JP2012201769A - Rapid heatup method for organic matter gasification system - Google Patents

Abstract

A high-temperature temperature raising method in a heat carrier circulation type organic material gasification system is provided.
The above object is to perform a preheater heating operation in which hot air is supplied from a hot air generator 1 to a preheater 2 in a state where the supply of raw materials to the pyrolyzer 4 and the circulation of the heat carrier are stopped. After the internal temperature reaches the predetermined preheater steady operation temperature, the rapid heating operation in which the heat carrier is circulated while continuing the raw material supply stop state and the hot air supply state is performed. This can be solved by carrying out until the temperature in the reactor 4 reaches a predetermined reformer steady operation temperature and a thermal cracker steady operation temperature.
[Selection] Figure 1

Description

  The present invention relates to a fast temperature raising method in a gasification system for organic substances such as woody biomass.

  In recent years, as a new energy supply system aimed at substituting fossil fuels and preventing global warming, technologies for gasifying woody biomass such as thinned wood and generating heat and electrical energy using this gas as fuel have been proposed and used. ing.

  Various gasification systems have been proposed. Among them, the heat carrier circulation system described in Patent Document 1 is one that is excellent in that it can generate a gas having a high hydrogen concentration. This gasification system includes a preheater, a reformer, a pyrolyzer, and a separator in order from the top, and a large number of heat carriers (heat carrying media) for carrying heat are heated by the preheater. Thereafter, the reformer, the thermal decomposer, and the separator are sequentially passed, and then returned to the preheater again by a transfer device such as a bucket conveyor.

  The organic material raw material is continuously and quantitatively supplied to the upper supply port of the pyrolyzer by, for example, a supply pipe connecting the reformer and the pyrolyzer by an appropriate quantitative feeder such as a screw conveyor. The organic substance supplied into the pyrolyzer comes into contact with a heated heat carrier supplied from the preheater via the reformer, and thereby char (solid carbon-containing residue) and pyrolysis gas (volatile) Sex phase). The char that is a solid content is supplied to the separator together with the heat carrier, and the pyrolysis gas that is a gas is raised and supplied to the reformer while making countercurrent contact with the heat carrier.

  The reformer is supplied with water vapor as a reaction medium, and is in contact with the water vapor under the condition that the pyrolysis gas is heated by a heat carrier and is in a high temperature environment of about 950 ° C. The hydrogen-containing concentration is much higher than the pyrolysis gas generated at around 0 ° C., and thus the amount produced is also increased.

  The gas generated in the reformer is sent to a gas processing / utilizing facility through a reformed gas discharge port provided in the upper part of the reformer.

  On the other hand, in the separator, the mixture supplied from the pyrolyzer is separated into char and heat carrier. The separated char is supplied to a hot air generator such as a hot stove, and the heat carrier is returned to the preheater by the transfer device.

  In the hot air generator, hot air (high temperature exhaust gas) is generated by the combustion of char. This hot air is supplied to the preheater, passed between the heat carriers passing through the preheater in a deposited state, and the heat carrier is heated by directly contacting the heat carrier. In the hot air generator, ash is generated by the combustion of char. Most of the ash is collected and removed in the hot air generator, but a part of the ash is supplied to the preheater and removed by a separating means such as a cyclone provided in the exhaust path of the preheater.

  In the steady operation, the heat carrier is heated to about 1000 ° C. by hot air in the preheater, releases heat near 550 ° C. in the thermal decomposition, and heat near 950 ° C. in the reformer, and has a different temperature range. Two endothermic reactions are induced.

  FIG. 16 shows the temperature change of each unit at the start-up (cold start) of the system from the air temperature state. In the cold start, through the startup operation of the related equipment, from the state where the entire system is at the temperature level temperature, first, the hot air generator burns auxiliary fuel to generate hot air, gradually increasing the hot air temperature, Finally, hot air of about 1050 ° C. is guided to the preheater to heat and heat the heat carrier from the temperature level. While the system is stopped, the system is cooled to a temperature state, and the inside of the furnace may be moistened due to intrusion of rainwater or condensation in the furnace. When the heat carrier in the preheater is sufficiently heated, for example, when the exhaust gas (preheater exhaust gas) coming out of the preheater exceeds approximately 200 ° C., the circulation of the heat carrier is also started under the preheater. It is dropped into the installed reformer. At the same time, the cooled heat carrier in the reformer is also dropped into the thermal decomposer provided thereunder, and further, the heat carrier of the thermal decomposer starts to be discharged, and the heat carrier of the entire system starts to circulate. As described above, the heat carrier heated by the preheater supplies heat to the circulation path such as a reformer, a thermal decomposer, a separator, and a transfer device (bucket conveyor) along with the circulation, The temperature rises. In the temperature raising process, if there is moisture in the system, the temperature rise may stagnate for a while at 100 ° C until the moisture evaporates, but once the evaporation is over, it starts to rise again, and the temperature of the pyrolyzer changes to the steady operating temperature. Starting from the point of time when the temperature reaches (about 600 degrees), the reformer operates at the steady operating temperature while suppressing excessive temperature rise exceeding the temperature limit of the thermal cracker due to its thermal decomposition (endothermic reaction). Wait for it to reach (about 950 degrees).

  An appropriate amount of the heat carrier is packed in advance in a preheater, a reformer, a thermal decomposer, a separator, a bucket conveyor, and the like, and is circulated so as to have a preset circulation amount. For example, the signal from the heat carrier level meter installed in the preheater and pyrolyzer controls the opening and closing of some segment valves so that the accumulation level of the heat carrier in the preheater and pyrolyzer falls within a certain range. The fine adjustment of the discharge amount when the discharge amount from the pyrolyzer is increased by the char generated in the pyrolyzer when the raw material is charged is performed based on this level meter signal.

  In the case of the heat carrier circulation type system, the circulation amount of the heat carrier can be adjusted by operating the opening / closing frequency (time interval) of the segment valve provided between the reformer and the pyrolyzer. The heat carrier is repeatedly heated and radiated while circulating in the system, but this one cycle is obtained by dividing the total amount of heat carrier by the amount of circulation per hour. 8 hours is the cycle time. For example, when the total amount of the heat carrier is about 4.7 tons, the circulation rate of the heat medium is about 400 to 600 kg / h.

Japanese Patent No. 4264525

  However, such a heat carrier circulation type system has a problem that it is not easy to guide the reformer and the pyrolyzer to different steady operation temperatures, and the system cannot be heated up to the steady operation temperature at high speed. It was.

  For example, in a heat carrier circulation type system in which the total amount of heat carrier is about 4.7 tons and the heat carrier circulation rate is about 400 to 600 kg / h, the system temperature is about the temperature (for example, reformer 25 ° C., thermal decomposition In order to raise the temperature from the state lowered to 25 ° C. to the steam reforming of the pyrolysis gas, that is, the temperature of the reformer to 950 ° C. and the pyrolyzer to the level of 550 ° C. capable of thermal decomposition of organic matter. Because of the heat radiation from the equipment, it is necessary to circulate the heat carrier for about 7 cycles or more, 3 to 4 days in days, and sometimes more.

In this way, if the time required to bring the system to a temperature capable of steam reforming of the pyrolysis gas is long, the system is started on the morning of the operation day and stopped in the evening of that day. Start daily stop (abbreviated as DSS) is impossible. If there is only a problem that the temperature rise time is long, it can be solved by performing continuous operation for 24 hours without stopping the system. For example, the gas generated by the heat carrier circulation system is used for power generation and sales. When electricity is used, 24-hour continuous operation may not be suitable, for example, when the profit at night is extremely low due to low electricity purchase prices and high labor costs.

  In addition, when the operation is closed on the weekend, if the temperature of the system is started again from Monday, it takes too much time to raise the temperature, and gas production and power generation on that day cannot be performed.

  Furthermore, as another problem, when the temperature of the reactor is extremely lowered due to the temperature rising process of the system or excessive supply of raw materials, even if trying to return the temperature of the reactor to the specified temperature, it cannot be returned immediately, It is also a problem to be forced to drive economically.

  Therefore, a main problem of the present invention is to provide a high-speed temperature raising method in a heat carrier circulation type organic substance gasification system.

