JP6363808B1 - Biomass carbide production system - Google Patents

Abstract

A biomass carbide production system capable of improving energy saving without impairing the reduction effect of greenhouse gases while efficiently burning pyrolysis gas in the pyrolysis gas incineration section when producing biomass carbide from hydrous biomass I will provide a. A solid biomass fuel is burned to generate a combustion gas, and the combustion gas is supplied to a pyrolysis gas incineration unit 4 and brought into contact with the pyrolysis gas G2, and a drying processing unit 2 A dry biomass distribution unit 20 that takes out part of the generated dry biomass X2 and supplies it to the biomass burner 50 as a solid biomass fuel is provided. [Selection] Figure 1

Description

  The present invention comprises a drying treatment unit that dries hydrous biomass to produce dry biomass, a carbonization treatment unit that carbonizes the dry biomass to produce biomass carbide, and burns pyrolysis gas generated in the carbonization treatment unit. The present invention relates to a biomass carbide manufacturing system including a pyrolysis gas incineration unit for incineration.

  2. Description of the Related Art Conventionally, there is known a biomass carbide manufacturing system that manufactures biomass carbide by carbonizing after drying hydrous biomass such as dewatered sludge (see, for example, Patent Document 1). Such a biomass carbide manufacturing system can reduce the emission of greenhouse gases because it can omit the incineration of biomass waste and can use the manufactured biomass carbide as an alternative fuel for a thermal power plant. It is attracting attention as.

In such a biomass carbide manufacturing system, a configuration for effectively recovering heat generated in the system is adopted for the purpose of reducing the consumption of fossil fuel that causes greenhouse gas emissions.
Specifically, the pyrolysis gas generated in the carbonization processing unit is incinerated in the pyrolysis gas incineration unit, and the exhaust gas generated at that time is supplied to the drying processing unit as a heat source.
Furthermore, in the biomass carbide manufacturing system described in Patent Document 1, a part of the hydrated biomass (sewage sludge after dehydration) before being supplied to the drying treatment unit (drying furnace 20) is extracted, and the extracted hydrated biomass is used. A biomass burning section (sludge incinerator 70) is provided for appropriately adding dry biomass and burning it. And the exhaust gas produced | generated by the biomass combustion part is mixed with the exhaust gas produced | generated by the pyrolysis gas incineration part, Then, it supplies to a carbonization process part and a drying process part as a heat source, and heat recovery is performed.

JP 2005-319374 A

  In the biomass carbide production system, it is desired to efficiently secure a heat source without impairing the greenhouse gas reduction effect. For example, in the pyrolysis gas incinerator, a high temperature heat source is required to sufficiently heat the pyrolysis gas and decompose the dioxins and the like in the pyrolysis gas. Therefore, in the conventional system described above, a fossil fuel burner using fossil fuel (auxiliary fuel) as a fuel is provided in the pyrolysis gas incinerator. When the fossil fuel is burned by the fossil fuel burner to cover the amount of heat necessary for the pyrolysis gas incinerator, the greenhouse gas reduction effect is impaired and the energy saving performance is deteriorated. It was.

  In view of this situation, the main problem of the present invention is that when producing biomass carbide from hydrous biomass, the pyrolysis gas is efficiently combusted in the pyrolysis gas incineration section, while saving energy without impairing the greenhouse gas reduction effect. It is in the point which provides the biomass carbide manufacturing system which can improve property.

The first characteristic configuration of the present invention is a drying treatment unit that dries hydrous biomass to produce dry biomass;
A carbonization treatment unit that carbonizes the dry biomass to produce biomass carbide,
A biomass carbide production system comprising a pyrolysis gas incineration unit for burning and incinerating pyrolysis gas generated in the carbonization unit,
A solid biomass fuel is burned to generate a combustion gas, and a biomass burner for supplying the combustion gas to the pyrolysis gas incineration unit is provided, and a part of the dried biomass generated in the drying processing unit is taken out to form the solid It is in the point provided with the dry biomass distribution part supplied to the said biomass burner as biomass fuel.

According to this configuration, a part of the dried biomass generated in the drying processing unit is burned by the biomass burner as solid biomass fuel, so that a sufficient amount of combustion gas is efficiently generated, and the combustion gas is converted into pyrolysis gas. It can be supplied to the incinerator as a heat source. Furthermore, in the pyrolysis gas incineration unit, the pyrolysis gas can be sufficiently heated by the combustion gas supplied from the biomass burner and burned efficiently, for example, fossil fuel auxiliary combustion to make up for the lack of heat. Can be omitted or simplified.
Therefore, according to the present invention, in producing biomass carbide from hydrous biomass, biomass capable of improving energy saving without impairing the greenhouse gas reduction effect while efficiently burning the pyrolysis gas in the pyrolysis gas incinerator Carbide manufacturing system can be realized.

  The 2nd characteristic structure of this invention exists in the point which supplies the waste gas discharged | emitted from the said pyrolysis gas incineration part as a heat source to the said drying process part.

