a predetermined particle size) and unsieved material, and to supply the unsieved material to a pulverizer. In this case, it becomes possible to ship the sieved material (biomass solid fuel with a relatively large particle size) to the outside as a product, while effectively utilizing the unsieved material (biomass solid fuel with a relatively small particle size) that may not be suitable as a product for the production of clinker.

[0076] Example 6. In any of the systems in Examples 1 to 5, the clinker production unit includes a kiln configured to produce clinker by firing cement raw materials, a calcination furnace configured to calcine the cement raw materials supplied to the kiln, and a rising duct configured to connect the kiln's tail end to the calcination furnace, wherein the first flow path may be configured to introduce high-temperature combustion gas into at least one of the kiln, the calcination furnace, and the rising duct. In this case, since the high-temperature combustion gas is used for calcining or firing the cement raw materials, the amount of external fuel used for calcining or firing the cement raw materials is reduced. Therefore, it is possible to reduce the cost of clinker production.

[0077] Example 7. In any of the systems in Examples 1 to 6, the raw material preparation unit includes a raw material grinder configured to grind cement raw materials while in contact with a drying gas, and the second flow path may be configured to introduce the low-temperature combustion gas into the raw material grinder. In this case, since the low-temperature combustion gas is used to dry the cement raw materials, the amount of external fuel used to dry the cement raw materials is reduced. Therefore, it is possible to reduce the production cost of clinker.

[0078] Example 8. In any of the systems in Examples 1 to 6, the raw material preparation unit includes a dryer configured to supply hot air to the cement raw material to dry the cement raw material at least partially, and a raw material grinder configured to grind the cement raw material dried by the dryer while bringing it into contact with a drying gas, and the second flow path may be configured to introduce a low-temperature combustion gas to at least one of the dryer and the raw material grinder. In this case, the same effects as in Example 7 can be obtained.

[0079] Example 9. In any of the systems in Examples 1 to 8, the biomass raw material may be a molded body in which powdered biomass is pressure-molded into a predetermined shape. In this case, the handling of the biomass raw material becomes easier. [Explanation of Symbols]

[0080] 1...Manufacturing system, 100...Fuel manufacturing equipment, 110...Heating device, 120...Combustion furnace, 130...Classifier, 140...Crusher, 200...Clinker manufacturing equipment, 201...Raw material preparation section, 202...Clinker generation section, 220...Dryer, 230...Raw material crusher, 252...Calibration furnace, 253...Rising duct, 260...Kiln, BF...Biomass solid fuel, BM...Biomass raw material, CG...Combustion gas, CGa...High-temperature combustion gas, CGb...Low-temperature combustion gas, D2, D5...Piping (first flow path), D3, D4...Piping (second flow path), MT1...Cement raw material, MT4...Cement clinker (clinker), PG...Pyrolysis gas.

Claims

1. A fuel manufacturing facility configured to produce biomass solid fuel from biomass raw materials, Equipped with clinker manufacturing facilities, The aforementioned fuel manufacturing equipment is A heating device configured to heat the biomass raw material to produce the biomass solid fuel, A combustion furnace configured to generate combustion gas by burning the pyrolysis gas generated by heating the biomass raw material in the heating device, The first channel and Including a second flow path, The aforementioned clinker manufacturing equipment is A raw material preparation unit configured to dry cement raw materials, It includes a clinker generating unit configured to generate clinker from the cement raw materials dried by the raw material preparation unit by burning fuel, The first flow path is configured to introduce high-temperature combustion gas discharged from the combustion furnace into the clinker generation section. A biomass solid fuel production system, wherein the second flow path is configured to introduce low-temperature combustion gas, which is discharged from the heating device after heating the biomass raw material, into the raw material preparation section.

2. The system according to claim 1, further comprising a pulverizer configured to pulverize the biomass solid fuel generated by the heating device and supply it to the clinker generation unit.

3. The system according to claim 2, wherein the pulverizer is a vertical mill.

4. The system according to claim 2, wherein the pulverizer is configured to pulverize the biomass solid fuel produced by the heating device and coal while mixing them together.

5. The system according to claim 2, further comprising a classifier configured to separate the biomass solid fuel produced by the heating device into sieved material larger than a predetermined particle size and other sieved material, and to supply the sieved material to the pulverizer.

6. The clinker generation unit is A kiln configured to produce clinker by firing the cement raw materials, A calcination furnace configured to calcine cement raw materials supplied to the kiln, The kiln includes a rising duct configured to connect the kiln's tail end and the calcination furnace, The system according to claim 1, wherein the first flow path is configured to introduce the high-temperature combustion gas into at least one of the kiln, the calcination furnace, and the rising duct.

7. The raw material preparation unit includes a raw material grinder configured to grind the cement raw material while bringing it into contact with a drying gas. The system according to claim 1, wherein the second flow path is configured to introduce the low-temperature combustion gas into the raw material grinder.

8. The raw material preparation unit is A dryer configured to supply hot air to the cement raw material to dry the cement raw material at least partially, The system includes a raw material grinder configured to grind the cement raw material, which has been dried by the dryer, while bringing it into contact with a drying gas. The system according to claim 1, wherein the second flow path is configured to introduce the low-temperature combustion gas into at least one of the dryer and the raw material grinder.

9. The system according to any one of claims 1 to 8, wherein the biomass raw material is a molded body obtained by pressurizing powdered biomass into a predetermined shape.

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