The present invention that has solved the above problems is as follows.
<Invention of Claim 1>
A number of heat carriers for carrying heat, a preheater for heating the heat carrier, a reformer for performing steam reforming of the pyrolysis gas, and pyrolysis for pyrolyzing the organic material raw material And a hot air generator for generating hot air,
The heat carrier is passed through the preheater, the reformer, and the thermal decomposer in this order, and then returned to the preheater by the transfer device and circulated, and the organic material raw material is supplied into the thermal decomposer, Supplying steam directly or indirectly into the reformer,
In the pyrolyzer, the organic material is pyrolyzed into char and pyrolysis gas by bringing it into contact with a heated heat carrier, and the pyrolysis gas is reformed in countercurrent contact with the heat carrier. Supply
In the reformer, a gas having an improved hydrogen-containing concentration is produced by bringing the pyrolysis gas into contact with the water vapor while being heated by the heat carrier,
In the hot air generator, hot air is generated and supplied to the preheater,
In the preheater, the hot air supplied from the hot air generator is passed between the heat carriers passing through the preheater in a deposited state, and the heat carrier is heated by directly contacting the heat carrier.
A method of fast heating in an organic material gasification system configured as follows:
In the state where supply of the organic material raw material to the pyrolyzer and circulation of the heat carrier are stopped, hot air is supplied from the hot air generator to the preheater, and a preheater heating operation is performed.
After the temperature in the preheater reaches a predetermined preheater steady operation temperature, the rapid heating operation for circulating the heat carrier while continuing the supply stop state of the organic material and the hot air supply state, Until the temperature in the reformer and the temperature in the pyrolyzer reach the predetermined reformer steady-state operating temperature and the thermal cracker steady-state operating temperature, respectively.
A method for rapidly raising temperature in a gasification system for organic substances.

(Function and effect)
In this way, when the circulation of the heat carrier and the supply of the raw material are stopped, the temperature in the preheater is raised to the steady operation temperature, and then the supply of the heat carrier is started without starting the supply of the raw material. As shown in FIG. 15, the temperature of the reformer and the pyrolyzer is smoothly increased without exceeding the temperature limit of the equipment. Guided to steady operating temperature. And even if the raw material supply is started after the reformer and the pyrolyzer reach the steady operation temperature, it is possible to prevent a temperature drop that makes gasification impossible. Moreover, this effect is exhibited not only in a cold start described later but also in a hot start. Therefore, according to the present invention, the temperature of the system can be increased to a temperature at which gasification is possible.
On the other hand, when the temperature of the entire system is started while circulating the heat carrier and supplying the raw material, the temperature becomes too low when the heat carrier returns to the preheater via the thermal decomposer, and the thermal decomposer is in steady operation. Since the temperature is the lowest, as shown by a solid line in FIG. 16 and a two-dot chain line in FIG. 15, the pyrolyzer reaches the steady operating temperature, but the reformer does not reach the steady operating temperature, and the gas A half-finished situation that cannot be realized continues. That is, this is the main factor of prolonged temperature rise in the heat carrier circulation type system.

<Invention of Claim 2>
2. The organic substance gas according to claim 1, wherein the preheater steady operation temperature is 1000 ° C. or more, the reformer steady operation temperature is 950 ° C. or more, and the pyrolyzer steady operation temperature is 550 ° C. or more. Method for rapid temperature increase in a computer system.

(Function and effect)
The steady operating temperature of each unit is preferably within the above range.

<Invention of Claim 3>
At the time of cold start, the preheater, the reformer, and the thermal cracker are heated from the air temperature state to the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively.
Without supplying the organic material raw material and circulating the heat carrier, start supplying hot air to the preheater, and the hot air supply continues after the preheater temperature exceeds a predetermined temperature. Started circulating the heat carrier,
After the temperature inside the pyrolyzer reaches the pyrolyzer steady operation temperature due to the circulation of the heat carrier, the preheater heating operation is started,
After the preheater temperature increasing operation, the temperature in the preheater reaches the predetermined preheater steady operation temperature, and then the temperature in the reformer and the temperature in the pyrolyzer are the predetermined reformer steady operation temperature. 3. The high-speed heating method in the organic material gasification system according to claim 1, wherein the rapid heating operation is performed until reaching a steady operation temperature of the pyrolyzer, and then the supply of the organic material raw material is started.

(Function and effect)
As described above, in the conventional cold start, the state in which steam reforming can be performed, that is, the temperature inside the reformer reaches 950 ° C. for 3 to 4 days. Requires continuous operation. On the other hand, in the cold start of the present invention, the temperature is raised as before until the pyrolyzer reaches the steady operation temperature, but after that, the heating efficiency is increased by interposing the preheater temperature raising operation and the rapid heating operation. As a result, the temperature of each vessel reaches the steady operating temperature smoothly and rapidly.

<Invention of Claim 4>
The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. From the steady operation of supplying hot air to the preheater, circulating the heat carrier, and supplying the organic material raw material,
In a state where the supply of the organic material raw material is stopped, at least one of increase / decrease in the amount of heat supplied to the preheater and increase / decrease in the circulation rate of the heat carrier is performed, and at least one of the hot air supply amount and the supply hot air temperature to the preheater is performed. The temperature in the preheater is lower than the steady operation temperature of the preheater and equal to or higher than a predetermined lower limit temperature, and the temperature in the thermal decomposer is lower than the steady operation temperature of the thermal decomposer and a predetermined lower limit temperature. After shifting to the heat retention operation, the temperature inside the reformer is lower than the reformer steady operation temperature and at or above a predetermined lower limit temperature,
After the temperature maintaining operation is shifted to the preheater temperature increasing operation and the temperature in the preheater reaches a predetermined preheater steady operation temperature, the temperature in the reformer and the temperature in the thermal decomposer are set to a predetermined value. The organic substance according to claim 1, wherein the rapid heating operation is performed until the steady state temperature of the reformer and the steady state temperature of the pyrolyzer are respectively reached, and then the supply of the organic material raw material is resumed, and a hot start is performed. Fast heating method in the gasification system.

(Function and effect)
As described above, it may be desirable to temporarily stop the operation in order to operate the gasification system. For example, when generating electricity using the generated gas and selling power, there are cases where nighttime profits with low electricity purchase prices and high labor costs are drastically reduced, or operations are closed on weekends and consecutive holidays. In such a temporary shutdown, if the system is cooled to some extent, it takes a long time to raise the temperature of the system to a state where it can be gasified again.
For example, if this system stops the supply of raw materials before consecutive holidays and starts the supply of raw materials after the consecutive holidays several days later, once the system is stopped until hot air blowing is stopped, the internal temperature of the pyrolyzer However, in winter measurements from 2 ° C to 4 ° C, it cools from 500 ° C to 100 ° C in 24 hours. Even in the part where the heat remains most, such as a preheater, it is cooled to about the temperature in 5 to 6 days. Once the system has cooled down to about the temperature, it will be cold-started, so it takes a long time to start, and gasification will not begin immediately even after the temperature rises from the end of consecutive holidays. It will not be possible.
Therefore, when the system is temporarily stopped, the heat insulation operation is performed as described above to keep the system at a certain temperature or higher, and then the raw material supply is resumed through the preheater heating operation and the rapid heating operation of the present invention. By adopting such a hot start, the system can be restarted quickly while suppressing energy consumption.
The difference between the above-mentioned heat insulation operation and the standby operation described below is mainly the difference in the system temperature to be maintained. The heat insulation operation is performed at the lower limit temperature required for efficient hot start temperature increase. The standby operation is a steady operation temperature state in which raw materials can be supplied at any time, that is, an operation that maintains a high temperature. In both standby operation and heat insulation operation, the temperature of the system is maintained in a state where the material supply is stopped, and the energy consumption increases as the temperature is kept high. Instead, it is more reasonable to employ the above-described heat retention operation.