  According to this configuration, dry biomass can be efficiently generated in the drying processing unit using the exhaust gas discharged from the pyrolysis gas incineration unit as a heat source. And since a part of the dry biomass is burned with a biomass burner as solid biomass fuel, energy-saving property can be improved.

  The third characteristic configuration of the present invention is that the biomass burner is installed in the pyrolysis gas incineration unit, and combustion gas generated by the biomass burner is directly supplied to the pyrolysis gas incineration unit.

  According to this configuration, the biomass burner is installed in the pyrolysis gas incineration unit, and the combustion gas generated by the biomass burner is directly supplied to the pyrolysis gas incineration unit where the pyrolysis gas burns. Can be brought into contact with the pyrolysis gas in a high temperature state in which heat dissipation is suppressed, and a larger amount of heat can be given to the pyrolysis gas.

FEATURES configuration of the present invention is that the moisture content of the dry biomass to be supplied to the biomass burner is in a range of 5% or more and 30% or less.

  According to this structure, the combustion gas which has sufficient calorie | heat amount can be produced | generated in a biomass burner, suppressing the efficiency fall of a drying process part. That is, by setting the moisture content of the dry biomass supplied to the biomass burner to 5% or more, more preferably 10% or more, the amount of heat necessary for drying the water-containing biomass in the drying treatment section is limited, and the excess It is possible to suppress a decrease in efficiency due to dryness. Further, by setting the moisture content of the dry biomass supplied to the biomass burner to 30% or less, more preferably 25% or less, the latent heat of moisture contained in the dry biomass is limited in the biomass burner, so that it has a sufficient amount of heat. Combustion gas can be generated.

FEATURES configuration of the present invention is that the combustion amount of the biomass burner is assumed to correspond to the required amount of heat in the pyrolysis gas burning section.

  According to this configuration, the combustion amount of the biomass burner is equivalent to the amount of heat required in the pyrolysis gas incineration unit. Omitted, the pyrolysis gas incineration part can be simplified while sufficiently reducing the greenhouse gas effect and further improving energy saving.

A fourth characteristic configuration of the present invention is that at least a part of combustion air used for combustion of pyrolysis gas in the pyrolysis gas incinerator is supplied to the nozzle of the biomass burner.

  According to this configuration, in the biomass burner, the air ratio of combustion air to dry biomass as fuel becomes excessive, for example, about 2.0, but the surplus combustion air is momentum together with the combustion gas ejected from the nozzle. Since it is well blown into the pyrolysis gas incineration section, mixing of the pyrolysis gas and combustion air can be promoted in the pyrolysis gas incineration section to improve combustion efficiency.

Schematic configuration diagram of biomass carbide manufacturing system

Embodiments of the present invention will be described with reference to the drawings.
The biomass carbide production system shown in FIG. 1 (hereinafter sometimes referred to as “the present system”) is a biomass carbide X3 that is used as an alternative fuel by dehydrating, drying, and carbonizing hydrated biomass X1 such as sewage sludge. It is configured as a system for manufacturing.

  Specifically, the present system includes a dewatering device 1 for dewatering the hydrated biomass X1 such as sewage sludge, and a drying processing unit 2 for drying the hydrated biomass X1 after being dehydrated by the dewatering device 1 to generate the dried biomass X2. The carbonization processing unit 3 that carbonizes the dry biomass X2 supplied from the drying processing unit 2 to generate the biomass carbide X3 is disposed along a path through which the biomass X1, X2, and X3 flow. Furthermore, the present system is provided with a pyrolysis gas incineration unit 4 that burns and incinerates the pyrolysis gas G2 generated in the carbonization processing unit 3. The system is also provided with a control device 60 for controlling the operation. Note that the dehydrating apparatus 1 may be omitted or simplified depending on the state of the supplied hydrous biomass X1, the processing capacity of the drying processing unit 2, and the like.

  The dehydration apparatus 1 is configured by, for example, a known pressure dehydrator, a centrifugal dehydrator, or the like, and is configured to input a water-containing biomass X1 having a high water content and to separate moisture from the input water-containing biomass X1. ing. Therefore, the dehydrated water-containing biomass X1 having a reduced water content is discharged from the dehydrator 1.

The drying processing unit 2 is composed of, for example, a known hot air dryer or the like. The dehydrated water-containing biomass X1 supplied from the dehydrator 1 is input, and the input water-containing biomass X1 is directly heated to the hot air while stirring. It is comprised so that it may be made to contact and dry. Therefore, from the drying processing unit 2, the dried biomass X2 after drying is discharged, and the exhaust gas G1 at about 150 ° C. to 250 ° C. containing the moisture released from the water-containing biomass X1 is discharged. Then, the dried biomass X <b> 2 dispensed from the drying processing unit 2 is granulated by the granulating device 6 and then supplied to the carbonization processing unit 3. On the other hand, the exhaust gas G1 discharged from the drying processing unit 2 is supplied to the pyrolysis gas incineration unit 4 through the blower 11 after the solid content is appropriately removed by the cyclone dust collector 7.
The solid content removed by the cyclone dust collector 7 is mixed with the dry biomass X2 discharged from the dry processing unit 2.
Moreover, in this embodiment, although the granulator 6 which granulates dry biomass X2 is installed in the upstream of the distribution part buffer tank 21 mentioned later, about the installation location of this granulator 6, it is a drying process part. For example, it may be on the transport path of the dry biomass X2 from 2 to the carbonization processing unit 3, and may be installed on the upstream side or downstream side of the carbonization processing unit buffer tank 23 described later on the downstream side of the distribution unit buffer tank 21, for example. I do not care. Moreover, this granulating apparatus 6 may be omitted as appropriate.