<Invention of Claim 5>
The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. From the state where the raw material supply is stopped until the raw material supply is started,
(Ii) Temporary or continuous stop of circulation of the heat carrier,
(B) Temporary or continuous execution of circulation of the heat carrier, and (ha) increase or decrease of at least one of hot air supply amount and supply hot air temperature to the preheater,
The temperature in the preheater, the temperature in the reformer, and the temperature in the pyrolyzer are changed to the preheater steady operation temperature, the reformer steady operation temperature, and the heat by the at least one operation of The high-speed temperature rising method in the gasification system of any one of Claims 1-4 which performs standby operation | maintenance each maintained to a cracker steady operation temperature.

(Function and effect)
For example, in operating this gasification system, it may be desirable to keep the system temperature at a steady operating temperature without supplying raw materials. For example, when the equipment of the system has reached a steady operating temperature due to rapid heating operation, but there is a time when the raw material supply cannot be started for a while until the raw material supply starts, or when the nighttime raw material supply stop in DSS, This is the case when the system temperature is kept at the steady operating temperature state for resumption. In such a case, by performing the standby operation described above, it is possible to maintain a temperature state at which the raw material can be supplied at any time. More specifically, the temperature of each device can be lowered by heat radiation by the operation of (ii), the temperature of each device can be raised by the heat supply by the operation of (ro), and the heat carrier by the operation of (ha). The degree of heating can be changed.

<Invention of Claim 6>
The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. When the temperature inside the pyrolyzer becomes less than the steady operation temperature of the pyrolyzer during steady operation in which the hot air is supplied, the heat carrier is circulated, and the organic material raw material is supplied. ,
After the preheater temperature increasing operation is performed and the temperature in the preheater reaches a predetermined preheater steady operation temperature, the temperature in the reformer and the temperature in the pyrolyzer are in a predetermined reformer steady operation. The rapid heating operation is performed until the temperature and the pyrolyzer steady operation temperature are reached, respectively, a reset operation is performed, and after the reset operation, the supply of the organic material raw material is resumed with a smaller supply amount than before the reset operation.
The high-speed temperature rising method in the gasification system of the organic substance of any one of Claims 1-5.

(Function and effect)
This system circulates the heat carrier in the system and utilizes the heat storage in the preheater and the heat release in the reformer and pyrolyzer to thermally decompose the organic substance in the pyrolyzer and the reformer. However, if the raw material is supplied too much to the pyrolyzer, the temperature of the heat carrier will decrease in the pyrolyzer due to endothermic reaction and evaporation of moisture. When the temperature exceeds the allowable range, the heat carrier temperature enters a temperature lowering spiral that decreases with each circulation. For example, in the normal case, the lower limit temperature allowable as the heat carrier temperature in the pyrolyzer is approximately 500 ° C., and below this temperature, when returning to the preheater, the temperature becomes 400 ° C. or lower, and the temperature rise limit in the preheater For this reason, a vicious circle called a temperature lowering spiral occurs, and the heat carrier cannot be returned to the steady operating temperature. On the other hand, when the above-described reset operation is performed, it is possible to escape from a vicious cycle of temperature decrease.

<Invention of Claim 7>
When the preheater internal temperature reaches the preheater steady operation temperature and the exhaust gas temperature of the preheater exceeds the equipment limit temperature, the following:
(I) When the circulation of the heat carrier is stopped, the circulation of the heat carrier is temporarily started.
(B) Temporarily or continuously, among the hot air supply amount and supply hot air temperature to the preheater, the supply hot air temperature is maintained and the hot air supply amount is decreased.
(C) Temporarily stopping the supply of hot air to the preheater,
(D) Temporarily blow cooling air to the preheater,
Performing at least one overheat suppression operation of
The high-speed temperature rising method in the gasification system of the organic substance of any one of Claims 1-6.

(Function and effect)
During preheater heating operation, rapid heating operation, standby operation, etc., the temperature in the preheater may reach the preheater steady operation temperature, and the temperature may rise and the exhaust gas temperature of the preheater may exceed the equipment limit temperature. However, at that time, it is possible to prevent overheating of the preheater due to continued operation while suppressing the temperature drop of the preheater by executing at least one overheat suppression operation of (i) to (d) above. . The term “temporary” includes intermittent (hereinafter the same). For example, when the circulation of the heat carrier (a) is resumed temporarily or continuously, and the temperature inside the preheater still does not decrease, the supply of hot air to the preheater is maintained and the hot air supply amount is decreased (b) to By performing the operation (c), it is possible to prevent overheating of the preheater due to continuation of the preheater heating operation or the like, but there is still a case where the temperature rise of the preheater cannot be suppressed. Therefore, in such a case, it is preferable to perform the preheater cooling process as described in (2) above.

<Invention of Claim 8>
8. The method according to claim 1, wherein at least one of a hot air supply amount and a supply hot air temperature to the preheater is increased simultaneously with, immediately before or immediately after the start of circulation of the heat carrier in the rapid heating operation. Fast heating method in organic material gasification system.

(Function and effect)
When the heat carrier circulation is started in the rapid heating operation, the temperature of the preheater may be excessively lowered. Thus, at the same time as the heat carrier circulation start or immediately before or after the heat carrier supply amount and It is preferable to increase at least one of the supply hot air temperatures to prevent a temperature drop of the preheater.

<Invention of Claim 9>
In stopping the system, in a state where the supply of the organic material raw material to the pyrolyzer is stopped, the heat carrier circulation and the hot air supply to the preheater are continued, and a post-processing operation is performed for a predetermined time. The high-speed temperature raising method in the organic material gasification system according to claim 1, wherein the circulation of the heat carrier and the supply of hot air to the preheater are stopped later.

(Function and effect)
If the heat carrier circulation is stopped immediately when the system is shut down, a large number of heat carriers are agglomerated due to the solidification of the tar dripping into the pyrolyzer, and the heat carrier circulation is inhibited at the start of the next system. May bring. On the other hand, when the post-processing operation is performed as described above, the heat carrier heated by the hot air circulates even when tar is dropped in the pyrolyzer, so that it is difficult to cause a solidified state. Become.

  As described above, according to the present invention, in the heat carrier circulation type organic substance gasification system, it is possible to increase the temperature of the system to a temperature at which gasification is possible at high speed.

It is a flowchart of a gasification system. It is a longitudinal cross-sectional view of a preheater. It is AA sectional drawing and BB sectional drawing of FIG. It is a longitudinal cross-sectional view of a reformer. It is CC sectional drawing and DD sectional drawing of FIG. It is a longitudinal cross-sectional view of a pyrolyzer. It is EE sectional drawing of FIG. It is the schematic of a separator. It is the schematic of an umbrella-shaped screen. It is the schematic of a separator. It is a longitudinal cross-sectional view of a preheater. It is FF sectional drawing of FIG. It is a fractured perspective view of a preheater. It is a graph which shows roughly the example of temperature change of a preheater. It is a graph which shows roughly the example of a temperature change of each vessel in a cold start. It is a graph which shows roughly the example of temperature change of each container in the conventional cold start.

Hereinafter, an embodiment of the present invention will be described in detail with reference to the accompanying drawings.
The gasification system according to the present invention can be implemented, for example, with the equipment configuration shown in FIG. That is, the gasification system shown in FIG. 1 includes, in order from the top, a preheater 2, a reformer 3, a pyrolyzer 4, and a separator 5, and a large number of heat carriers for carrying heat. After the (heat-carrying medium) is heated by the preheater 2, the reformer 3, the pyrolyzer 4 and the separator 5 are passed in that order, and then returned to the preheater 2 again by the transfer device 6 such as a bucket conveyor. It is comprised as follows.

  As the heat carrier, a granular material having a particle size of about 5 to 20 mm, preferably about 8 to 12 mm can be used, and a spherical one is particularly suitable. Moreover, as a heat carrier material, a hard material having a large heat capacity such as alumina is suitable. The particle size is measured according to JIS A 1102, “Aggregate Screening Test Method”, using a sieve specified in JIS Z 8801-1, “Sieving for Testing-Part 1: Metal Mesh Screen”. This means the particle size (screen opening) by the sieving method (the same applies hereinafter).

  The organic material raw material is stored in the raw material hopper 17, and is cut out by an appropriate quantitative supply device such as a screw conveyor 14 or a rotary feeder, for example, via a supply line 3 x that connects the reformer 3 and the thermal cracker 4. The fixed amount is continuously supplied to the upper supply port of the pyrolyzer 4. The supply line 3x is provided with a valve 3b, and control such as stopping the passage of solid content such as a heat carrier is possible. During the circulation of the heat carrier, the valve 3b is repeatedly opened and closed at a predetermined interval, so that the solid content of the heat carrier or the like is intermittently passed through.

  As the organic material raw material, woody biomass such as thinned wood and pruned branches is suitable, but other wastes such as plastic can also be used. Examples of the waste plastic include vinyl chloride, polyurethane, methacrylic resin, polystyrene, polypropylene, and polyethylene. The shape of the organic material raw material is not particularly limited, but it is preferably a material that is crushed, cut, and pelletized to a particle diameter of about φ1 to 50 mm, L = 1 to 150 mm, particularly about 1.6 times the particle diameter of the heat carrier. Can be used.

  The organic substance supplied into the pyrolyzer 4 is brought into contact with a heated heat carrier supplied from the preheater 2 via the reformer 3 in a mixed state, thereby causing an endothermic reaction, and char (solid Carbon-containing residue) and pyrolysis gas (volatile phase). The temperature in the pyrolyzer 4 can be determined as appropriate, but is preferably about 500 to 600 ° C. Among the pyrolysis products, char which is a solid content is supplied to the separator 5 together with the heat carrier via the supply line 4x, and the pyrolysis gas which is a gas is reformed while being in countercurrent contact with the heat carrier. Ascended and supplied to the vessel 3. The supply line 4x is provided with a valve 4b, and a damper 4d is provided in two stages on the downstream side thereof, so that the former can be controlled to stop the passage of solids such as a heat carrier. The latter enables control such as stopping the passage of a gas component. During circulation of the heat carrier, the valve 4b repeats opening and closing at a predetermined interval, and the upper and lower dampers 4d perform the opening and closing operation in the opposite direction, thereby interrupting the passage of gas and interrupting solids such as the heat carrier. Quantitatively passes.

The reformer 3 is supplied with water vapor as a reaction medium. When the pyrolysis gas is heated by the heat carrier and mixed with the water vapor, the reforming reaction of the following formula occurs, High gas is generated. The temperature in the reformer 3 can be determined as appropriate, but is preferably 950 ° C. or higher in order to perform reforming sufficiently and reliably.
C _n H _m + nH ₂ O → nCO + (m / 2 + n) H ₂ (1)
CO + H ₂ O → H ₂ + CO ₂ (2)

  Although steam can be supplied by an appropriate method, in the illustrated example, the water in the water storage tank 19 is pumped by the feed water pump 19p, and is separately supplied from the reformer 3 in the waste heat boiler (indirect contact heat exchanger) 7. Steam is generated using the heat of the supplied product gas and then supplied from the lower part of the reformer 3. In addition to or instead of supplying steam to the reformer 3, steam used for the reforming reaction in the reformer 3 can also be indirectly supplied via the pyrolyzer 4 as shown.

  On the other hand, in the separator 5, the mixture supplied from the pyrolyzer 4 is separated into char and heat carrier. The separated char is supplied to a hot air generator 1 such as a hot stove by a transfer device 1 i such as a screw conveyor, and the heat carrier is returned to the preheater 2 by a transfer device 6. The supply line 6x from the transfer device 6 to the preheater 2 is provided with a valve 6b, and a damper 6d is provided in two stages downstream thereof, and the former stops the passage of solids such as a heat carrier. The latter can be controlled such as stopping the passage of gas components by the latter. During circulation of the heat carrier, the valve 6b repeatedly opens and closes at a predetermined interval, and the upper and lower dampers 6d perform the opening and closing operation in reverse, thereby blocking the passage of gas and interrupting the solids such as the heat carrier. Quantitatively passes.

  The hot air generating apparatus 1 includes a burner, and the char is burned by supplying air into the furnace through the burner, and hot air (high temperature exhaust gas) is generated. In the operation of the hot air generator, gas auxiliary fuel such as LPG and liquid fuel such as BDF can be supplied to the burner continuously or when necessary, such as at the start of operation, and burned. Hot air generated by the hot air generator 1 is supplied to the preheater 2. Moreover, the ash produced | generated by combustion of char with the hot air production | generation apparatus 1 is collect | recovered within the hot air production | generation apparatus 1, and is discharged | emitted by the ash storage part 1p.

  In the preheater 2, the hot air supplied from the hot air generator 1 is passed between the heat carriers passing through the preheater 2 in a deposited state, and the heat carrier is heated by directly contacting the heat carrier. The heat carrier heated by the preheater 2 is supplied to the reformer 3 via the supply line 2x. The supply pipe 2x is provided with a valve 2b, and a damper 2d is provided in two stages on the downstream side thereof, so that the former can be controlled to stop the passage of solids such as a heat carrier. The latter enables control such as stopping the passage of a gas component. During the circulation of the heat carrier, the valve 2b repeats opening and closing at a predetermined interval, and the upper and lower dampers 2d perform the opening and closing operation in the opposite direction, thereby interrupting the passage of gas and interrupting the solids such as the heat carrier. Quantitatively passes.

  The hot air used for heating the heat carrier in the preheater 2 is exhausted from the preheater 2 by the induction blower 15 and is mixed into the exhaust gas through the separating means 8 such as a cyclone. After the air is removed, it is preferably used in the air heater ((indirect contact heat exchanger)) 9 for heating the air supplied to the hot air generator 1, and then released to the atmosphere. In addition, prior to preheating in the air heater 9, heat is exchanged with steam (which can be manufactured and supplied by the above-described method) using a preheater (indirect contact type heat exchanger) 9i, and preheating is performed. More preferred.

  In the illustrated example, the hydrogen-containing product gas generated by the reformer 3 is sent from the reformer 3 to the gas treatment / use facility by the induction blower 11 and cooled to about 250 ° C. by the waste heat boiler 7. Subsequently, after being supplied to the wet scrubber 10 to remove tar and cooled to about 40 ° C., it is stored in the gas holder 12. The wet scrubber 10 in the illustrated example discharges cleaning water sprayed from the upper part from the lower part, cools it with a cooler (indirect contact heat exchanger) 10c, and sprays water again from the upper part. Indicates a washing water circulation pump, reference numeral 10d indicates a cooling water circulation pump that circulates cooling water with respect to the cooler, reference numeral 10t indicates a cooling tower that cools the cooling water by outside air, and reference numeral 18 indicates a cleaning water. 1 shows a wastewater treatment device for treating water.

  Although the form of use of the generated gas is not particularly limited, as shown in the figure, it is also one preferable form that the gas engine generator 13 is used to convert it into electric power. Moreover, it is also a preferable form that a part of the generated gas is used as an auxiliary fuel for the hot air generator 1.

  On the other hand, the heat carrier circulation cycle can be adjusted by manipulating the opening / closing frequency of the segment valve 3b among the opening / closing frequencies (intervals) of the segment valves 2b, 3b, 4b, 6b provided between the devices. In normal cases, 12 to 8 hours is appropriate as the cycle time. This one cycle can be obtained by dividing the total heat carrier amount by the circulation amount per hour. The other segment valves 2b, 4b, and 6b measure the heat carrier accumulation height by the heat carrier level meter installed in the preheater 2 and the pyrolyzer 4, and if the level is high, the opening and closing frequency is accelerated, the level When the temperature is low, automatic adjustment is made to slow down, and the heat carrier deposition height of the preheater 2 and the thermal decomposer 4 is kept in a certain range.

(Preheater)
Although the preheater 2 is not particularly limited, for example, one having an ash removing means as shown in FIGS. 2 and 3 is suitable. That is, the preheater 2 shown in FIGS. 2 and 3 has a cylindrical upper heat carrier passage 20 extending in the vertical direction, and a funnel shape (inverted truncated truncated cone shape) continuous below the upper heat carrier passage 20. The lower heat carrier passage 21 may be used as long as the diameter decreases toward the lower side.) The lower heat carrier passage 21 is provided at the center of the upper surface of the upper heat carrier passage 20 and at the lower end of the lower heat carrier passage 21. The exhaust port 21x has an exhaust port 20x on the side surface of the upper heat carrier passage 20 and a hot air outlet 22n on the side surface of the lower heat carrier passage 21, respectively.