  The carbonization processing unit 3 is composed of, for example, a known indirect heating type rotary kiln and the like. The dried dry biomass X2 supplied from the drying processing unit 2 is input, and the input dry biomass X2 is stirred and low. It is configured to be heated and carbonized indirectly in an oxygen atmosphere. Therefore, from the carbonization processing unit 3, the carbonized biomass carbide X3 is discharged and the pyrolysis gas G2 including the combustible gas generated during the pyrolysis of the dry biomass X2 is discharged. And the biomass carbide | carbonized_material X3 discharged | paid_out from the carbonization process part 3 is discharged | paid out as a product, for example, after being cooled by the cooling conveyor 5. FIG. On the other hand, the pyrolysis gas G2 discharged from the carbonization processing unit 3 is supplied to the pyrolysis gas incineration unit 4.

  The pyrolysis gas incineration unit 4 is composed of, for example, a known gas combustion furnace, and the pyrolysis gas G2 supplied from the carbonization processing unit 3 is converted into solid content contained in the exhaust gas G1 supplied from the drying processing unit 2. At the same time, it is configured to be completely burned and incinerated while being mixed and stirred with the combustion air A in a high temperature environment. Therefore, from the pyrolysis gas incinerator 4, exhaust gas G3 at about 800 ° C. to 900 ° C. including the exhaust gas of the pyrolysis gas G2 is discharged.

The high-temperature exhaust gas G3 discharged from the pyrolysis gas incineration unit 4 is appropriately mixed with the exhaust gas G1 discharged from the drying processing unit 2 to be supplied to the drying processing unit 2 as exhaust gas G4. That is, in the drying processing unit 2, the exhaust gas G4 discharged from the pyrolysis gas incineration unit 4 is supplied as a heat source, and the hydrous biomass X1 is dried in a form in which the exhaust gas G4 is brought into contact with the hydrous biomass X1 as hot air. .
In the present embodiment, the exhaust gas G4 discharged from the pyrolysis gas incineration unit 4 is used as a heat source of the drying processing unit 2 so that the exhaust gas G4 is brought into direct contact with the hydrated biomass X1 as hot air. However, naturally, the heat of the exhaust gas G4 may be indirectly applied to the hydrated biomass X1. In addition, the configuration in which the exhaust gas G4 discharged from the pyrolysis gas incineration unit 4 is supplied to the drying processing unit 2 and used as a heat source may be omitted or modified as appropriate.

Further, the remaining exhaust gas G3 after being discharged from the pyrolysis gas incineration unit 4 and the supply to the drying processing unit 2 is taken out of, for example, the fly ash by the exhaust gas processing unit 9 after passing through the air preheater 8. After being removed and detoxified, it is released into the atmosphere.
In the air preheater 8, the combustion air A supplied through the blower 13 is preheated by heat exchange with the exhaust gas G3 at about 800 ° C to 900 ° C. The combustion air HA preheated by the air preheater 8 is supplied as a primary combustion air for the fossil fuel F to a fossil fuel burner 51, which will be described later. It can be supplied to the pyrolysis gas incinerator 4. Then, the control device 60 of the present system maintains the air ratio with respect to the combustible material containing the pyrolysis gas G2 in the pyrolysis gas incineration unit 4 at about 1.3, which is slightly higher than the theoretical air ratio. The opening degree of the combustion air adjustment valve 53 is controlled based on the detection result of the oxygen concentration sensor 16 that detects the oxygen concentration of the exhaust gas G3 discharged from the gas incinerator 4.

The pyrolysis gas incinerator 4 is provided with a fossil fuel burner 51 for maintaining a high temperature necessary for combustion of the pyrolysis gas G2. That is, the fossil fuel burner 51 jets the fossil fuel F supplied through the fuel adjustment valve 52 from the nozzle 51a to the pyrolysis gas incinerator 4 and burns it with the combustion air HA supplied from the air preheater 8. . Then, the control device 60 of the present system maintains the furnace top temperature of the pyrolysis gas incinerator 4 (an example of the furnace temperature) at about 800 ° C. to 900 ° C. The degree of opening of the fuel adjustment valve 52 is controlled based on the detection result of the temperature sensor 15 that detects this.
Further, the control device 60 maintains the air ratio of the fossil fuel burner 51 to the fossil fuel F at, for example, about 1.3, which is slightly higher than the theoretical air ratio. The amount of air blown by the blower 13 for the combustion air A is controlled on the basis of the opening degree of the fuel adjustment valve 52 corresponding to.

  The above is the basic configuration of the present system, and this system is configured to produce biomass carbide X3 from the hydrated biomass X1 by adopting a unique and rational feature configuration. Hereinafter, the characteristic configuration of this system will be described in order.

[Biomass burner]
This system is provided with a biomass burner 50 as a biomass combustion section that burns solid biomass fuel to generate a combustion gas including a flame and combustion exhaust gas, and supplies the combustion gas as a heat source. A dry biomass distribution unit 20 is provided that takes out a part of the dry biomass X2 produced in step 1 and supplies it to the biomass burner 50 as a solid biomass fuel.
Further, the biomass burner 50 supplies the generated combustion gas to the pyrolysis gas incineration unit 4 when supplying the combustion gas generated by burning dry biomass X2 as a heat source. The temperature of the pyrolysis gas G2 is increased.

  That is, in the biomass burner 50, a part of the dry biomass X2 that is efficiently generated in the drying processing unit 2 using the exhaust gas G4 as a heat source is supplied as solid biomass fuel. When the dry biomass X2 burns, a combustion gas containing a sufficient amount of flame and combustion exhaust gas is generated, and the combustion gas is supplied to the pyrolysis gas incinerator 4 as a heat source. Then, in the pyrolysis gas incinerator 4, the combustion gas supplied from the biomass burner 50 can sufficiently raise the temperature of the pyrolysis gas G2 and efficiently burn it.

  By providing the biomass burner 50, the fossil fuel burner 51 that supplies the combustion gas to the pyrolysis gas incineration unit 4 in the same manner as the biomass burner 50 is capable of supporting the fossil fuel F in an amount necessary to make up for the lack of heat. Will be done. Therefore, compared with the case where the biomass burner 50 is not provided, the combustion amount of the fossil fuel F in the fossil fuel burner 51 can be suppressed low. As a result, the amount of greenhouse gas generated can be reduced.

  If the combustion amount of the biomass burner 50 corresponds to the necessary heat amount in the pyrolysis gas incineration unit 4, the pyrolysis gas incineration unit 4 can be sufficiently heated only by the biomass burner 50. Thereby, the auxiliary combustion by the fossil fuel burner 51 for supplementing the heat quantity deficient in the pyrolysis gas incinerator 4 can be omitted.

  The biomass burner 50 is provided in the pyrolysis gas incineration unit 4 and is configured to supply combustion gas containing the generated flame directly to the pyrolysis gas incineration unit 4 through the nozzle 50a. That is, the combustion gas generated by the biomass burner 50 is supplied to the pyrolysis gas incineration unit 4 in a high temperature state in which heat dissipation is suppressed. Therefore, a large amount of heat can be applied from the combustion gas generated by the biomass burner 50 to the pyrolysis gas G2.

  Furthermore, the moisture content of the dried biomass X2 that is dispensed from the drying processing unit 2 and supplied to the biomass burner 50 is in the range of 5% to 30%, more preferably in the range of 10% to 25%. For example, the processing conditions in the drying processing unit 2 are set. That is, by setting the moisture content of the dry biomass X2 supplied to the biomass burner 50 to 5% or more, more preferably 10% or more, the amount of heat necessary for drying the hydrous biomass X1 in the drying processing unit 2 is limited. Thus, it is possible to suppress a decrease in efficiency due to the excessive drying. Moreover, if the moisture content of the dry biomass X2 dispensed from the dry processing unit 2 is 10% or more, the dry biomass X2 in the dry processing unit 2 can be prevented from being ignited with certainty. On the other hand, by setting the moisture content of the dry biomass X2 supplied to the biomass burner 50 to 30% or less, more preferably 25% or less, the latent heat of moisture contained in the dry biomass X2 in the biomass burner 50 is limited and sufficient. Combustion gas having a sufficient amount of heat can be generated.

  In addition, the process conditions of the drying process part 2 for maintaining the moisture content of the dry biomass X2 in a desired setting range can be preset based on an experimental result, an empirical rule, etc., for example. Further, the moisture content of the dried biomass X2 discharged from the drying processing unit 2 can be directly measured and acquired, but indirectly estimated based on the temperature of the exhaust gas G1 discharged from the drying processing unit 2, for example. And can be obtained. And the moisture content of the dry biomass X2 acquired in this way is constantly monitored, and the processing conditions in the drying processor 2 are controlled by the control device 60 so that the moisture content is maintained within a desired setting range. It can also be configured as follows.

  Combustion air A is supplied from the blower 12 to the biomass burner 50. This combustion air A is distributed, a part thereof is supplied as the primary combustion air for the dry biomass X2, and the other part is supplied to the nozzle 50a through the combustion air regulating valve 54.

  The control device 60 of the present system allows the biomass burner 50 to dry the biomass burner 50 in order to maintain the air ratio with respect to the dry biomass X2 serving as fuel in the biomass burner 50 in an excess air state of, for example, about 2.0, higher than the theoretical air ratio. Based on the supply amount of the biomass X2, the blowing amount of the combustion air A by the blower 12 is controlled. Further, the control device 60 of the present system is configured such that the ratio of the supply amount of the combustion air A to the biomass burner 50 and the supply amount of the combustion air A to the nozzle 50a is, for example, the latter supply amount rather than the former supply amount. Is controlled so that the opening degree of the combustion air regulating valve 54 is maintained at a predetermined setting ratio that is slightly larger.