  In the illustrated example, the lower heat carrier passage 21 is formed by a funnel-shaped member 22 having a large number of transmission holes 22n formed on the entire surface, such as punching metal, and surrounds the outside of the funnel-shaped member 22. An annular space 23 is formed, and a hot air supply port 24 from the outside communicates with a side surface of the annular space 23, the transmission hole 22 n of the funnel-shaped member 22 serves as a hot air blowing port, and the annular space 23 serves as a hot air blowing port 22 n. It becomes a distribution supply path communicating with all. The funnel-shaped member 22 can be formed of a heat-resistant metal such as a nickel alloy or a heat-resistant ceramic such as alumina ceramics, and the peripheral walls of the upper heat carrier passage 20 and the annular space 23 can be formed of a heat-resistant ceramic material such as alumina ceramics. The outer surface of 2 can be formed of an iron skin.

  In the preheater 2, the heat carrier descends while maintaining a certain accumulation state in the upper and lower heat carrier passages 20, 21, and passes through the lower heat carrier passage 21 from each hot air outlet 22 n, that is, It is heated in contact with hot air blown from a plurality of locations in the circumferential direction. As described above, when hot air is supplied from a plurality of locations in the circumferential direction to the heat carrier group passing through the lower heat carrier passage 21, the number of passages of the heat carrier decreases as the diameter of the lower heat carrier passage 21 decreases. In combination with the reduction, the fresh hot air from the hot air generating device 1 is brought into contact with more heat carriers directly or in a state close thereto, so that the heating efficiency of the heat carrier is improved.

  Characteristically, the size of the transmission hole 22n of the funnel-shaped member 22 is set so that the ash / dust D passes but the heat carrier does not pass, and communicates to the outside from the annular space 23 which is a distribution supply path. An ash / dust outlet 25 is formed. The shape of the transmission hole 22n of the funnel-shaped member 22 may be an appropriate shape such as an elliptical shape or a triangular shape in addition to a circular shape as shown in the illustrated example. The size of the transmission hole 22n can be determined as appropriate according to the size of the heat carrier. For example, the diameter of the transmission hole 22n (in the case of a circular hole means the diameter, and short in the case of other shapes (elliptical hole or the like)). The diameter (meaning the shortest of the diameters) can be less than the particle size of the heat carrier, in particular 70% or less, and the lower end of the ash / dust outlet 25 is aligned with the lower end of the annular space 23. Furthermore, the outlet 25 preferably extends from the side surface of the annular space 23 in the horizontal direction or downward.

  By having such an outlet 25, the ash / dust D accumulated in the preheater 2 is removed through the outlet 25, and the hot air outlet 22n and the distribution supply path 23 can be prevented from being blocked. Therefore, it is possible to prevent the heating carrier heating efficiency in the preheater 2 from decreasing with time, and to prevent the hydrogen concentration of the product gas from decreasing.

  The removal of the ash / dust D from the outlet 25 may be performed by mechanical means such as ash scraping. However, since the operation becomes complicated, the blowing that communicates with the distribution supply path 23 as in the illustrated example. An opening 26 is provided, and compressed air (inert gas may be used instead of compressed air; the same applies hereinafter) is blown from here, and ash / dust D is placed on the compressed air and discharged from the outlet 25. Then, it is preferable because the ash / dust D can be extracted regardless of the temperature in the furnace, and can also be automatically executed periodically. The number, position, and blowing direction of the blowing ports 26 can be determined as appropriate. However, it is preferable that the blowing ports 26 are provided on the side surface opposite to the outlet 25 in the annular distribution supply path 23 as illustrated. In particular, a plurality (two in the illustrated example) of the air inlets 26 are provided side by side in the circumferential direction, and compressed air from one air inlet 26 is supplied from one side of the annular distribution supply passage 23 as indicated by an arrow in the figure. Further, if the compressed air from the other blow-in port 26 is caused to circulate from the other side of the annular distribution supply path 23 toward the outlet 25, the ash / dust D in the distribution supply path 23 is smoothed. Since it can send out to the extraction outlet 25, it is preferable. The discharge of ash by the compressed air in the preheater 2 can be performed during the gasification operation as well as when the gasification operation is not performed. When discharging ash by compressed air, in order not to lower the temperature in the preheater 2, the compressed air to be supplied is appropriately exchanged with, for example, heat exchange with the waste heat similar to the supply air to the hot air generator 1. It can be supplied after being heated in advance to the temperature in the reformer 3 or in the vicinity thereof by the heating means.

(Reformer)
Ashes move in the order of the preheater 2, the reformer 3, and the pyrolyzer 4 along with the heat carrier, a path (for example, in the reformer 3 and between the reformer 3 and the pyrolyzer 4 (for example, And other problems such as an abnormal rise in the internal pressure of the thermal decomposer 4 due to blockage of the path between the reformer 3 and the thermal decomposer 4. This problem is alleviated by removing the ash in the preheater 2 described above, but it is more preferable to provide ash removing means in the reformer 3 as well.

  4 and 5 show an example of the reformer 3 having the same ash removal means as the preheater 2. That is, the reformer 3 has a cylindrical upper heat carrier passage 30 extending in the vertical direction, and a funnel shape (inverted truncated truncated cone shape continuous below the upper heat carrier passage 30. The diameter increases toward the lower side. The lower heat carrier passage 31, the supply port 30 i at the center of the upper surface of the upper heat carrier passage 30, and the gas introduction and heat carrier discharge at the lower end of the lower heat carrier passage 31. The outlet 31x, the reformed gas discharge port 30x on the side surface of the upper heat carrier passage 30 and the water vapor inlet 37 communicating with the lower end of the lower heat carrier passage 31 are provided.

  In the reformer 3, the heat carrier sufficiently heated by the preheater 2 is supplied from the upper supply port 30 i, and the reforming is performed while lowering the upper and lower heat carrier passages 30, 31 while maintaining a certain degree of deposition. The inside of the mass container 3 is maintained at the reforming reaction temperature. Under this temperature condition, the pyrolysis gas and water vapor introduced into the reformer 3 cause the above-described reforming reaction to generate a reformed gas containing a high amount of hydrogen, and the gas is passed through the reformed gas outlet 30x. Supplied to processing and utilization facilities.

  Characteristically, in the reformer 3 of the illustrated example, the lower heat carrier passage 31 is formed by a funnel-shaped member 32 having a large number of transmission holes 32n formed on the entire surface, such as punching metal. The size of the transmission hole 32n of the funnel-shaped member 32 is set so that the ash / dust D passes but the heat carrier does not pass, and an annular space 33 is formed so as to surround the outside of the funnel-shaped member 32. An ash / dust outlet 35 communicating with the outside from the side surface of the annular space 33 is formed. The through hole 32n of the funnel-shaped member 32 becomes an ash / dust intake port, and the annular space 33 becomes an ash / dust drop space communicating with all of the ash / dust intake port 32n. By having the ash / dust intake port 32n, the ash / dust removal space 33, and the outlet 35, ash that cannot be removed by the preheater 2 can be removed by the reformer 3, and the reformer As a result, it is possible to effectively prevent the accumulation of ash in the path between the reformer 3 and the pyrolyzer 4.

  The funnel-shaped member 32 can be formed of a heat-resistant metal such as a nickel alloy or a heat-resistant ceramic such as alumina ceramic, and the peripheral walls of the upper heat carrier passage 30 and the annular space 33 can be formed of a heat-resistant ceramic material. Can be formed by iron skin.

  The position and orientation of the ash / dust outlet 35, such as the shape and size of the transmission hole 32n of the funnel-shaped member 32, can be modified in the same manner as in the preheater 2. Further, as in the case of the preheater 2, in order to facilitate the removal of the ash / dust D from the outlet 35, an air inlet 36 communicating with the ash / dust drop space 33 is provided, and the ash / dust drop space 33 is provided. Alternatively, compressed air (inert gas may be used instead of compressed air; the same applies hereinafter) may be blown and discharged from the outlet 35. The ash is discharged by the compressed air in the reformer 3 when the gasification operation is not performed. In order to prevent the temperature inside the reformer 3 from being lowered when ash is discharged, an appropriate heating means such as heat exchange between the compressed air to be supplied and waste heat similar to the supply air to the hot-air generator 1 is used. Can be supplied after being heated in advance to the temperature in the reformer 3 or in the vicinity thereof. The position and direction of the compressed air blowing port 36 can be modified in the same manner as in the preheater 2. In the illustrated example, a blowing port 36 is added to the center between the blowing ports 36 on both sides with respect to the blowing port arrangement similar to that of the preheater 2.

(Separator)
The separator 5 is not particularly limited, and a rotary sieve, a vibrating sieve, or the like can be suitably used. In the case of using the separator 5 using such a screen, if the size of the char after pyrolysis is sufficiently smaller than the heat carrier, the heat carrier and the char can be reliably connected by using a screen that allows only the char smaller than the heat carrier to pass through. Can be separated. However, in reality, there is a limit even if the particle size of the organic material raw material is made uniform by crushing or the like, and generation of char larger than the heat carrier is inevitable, and this large lump of char is sent to the preheater 2 together with the heat carrier. The ash is generated by burning in the preheater 2. Moreover, the ash generated in this way is more easily deposited in the heat carrier circulation path, such as in the preheater 2 and the reformer 3, than being discharged with the exhaust of the preheater 2.

  Therefore, as shown in FIG. 8, as the separator 5, the first solid having a particle size equal to that of the heat carrier (mainly heat carrier) and the second solid having a particle size smaller than the first solid (mainly small). Char) and a third solid having a particle size larger than that of the first solid (mainly large char), and the first solid, the second solid and the second solid separated by the separator 5 Of the three solids, the first solid is returned to the preheater 2 by the transfer device 6, and the second solid and the third solid are preferably supplied to the hot air generator 1.

  The separator 5 is separated into solids of three kinds of particle sizes, and is configured to send char larger than the heat carrier to the hot-air generating device 1 together with char smaller than the heat carrier. It is preferable to suppress. In practice, strict separation is difficult, and a certain amount of char is supplied to the preheater 2 together with the heat carrier, and ash is generated in the preheater 2. Therefore, the above-mentioned ash removal is extremely effective. Means.

  The form of the separator 5 is not particularly limited. For example, as shown in the figure, a cylindrical inner screen 50 that allows the first solid and the second solid to pass but does not pass the third solid, and the second solid A two-stage screen type rotary sieve 5 having a cylindrical outer screen 51 having a diameter larger than that of the inner screen 50, which allows the objects to pass therethrough but does not allow the first and third solid substances to pass therethrough, can be used. In the rotary sieve 5, the separation object supplied into the screens 50 and 51 is such that the axes of the screens 50 and 51 are slightly inclined with respect to the horizontal direction (in addition to or instead of this). Further, the blades extending along the spiral direction are projected on the inner peripheral surfaces of the screens 50 and 51, and the blades are rotated along with the rotation of the screens 50 and 51 so that the separation object is transferred like a screw conveyor. And the screens 50 and 51 are rotated around the axis so that the screens 50 and 51 pass through the screens 50 and 51 while moving downward in the rotation direction of the screens 50 and 51 and in the inclination direction of the axis. It is based on the basic principle that it is separated into a thing and a thing which does not pass. In this example, when the char and heat carrier to be separated are supplied to one end side of the inner screen 50, the first solid and the second solid pass through the inner screen 50 and are supplied into the outer screen 51. The third solid material moves to the other end side of the inner screen 50 without passing through the inner screen 50, is collected from the opening on the other end side of the inner screen 50, and is supplied into the outer screen 51. Of the second solids, the second solids are collected through the outer screen 51, and the first solids move to the other end of the outer screen 51 without passing through the outer screen 51. It is collect | recovered from opening of the other end side.

(Pyrolyzer)
Chars larger than the heat carrier can be solved by separating them into three types of particle sizes in the separator 5, but there is a problem that the cost and installation area of the separator 5 increase. Therefore, as shown in FIGS. 6 and 7, the heat carrier discharge port 41x in the pyrolyzer 4 has a first solid material having a particle size equal to that of the heat carrier, and a second particle size smaller than that of the first solid material. It is also a preferable form to cover with a screen 42 that allows solids to pass but does not pass third solids having a particle size larger than the first solids. More specifically, the pyrolyzer 4 in the illustrated example has a cylindrical upper passage 40 extending in the vertical direction, and a funnel shape (inverted truncated truncated cone shape continuous below the upper passage 40). A lower passage 41), a supply port 40i at the center of the upper surface of the upper passage 40, a discharge port 41x covered with a screen 42 at the lower end of the lower passage 41, Each side surface of the lower passage 41 has a water vapor inlet 44.

  By providing such a discharge port screen 42, char larger than the heat carrier can be stopped by the screen 42 and not discharged from the thermal decomposer 4, and only the heat carrier and char smaller than the heat carrier can pass through the screen 42. The char larger than the heat carrier is prevented from being sent to the preheater 2 regardless of the separator 5 (that is, even if using a simple separator 5 such as a sieve device that passes only char smaller than the heat carrier). it can. Moreover, the char larger than the heat carrier stopped by the screen 42 is crushed by receiving external force due to heat and the movement of the heat carrier, and eventually passes through the screen 42 with a size smaller than the heat carrier. The discharge port of the pyrolyzer 4 is not blocked.

  The shape and the like of the discharge port screen 42 can be determined as appropriate, and may be flat punching metal. However, as shown in FIG. 9A, an umbrella shape whose diameter increases toward the discharge port 41x (see FIG. 9A). In the example shown, it has a conical shape, but it can also be in the shape of a pyramid, a dome, etc.) On the side of the body, a passage hole 42n (in the illustrated example, an isosceles triangular shape with an opening width increasing toward the discharge port 41x) However, a suitable shape such as a drop-like shape) is preferably provided in the circumferential direction at a predetermined interval. In such an umbrella-shaped screen 42, solids descending in the pyrolyzer 4 can smoothly move to the passage holes 42 n on the side surface of the screen 42. Moreover, since the passage hole 42n on the side surface of the screen 42 has a shape in which the opening width increases toward the discharge port side, the solid matter that descends while contacting along the side surface of the screen 42 enters the passage hole 42n. It is difficult to catch and smooth separation is possible.

  In addition to this, for example, as shown in FIG. 9B, an upper surface that does not have a passage hole and a passage hole 42n that extends with a predetermined width along the vertical direction are formed at intervals in the circumferential direction. A cylindrical screen 42 having a surface and an open bottom surface communicating with the discharge port 41x can also be used.

  On the other hand, when the discharge port screen 42 is provided, as the separator 5, a first solid and a second solid separated by the separator 5 are used, which are separated into two types of a first solid and a second solid. Among these, it is preferable that the first solid material is returned to the preheater 2 by the transfer device 6 and the second solid material is supplied to the hot air generating device 1 because the equipment becomes simpler. However, of course, even if the above three types of separation are used, the effect of improving the separation performance by demultiplexing is brought about. The form of the separator 5 in this case is not particularly limited. For example, as shown in FIG. 10, the rotary sieve 5 having a cylindrical screen 52 that passes the second solid but does not pass the first solid. Can be used. In the rotary sieve 5, when the char and heat carrier to be separated are supplied to one end of the screen 52, the axis of the screen 52 is slightly inclined with respect to the horizontal direction (with or without this) Instead, a configuration in which a blade along the spiral direction is projected on the inner peripheral surfaces of the screens 50 and 51 and the blades are rotated along with the rotation of the screens 50 and 51 so that the separation object is transferred like a screw conveyor. ), And the screen 52 is rotated around the axis, whereby the second solid is collected through the screen 52, and the first solid is not passed through the outer screen 52. The other end side of the outer screen 52 is recovered from the other end side opening.

(Fast heating method)
Next, referring to the temperature change during system operation shown in FIG. 14, the features of the present invention are as follows: (a) Application of high-speed temperature rise in cold start, (b) Standby operation, (c) Hot start The application will be described in the order of application of high-speed temperature rise, (d) overheat suppression operation, (e) reset operation, and (f) post-processing operation.