  That is, since the biomass burner 50 is in an excess air state, at least a part of the combustion air A used for combustion of the pyrolysis gas G2 in the pyrolysis gas incinerator 4 is supplied to the nozzle 50a of the biomass burner 50. Will be. Therefore, a part of the combustion air A supplied to the nozzle 50a is not consumed for the combustion of the dry biomass X2, but vigorously enters the pyrolysis gas incineration unit 4 together with the combustion gas containing the flame ejected from the nozzle 50a. Will be blown. Then, in the pyrolysis gas incinerator 4, the combustion air A blown vigorously from the nozzle 50a of the biomass burner 50 is well mixed with the pyrolysis gas G2, and as a result, the pyrolysis gas G2 This will improve the combustion efficiency.

  The low-temperature combustion air A supplied from the blower 12 is mixed with the high-temperature combustion air HA preheated by the air preheater 8 via the adjustment valve 55. With this configuration, the combustion air A supplied to the biomass burner 50 can be heated to reduce heat loss. Furthermore, a temperature sensor 56 that detects the temperature of the combustion air A supplied to the biomass burner 50 is provided, and the detected temperature is maintained within an allowable temperature range of the biomass burner 50 by the temperature sensor 56, for example. As described above, the mixing amount of the high-temperature combustion air HA is set by adjusting the opening of the adjusting valve 55.

[Buffer tank]
In this system, the dry biomass X2 generated in the dry processing unit 2 is temporarily stored, and when the supply amount of the dry biomass X2 to the biomass burner 50 changes, the dry biomass X2 to the carbonization processing unit 3 is changed. As dry biomass storage means for maintaining the supply amount at the set supply amount, a distribution unit buffer tank 21, a combustion unit buffer tank 22, and a carbonization processing unit buffer tank 23 are provided. That is, in the carbonization processing unit 3, the supply amount of the dry biomass X2 is maintained at the set supply amount, so that the dry biomass X2 is carbonized under stable processing conditions, and the quality of the high quality biomass carbide X3 is stable. Is generated.
In addition, in this application, the buffer tank 22 for combustion parts and the buffer tank 23 for carbonization process parts may be called a buffer tank after distribution.

The distribution unit buffer tank 21 temporarily stores the dry biomass X2 in the dry biomass distribution unit 20 that distributes the dry biomass X2 generated in the dry processing unit 2 to the biomass burner 50 side and the carbonization processing unit 3 side. It is configured as.
The combustion unit buffer tank 22 is configured to temporarily store the dry biomass X2 in a path from the dry biomass distribution unit 20 to the biomass burner 50.
The carbonization processing unit buffer tank 23 is configured to temporarily store the dry biomass X2 in a path leading from the dry biomass distribution unit 20 to the carbonization processing unit 3.

  In the present embodiment, three buffer tanks 21, 22, and 23 are provided as the dry biomass storage means, that is, a distribution unit buffer tank 21, a combustion unit buffer tank 22, and a carbonization processing unit buffer tank 23. However, only the distribution unit buffer tank 21 may be provided, or one of the combustion unit buffer tank 22 and the carbonization processing unit buffer tank 23 may be omitted. That is, by providing at least the distribution unit buffer tank 21 as the dry biomass storage means, it is possible to stabilize the processing conditions of the carbonization processing unit 3 and generate high-quality biomass carbide X3.

  Each buffer tank 21, 22, 23 is provided with feeders 21a, 21b, 22a, 23a for discharging the stored dry biomass X2 to the supply destination. These feeders 21a, 21b, 22a, and 23a are controlled by the control device 60 so that the amount of dry biomass X2 discharged from the buffer tanks 21, 22, and 23 can be adjusted.

  That is, the dry biomass X <b> 2 generated by the drying processing unit 2 is temporarily stored in the distribution unit buffer tank 21. Then, the dry biomass X2 paid out from the distribution unit buffer tank 21 by the feeder 21a is temporarily stored in the combustion unit buffer tank 22, and the stored dry biomass X2 is paid out by the feeder 22a to be solid biomass. The biomass burner 50 is supplied as fuel.

  On the other hand, the dry biomass X2 discharged from the distribution unit buffer tank 21 by the feeder 21b is temporarily stored in the carbonization processing unit buffer tank 23, and the stored dry biomass X2 is discharged by the feeder 23a and carbonized. It is supplied to the carbonization processing unit 3 as a processing target.

  The control device 60 of this system functions as the biomass combustion control means 61 by executing a predetermined program. The biomass combustion control means 61 is configured so that the furnace top temperature in the pyrolysis gas incineration unit 4 detected by the temperature sensor 15 is maintained at a predetermined set furnace top temperature (for example, about 800 ° C. to 900 ° C.). The supply amount of the dry biomass X2 to the burner 50 is controlled.