  In the following description, the temperature inside the preheater 2, the temperature of the exhaust gas from the preheater 2, the temperature inside the reformer 3, and the temperature inside the pyrolyzer 4 are detected by thermometers 2t, 2x, 3t, 4t, Can be monitored. Further, the temperature in the preheater 2 is the temperature of the lower part in the preheater 2 (that is, the temperature of the heat carrier before the preheating is completed and discharged toward the reformer 3 as can be seen from the illustrated position. Means). Further, the circulation of the heat carrier can be stopped by closing each segment valve 2b, 3b, 4b, 6b and stopping the transfer device 6, and the circulation is started by each segment valve 2b, 3b, 4b, 6b can be driven to open and close at each predetermined opening and closing frequency and the transfer device 6 is started. In addition, starting and stopping the supply of the organic material raw material can be performed by starting and stopping the raw material supply systems 14 and 17, and starting and stopping other facilities required at that time are also performed. In addition, the start and stop of hot air supply can be performed by starting and stopping fuel supply to the hot air supply and generation device 1 and the accompanying ignition and extinguishing, and starting and stopping other equipment required at that time Is also done.

(A) Application to cold start.
As shown in FIGS. 14 and 15, the cold start is a system start-up from a state where the entire system is at an air temperature level. Normally, in this state, all devices other than the measuring device are in a stopped state. From this state, the temperature is raised in the same manner as before until the temperature in the pyrolyzer 4 reaches the steady operating temperature of the pyrolyzer. That is, first, in the hot air generator 1, the auxiliary fuel is burned to generate hot air, and the hot air temperature is gradually increased. When the temperature in the preheater 2 reaches a predetermined temperature, for example, when the exhaust gas (preheater exhaust gas) exiting the preheater 2 exceeds 200 ° C., circulation of the heat carrier is started and warmed in the preheater 2 The obtained heat carrier is sequentially dropped to the reformer 3 and the thermal decomposer 4 installed thereunder, and then returned to the preheater 2 again. As the heat carrier circulates, heat is supplied to the circulation path such as the reformer 3, the thermal decomposer 4, and the separator, and the entire system is heated.

  Characteristically, when the temperature of the pyrolyzer 4 exceeds the steady-state operating temperature of the pyrolyzer, for example, 600 ° C., the supply of the raw material is not started but the circulation of the heat carrier is stopped while the supply of the raw material is stopped. In this state, the preheater heating operation is performed in which the supply of hot air from the hot air generator 1 to the preheater 2 is continued. In this preheater temperature increasing operation, it is impossible to supply char to the hot air generating device 1, and therefore the hot air generating device 1 is operated with auxiliary fuel. By this preheater temperature raising operation, the temperature in the preheater 2 tends to rise as shown in FIG. 15, and reaches a preheater steady operation temperature (for example, 1000 ° C.) after a certain period of time. On the other hand, the heat is not supplied to the reformer 3 and the pyrolyzer 4 as the heat carrier stops circulating, so that the heat radiation cooling starts and the temperature decreases. Therefore, the temperature of the pyrolyzer 4 does not exceed the device limit temperature.

  When the temperature in the preheater 2 reaches a predetermined preheater steady operation temperature, circulation of the heat carrier is started while continuing the supply stop state of the organic material and the hot air supply state. As a result, as shown in FIG. 15, the temperature in the reformer 3 and the temperature in the thermal cracker 4 rapidly rise and reach a predetermined reformer steady operation temperature and thermal cracker steady operation temperature, respectively. . When the temperature in the reformer 3 and the temperature in the pyrolyzer 4 reach a predetermined reformer steady operation temperature and thermal cracker steady operation temperature, respectively, or immediately after a standby operation described later, the organic material raw material Is started and the operation shifts to steady operation.

  With such a technique, the retained heat is supplied to the reformer 3 and the pyrolyzer 4 along with the resumption of circulation of the heat carrier, and there is also an influence of the relationship between the level of steady operation temperature of each unit and the heating order. As shown in FIG. 15, the temperature of each part rises quickly with good balance. As a result, there is no waste of fuel and the temperature rise time is shorter than in the prior art.

  At the beginning of the rapid heating operation, the heat medium cooled from the transfer device 6 enters the preheater 2 due to the resumption of the heat carrier circulation, so that the temperature in the preheater 2 may be excessively lowered. Therefore, at the same time as immediately before or after the start of circulation of the heat carrier in the rapid heating operation, an operation of increasing at least one of the hot air supply amount and the supplied hot air temperature to the preheater 2 to alleviate or prevent the temperature drop of the preheater 2 In particular, it is preferable to prevent the temperature drop of the preheater 2 by increasing the hot air supply amount while keeping the hot air temperature constant. In the latter case, the supply amount of auxiliary fuel and the supply amount of combustion air in the hot air generation device 1 are increased so that the temperature of the generated hot air does not change. When the hot air generator 1 performs an automatic operation using the temperature of the combustion exhaust gas as an index, the supply amount of the auxiliary fuel is automatically controlled, so that only an operation for increasing the amount of combustion air is required. As long as this operation is a rapid heating operation, this operation can also be used for a hot start described later.

(B) Standby operation In the DSS operation, for example, when the normal operation is finished in the evening and the normal operation starts from the next day's business time, the plant is kept at the normal operation temperature so that the next operation can be surely started from the scheduled time. It may be desirable to put it on standby. On the other hand, once the plant fire is extinguished, the temperature difference from the outside air is large, so it becomes impossible to quickly cool the higher temperature portion and quickly return to the steady operating temperature.

Therefore, in such a case, the temperature in the preheater, the reformer is changed by at least one of the following (ii) to (ha) from the state where the raw material supply is stopped until the raw material supply is started. The temperature at which the raw material can be supplied at any time by performing standby operation to maintain the internal temperature and the internal temperature of the thermal cracker at the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. It is preferable to keep the state.
(Ii) Stop the heat carrier circulation temporarily or continuously. Thereby, the temperature of each apparatus can be reduced by heat radiation.
(B) The heat carrier is circulated temporarily or continuously. Thereby, the temperature of each apparatus can be raised by heat supply.
(Ha) Increase or decrease at least one of the hot air supply amount and the supply hot air temperature to the preheater 2. Thereby, the degree of heating of the heat carrier can be changed.

  In the present invention, this operation method for maintaining the high temperature environment is called standby operation, and the operation of the hot air generator 1 and the hot air generator 1 to the preheater 2 with the raw material supply system and the generated gas system stopped. This is an operation method for continuing the supply of combustion exhaust gas and the circulation of the heat carrier. In the example shown in FIG. 14, this standby operation is performed between a cold start and a steady operation, and between a hot start and a steady operation described later.

  For example, in the case of DSS, after operating in order of water vapor supply stop, induction blower 11 stop, washing water circulation stop, without stopping hot air supply and heat carrier circulation, the preheater 2, the reformer 3, the thermal decomposer The heat supply to 4 is continued to prevent a temperature drop, and a standby state is maintained in which the raw material supply can be started at any time. When the operation is stopped in the evening, and the next morning, when the operation is started at the normal business time, the standby operation is approximately 15 hours. In addition, when the operation starts on the following Monday after the evening stop on Friday, the operation is on standby for about 63 hours. Further, even when the temperature rises earlier than the raw material supply start time and reaches the steady operation temperature, this operation method makes it possible to maintain the temperature.

  In this standby operation, the internal temperature of any one of the preheater 2, the reformer 3, and the pyrolyzer 4 may rise more than necessary. To prepare for such a case, the temperature rise is suppressed. It is preferable to carry out the overheat suppression operation described later.

(C) Application of high-speed temperature increase in hot start In operating a gasification system, it may be desired to temporarily stop operation and reduce labor. As a typical example, when generating electricity using the generated gas and selling power, the nighttime profits with low electricity purchase prices and high labor costs are drastically reduced, or the operation is closed on weekends and consecutive holidays. Can be mentioned. In such a temporary shutdown, if the system is cooled to some extent, it takes a long time to raise the temperature of the system to a state where it can be gasified again.