  In this embodiment, the biomass combustion control means 61 directly detects the furnace top temperature in the pyrolysis gas incinerator 4 with the temperature sensor 15 and supplies the dry biomass X2 to the biomass burner 50 based on the detection result. Although the amount control is performed, the supply amount control can be performed by another method. For example, the biomass combustion control means 61 detects the moisture content of the dry biomass X2, and based on the detection result, the biomass burner necessary for maintaining the furnace top temperature in the pyrolysis gas incinerator 4 at a predetermined set furnace top temperature. It is also possible to calculate the amount of combustion at 50 and control the amount of dry biomass X2 supplied to the biomass burner 50 so that the amount of combustion can be maintained.

  Further, in the case where the combustion unit buffer tank 22 is provided, the supply amount control of the dry biomass X2 to the biomass burner 50 is controlled by the amount of dry biomass X2 discharged by the feeder 22a of the combustion unit buffer tank 22 Can be run as Further, when the combustion unit buffer tank 22 is omitted and only the distribution unit buffer tank 21 and the carbonization processing unit buffer tank 23 are provided, the supply amount control of the dry biomass X2 to the biomass burner 50 is performed by the distribution unit. The amount of dry biomass X2 dispensed by the feeder 21a of the buffer tank 21 can be executed as a control target.

  And even if it is a case where supply control of dry biomass X2 to biomass burner 50 is performed by biomass combustion control means 61, dry biomass X2 supplied to carbonization processing part 3 is distribution part buffer tank 21 or carbonization processing part. Since the buffer tank 23 is temporarily stored, the control device 60 of the present system can maintain the supply amount of the dry biomass X2 supplied to the carbonization processing unit 3 at a predetermined set supply amount. By this, in the carbonization process part 3, the dry biomass X2 can be carbonized on the stable process conditions, and the high quality biomass carbide | carbonized_material X3 with stable quality can be produced | generated.

  In the case where the carbonization processing unit buffer tank 23 is provided, the supply amount of the dry biomass X2 supplied to the carbonization processing unit 3 is set by the dry biomass X2 by the feeder 23a of the carbonization processing unit buffer tank 23. The payout amount can be set as a setting target. Further, in the case where the carbonization processing unit buffer tank 23 is omitted and only the distribution unit buffer tank 21 and the combustion unit buffer tank 22 are provided, the supply amount of the dry biomass X2 supplied to the carbonization processing unit 3 is set. Can be executed with the amount of dry biomass X2 dispensed by the feeder 21b of the distribution unit buffer tank 21 as a setting target.

  The control device 60 of this system functions as a payout control means 62 by executing a predetermined program. The payout control means 62 is configured such that the storage amount of the post-distribution buffer tank, which is at least one of the combustion unit buffer tank 22 and the carbonization processing unit buffer tank 23 measured by a level sensor (not shown), is a predetermined set storage amount The amount of dry biomass X2 discharged from the distribution unit buffer tank 21 to the post-distribution buffer tank is controlled so as to be maintained at the above.

For example, when the combustion unit buffer tank 22 is provided as a post-distribution buffer tank, the payout control means 62 is configured so that the storage amount of the combustion unit buffer tank 22 tends to decrease with respect to the set storage amount. When the amount of payout at the feeder 21a is controlled to the increase side, conversely, when the amount of storage in the combustion unit buffer tank 22 tends to increase with respect to the set storage amount, the amount of payout at the feeder 21a is decreased. By controlling, the storage amount of the combustion unit buffer tank 22 is maintained at the set storage amount.
On the other hand, when the carbonization processing unit buffer tank 23 is provided as a post-distribution buffer tank, the payout control means 62 is used when the storage amount of the carbonization processing unit buffer tank 23 tends to decrease with respect to the set storage amount. Controls the payout amount in the feeder 21b to the increase side, and conversely, when the storage amount in the carbonization processing unit buffer tank 23 tends to increase with respect to the set storage amount, the payout amount in the feeder 21b is increased. It controls to the reduction | decrease side, and the storage amount of the carbonization process part buffer tank 23 is maintained by the setting storage amount.

That is, in the case where the combustion unit buffer tank 22 is omitted and only the distribution unit buffer tank 21 and the carbonization processing unit buffer tank 23 are provided, the dispensing control means 62 is dried to the carbonization processing unit buffer tank 23 side. The payout amount of the feeder 21b that pays out the biomass X2 is a control target. Further, when the carbonization processing section buffer tank 23 is omitted and only the distribution section buffer tank 21 and the combustion section buffer tank 22 are provided, the payout control means 62 sends dry biomass to the combustion section buffer tank 22 side. The payout amount of the feeder 21a that pays out X2 is set as a control target.
With this configuration, the control unit 61 controls the supply amount of the dry biomass X2 to the biomass burner 50 by the biomass combustion control means 61 and the quantitative supply of the dry biomass X2 to the carbonization processing unit 3. The fluctuation | variation of the storage amount of the carbonization process part buffer tank 23 can be suppressed.

  Then, the discharge control means 62 controls the discharge amount of the dry biomass X2 from the distribution unit buffer tank 21 to the combustion unit buffer tank 22 or the carbonization processing unit buffer tank 23 to thereby control the combustion unit buffer tank 22 and the carbonization processing. An appropriate amount of dry biomass X2 is always stored in the buffer buffer tank 23. Thus, the amount of dry biomass X2 discharged from the combustion unit buffer tank 22 and the carbonization processing buffer tank 23, in other words, the supply amount of the dry biomass X2 to the biomass burner 50 and the carbonization processing unit 3, is the biomass burner 50 and carbonization. The amount suitable for the processing unit 3 is maintained.

  When the distribution unit buffer tank 21 is omitted and only the combustion unit buffer tank 22 and the carbonization processing unit buffer tank 23 are provided, the control device 60 distributes the dry biomass X2 in the dry biomass distribution unit 20. By controlling the state, the storage amount of the combustion part buffer tank 22 and the carbonization processing part buffer tank 23 can be maintained at an appropriate set storage amount.

  In addition, when the two buffer tanks 21 and 22 are arrange | positioned in the path | route through which the dry biomass X2 supplied to the biomass burner 50 flows, or the dry biomass X2 supplied to the carbonization process part 3 passes. In the case where two buffer tanks 21 and 23 are arranged in series on the flow path, the payout amount at the feeders 21a and 21b in the upstream distribution section buffer tank 21 is determined by the downstream buffer tanks 22 and 23. It may be set so as to be the same as the payout amount at the feeders 22a and 23a.

[Combustion residue mixing section]
This system is provided with combustion residue mixing units 31, 32, and 33 for mixing the combustion residue Y taken out from the biomass burner 50 with the biomass X1 and X2 supplied to the carbonization processing unit 3.
That is, in the biomass burner 50, unlike the refined fossil fuel, solid biomass fuel (dry biomass X2) that is difficult to burn completely is burned, so that a solid combustion residue Y containing unburned components is generated. Furthermore, since the biomass burner 50 supplies combustion gas directly to the pyrolysis gas incineration unit 4, the combustion residue Y generated at that time can be taken out from the bottom of the pyrolysis gas incineration unit 4, The combustion residue Y thus taken out is temporarily stored in the storage tank 30.
In the present case, the combustion residue Y of the biomass burner 50 is configured to be extracted from the pyrolysis gas incineration unit 4 side. However, the combustion residue Y may be extracted from the biomass burner 50 side.

  The combustion residue Y stored in the storage tank 30 in this way is not discarded, but is supplied to the combustion residue mixing parts 31, 32, 33 through the feeder 30a, and carbonized by the combustion residue mixing parts 31, 32, 33. The biomass X1 and X2 supplied to the unit 3 are mixed. Then, the combustion residue Y is supplied to the carbonization process part 3 as a part of raw material of biomass carbide | carbonized_material X3 with biomass X1, X2. By this structure, the unburned component of the combustion residue Y produced | generated with the biomass burner 50 can be carbonized, and can be collect | recovered as a part of biomass carbide | carbonized_material X3.

As the combustion residue mixing parts 31, 32, 33 as described above, one or more selected from the first combustion residue mixing part 31, the second combustion residue mixing part 32, and the third combustion residue mixing part 33 are used. Can be adopted.
That is, the first combustion residue mixing unit 31 is configured to mix the combustion residue Y with the hydrated biomass X1 supplied to the drying processing unit 2.
By providing such a combustion residue mixing unit 31, even when the combustion residue Y is at a high temperature, the combustion residue Y is suitably cooled by the moisture contained in the water-containing biomass X1 to be mixed, thereby causing undesired ignition or the like. Can be prevented.

The 2nd combustion residue mixing part 32 and the 3rd combustion residue mixing part 33 are comprised as what mixes the combustion residue Y with the dry biomass X2 supplied to the carbonization process part 3 from the drying process part 2, and are 2nd combustion. The residue mixing unit 32 is disposed on the upstream side of the dry biomass distribution unit 20, for example, on the upstream side of the granulating device 6, and the third combustion residue mixing unit 33 is disposed on the downstream side of the dry biomass distribution unit 20. Yes.
By providing such combustion residue mixing units 32 and 33, the combustion residue Y mixed with the dry biomass X2 can be appropriately supplied to the carbonization processing unit 3 as a part of the raw material of the biomass carbide X3. Moreover, by providing the 3rd combustion residue mixing part 33 arrange | positioned downstream from the dry biomass distribution part 20, the whole quantity of the combustion residue Y mixed with dry biomass X2 is appropriately used as a part of raw material of biomass carbide | carbonized_material X3. The carbonization treatment unit 3 can be supplied.

  The control device 60 of this system functions as the combustion residue mixing control means 63 by executing a predetermined program. This combustion residue mixing control means 63 is configured so that the heat generation amount of the biomass carbide X3 generated in the carbonization processing unit 3 is equal to or greater than a predetermined set heat generation amount (for example, about 15 MJ / kg). 33 is configured to control the amount of combustion residue Y mixed with biomass X1 and X2 by 33. Further, the amount of combustion residue Y generated in the biomass burner 50 varies depending on the amount of dry biomass X2 supplied to the biomass burner 50. From this, when the biomass combustion control means 61 executes the supply amount control of the dry biomass X2 to the biomass burner 50, the storage amount of the combustion residue Y in the storage tank 30 does not exceed the set storage amount. The fuel supply amount restriction process for restricting the supply amount is executed.

Specifically, in the fuel supply amount control process executed by the biomass combustion control means 61, the storage amount of the combustion residue Y in the storage tank 30 is detected by the level sensor 30 b provided in the storage tank 30. When the storage amount of the combustion residue Y reaches a preset storage amount, the supply amount is limited in such a manner that the supply amount of the dry biomass X2 to the biomass burner 50 is reduced by, for example, a predetermined width. To do.
Then, the generation amount of the combustion residue Y in the biomass burner 50 is reduced, so that the storage amount of the combustion residue Y in the storage tank 30 is maintained below the set storage amount, and surplus combustion residue to be disposed of Y can be reduced as much as possible.
In addition, when the supply amount of the dry biomass X2 to the biomass burner 50 is decreased in the fuel supply amount control process, the combustion amount in the biomass burner 50 is reduced, but the decrease in the combustion amount is a fossil fuel. This can be compensated by an increase in the combustion amount of the burner 51.

The calorific value of the biomass carbide X3 can be measured by sampling and testing the biomass carbide X3 discharged from the carbonization processing unit 3.
And the combustion residue mixing control means 63 controls the amount of discharge of the combustion residue Y in the feeder 30a to the decrease side when the calorific value of the measured biomass carbide X3 falls below the set calorific value, and the biomass carbide The ratio of the carbide of the combustion residue Y contained in X3 is decreased, the calorific value of the biomass carbide X3 is increased, and is recovered to a set calorific value or more. Thereby, in the carbonization process part 3, the quality deterioration of the biomass carbide | carbonized_material X3 resulting from the excessive increase in the mixing rate of the combustion residue Y is prevented.

[Another embodiment]
Another embodiment of the present invention will be described. Note that the configuration of each embodiment described below is not limited to being applied alone, but may be applied in combination with the configuration of another embodiment.

(1) In the above embodiment, the buffer tanks 21, 22, 23 and the combustion residue mixing units 31, 32, 33 are provided, but these may be omitted or modified as appropriate.

(2) In the above embodiment, the biomass burner 50 as the biomass burning unit is installed in the pyrolysis gas incineration unit 4 and the combustion gas generated by the biomass burner 50 is directly supplied to the pyrolysis gas incineration unit 4. Although comprised as mentioned above, it installs a biomass combustion part as a thing different from the pyrolysis gas incineration part 4, and supplies the combustion gas produced | generated by the biomass combustion part to the pyrolysis gas incineration part 4 through a duct You may comprise.

(3) In the above embodiment, apart from directly supplying the primary combustion air to the burners 50 and 51, the combustion is performed through the combustion air regulating valves 53 and 54 to the pyrolysis gas incinerator 4 and the nozzle 50 a connected thereto. Although the configuration is such that supply air A is supplied, the form of the supply of combustion air A to the pyrolysis gas incinerator 4 and the nozzle 50a and the control of the supply amount thereof are modified as appropriate, for example, by omitting one or both. It doesn't matter.

2 Drying process part 3 Carbonization process part 4 Pyrolysis gas incineration part 20 Dry biomass distribution part 21 Distribution part buffer tank (dry biomass storage means)
22 Combustion unit buffer tank (dry biomass storage means)
23 Buffer tank for carbonization section (Dry biomass storage means)
31, 32, 33 Combustion residue mixing part 50 Biomass burner (biomass combustion part)
50a Nozzle 61 Biomass combustion control means 62 Discharge control means 63 Combustion residue mixing control means A Combustion air G1, G3, G4 Exhaust gas G2 Pyrolysis gas X1 Hydrous biomass X2 Dry biomass X3 Biomass carbide Y Combustion residue

Claims (4)

A drying treatment unit for drying the hydrous biomass to produce dry biomass;
A carbonization treatment unit that carbonizes the dry biomass to produce biomass carbide,
A biomass carbide production system comprising a pyrolysis gas incineration unit for burning and incinerating pyrolysis gas generated in the carbonization unit,
A solid biomass fuel is burned to generate a combustion gas, and a biomass burner for supplying the combustion gas to the pyrolysis gas incineration unit is provided, and a part of the dried biomass generated in the drying processing unit is taken out to form the solid A biomass carbide production system comprising a dry biomass distribution unit that supplies the biomass burner as biomass fuel.   The biomass carbide manufacturing system according to claim 1, wherein the exhaust gas discharged from the pyrolysis gas incineration unit is supplied to the drying processing unit as a heat source.   The biomass carbide manufacturing system according to claim 1 or 2, wherein the biomass burner is installed in the pyrolysis gas incineration unit, and combustion gas generated by the biomass burner is directly supplied to the pyrolysis gas incineration unit. The biomass carbide production according to any one of claims 1 to 3 , wherein at least a part of combustion air used for combustion of pyrolysis gas in the pyrolysis gas incinerator is supplied to a nozzle of the biomass burner. system.

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