  For example, if this system stops the supply of raw materials before consecutive holidays and starts the supply of raw materials after the consecutive holidays several days later, once the system is stopped until hot air blowing is stopped, the internal temperature of the pyrolyzer However, in winter measurements from 2 ° C to 4 ° C, it cools from 500 ° C to 100 ° C in 24 hours. Even in the preheater 2 where the most heat remains, it is cooled to about the temperature in 5 to 6 days. Once the system has cooled down to about the temperature, it will be cold-started, so it takes a long time to start, and gasification will not begin immediately even after the temperature rises from the end of consecutive holidays. It will not be possible. In this case, it is conceivable to perform a stand-by operation, but the operation stop period is too long, resulting in an uneconomic operation.

  Therefore, when the system is temporarily stopped, a method is proposed in which the operation is not completely stopped from the steady operation, but is shifted to the heat insulation operation as shown in FIG. 14, and then the operation is resumed from the heat insulation operation. In the steady operation, the temperature in the preheater 2, the temperature in the reformer 3, and the temperature in the thermal decomposer 4 become the preheater steady operation temperature, the reformer steady operation temperature, and the thermal decomposer steady operation temperature. In the state where each has reached, supply of hot air to the preheater, circulation of the heat carrier, and supply of the organic material raw material are performed. From this state, the heat insulation operation is started, and after the supply of raw materials is stopped, the completion of gas generation is confirmed, the supply of water vapor to the reformer 3, the delivery of the generated gas by the induction blower 11 from the reformer 3, and the gas processing / utilization Although the facilities are respectively stopped, the operation of the hot air generator 1 and the supply of the combustion exhaust gas from the hot air generator 1 to the preheater 2 are continued. Since the supply of char to the hot air generator 1 is interrupted in a few hours as the raw material supply is stopped, the hot air generator 1 continues to operate with the auxiliary fuel.

  And in order to perform heat insulation efficiently, at least one of increase / decrease in the amount of heat supplied to the preheater 2 and increase / decrease in the circulation rate of the heat carrier is performed, and the temperature in the preheater 2 is lower than the steady operation temperature of the preheater and is predetermined. Above the lower limit temperature, the temperature in the pyrolyzer 4 is lower than the steady state operating temperature of the thermal decomposer and above the predetermined lower limit temperature, and the temperature in the reformer 3 is lower than the steady state operating temperature of the reformer and predetermined. Hold above the minimum temperature. This heat retention operation is based on the premise that the hot start high-speed temperature increase operation is started a predetermined time before the start of the next raw material (for example, 24 hours before), and the temperatures of the preheater 2, the reformer 3, and the thermal cracker 4 are set. The purpose is to keep it near the lower limit temperature. In a normal case, in order to quickly raise the preheater 2, the reformer 3, and the pyrolyzer 4 to a steady operation temperature (for example, in about 6 to 7 hours), the lower limit temperature of the preheater 2 is set to 750 ° C. The lower limit temperature of the reformer 3 is preferably 600 ° C., and the lower limit temperature of the pyrolyzer 4 is preferably 500 ° C.

  When the temperature of each device is lowered in the heat insulation operation, it is desirable to reduce the amount of heat supplied to the preheater 2 while maintaining the hot air temperature. In particular, the amount of auxiliary fuel supplied to the hot air generator 1 and the amount of air blown for combustion air It is desirable to reduce at least one of the above. Of course, the supplied hot air temperature may be lowered while maintaining the hot air supply amount, or both the hot air supply amount and the supplied hot air temperature may be reduced. Further, the circulation rate of the heat carrier is made slower than the standard, the hot air blowing is stopped until the temperature of each reactor drops to the above lower limit temperature, or both the hot air blowing and the circulation of the heat carrier are stopped, When the temperature drops to the lower limit temperature, it can be resumed.

  The preheater 2, the reformer 3, and the thermal decomposer 4 gradually enter a temperature lowering tendency by the above-described operations related to hot air and a heat carrier. At this time, there is basically no concern about overheating, but it is preferable to monitor the temperature drop of each unit just in case. When a situation occurs in which the pyrolyzer 4 exceeds the pyrolyzer steady operation temperature, the circulation of the heat carrier is temporarily stopped to reduce at least one of the temperature and the amount of hot air sent to the preheater 2, and the preheater The operation of lowering the temperature of the heat carrier at the outlet 2 is performed, and the temperature of the pyrolyzer 4 is cooled to a temperature equal to or lower than the steady-state operating temperature of the pyrolyzer, and then the circulation of the heat carrier is resumed.

  On the other hand, when the temperature of any vessel approaches or falls below the lower limit temperature, the temperature of the heat carrier that goes out of the preheater 2 is increased by operating in the direction of increasing the amount or temperature of hot air, and the circulation of the heat carrier is increased. Increase the amount of heat supplied to each unit as soon as possible. Even if the temperature of any of the reactors temporarily falls below the lower limit temperature in the heat insulation operation, the purpose of the heat insulation operation can be achieved if the temperature is restored to the lower limit temperature before the preheater temperature increase operation described below.

  When the operation is resumed, the heat carrier circulation is stopped from the heat retaining operation, and the operation proceeds to the above-described preheater temperature increasing operation. Then, after the temperature in the preheater 2 reaches the predetermined preheater steady operation temperature, the circulation of the heat carrier is restarted, and the temperature in the reformer 3 and the temperature in the thermal decomposer 4 are changed to the predetermined reformer. The aforementioned rapid heating operation is performed until the steady operation temperature and the pyrolyzer steady operation temperature are reached. By restarting the circulation of the heat carrier, the temperatures of the reformer 3 and the pyrolyzer 4 reach the steady operation temperature all at once. More specifically, the preheater heating operation is completed in a few hours, and during that time, the reformer 3 and the thermal decomposer 4 cause a temperature drop due to heat radiation cooling, but the heat carrier circulation is resumed and the reformer 3 is returned to. Is about 1000 ° C. from the preheater 2 and about 600 ° C. is dropped from the reformer to the pyrolyzer, so that the reformer 2 and the pyrolyzer 3 reach the appropriate temperature almost simultaneously.

  Thereafter, the supply of the organic material is resumed and gasification is started. In this way, the system is kept above a certain temperature by performing the heat insulation operation, and then restarting the system while suppressing energy consumption by restarting the raw material supply through the preheater temperature raising operation and the rapid heating operation of the present invention. It will be possible to do it promptly.

  During the heat insulation operation, the internal temperature of the preheater 2 is 700 ° C., the internal temperature of the reformer 3 is 600 ° C., and the internal temperature of the pyrolyzer 4 is around 500 ° C. From the temperatures, 1000 ° C., 950 ° C., Assuming a case where the temperature is raised to a steady operation temperature of 600 ° C., it is appropriate that the transition from the heat retention operation to the preheater temperature raising operation is started from 6 to 7 hours before the raw material supply scheduled start time. That is, the amount of heat carrier stored in each reactor is about one third of the total amount of heat carrier, and the total amount of heat carrier is assumed to be 4.7 tons, and the circulation amount of heat carrier is assumed to be 500 kilograms per hour. Then, the time for the total amount of the heat carrier of the preheater 2 to move to the reformer 3 is about 3 hours. Accordingly, the series of work time from the start of the preheater temperature rise to the steady operation temperature is about 6 hours, including the preheater temperature rise of about 3 hours. If the high temperature heating is started about 6 to 7 hours before the scheduled raw material charging time, the temperature can be sufficiently increased by the raw material charging scheduled time.

(D) Overheat suppression operation For example, since the circulation of the heat carrier is stopped during the preheater heating operation, the temperature in the preheater 2 reaches the preheater steady operation temperature, and the temperature further rises to increase the exhaust gas temperature of the preheater. May exceed the device limit temperature. Further, even during the standby operation, since each device has already reached the steady operation temperature, the temperature further increases, and the exhaust gas temperature of the preheater may exceed the device limit temperature. Of course, this is not without the danger during rapid heating operation and steady operation. Therefore, when the temperature in the preheater 2 reaches the preheater steady operation temperature and the exhaust gas temperature of the preheater 2 exceeds the device limit temperature (for example, about 550 ° C.), at least one of the following (A) to (D) It is desirable to perform an overheat suppression operation.
(B) When the circulation of the heat carrier is stopped, the circulation of the heat carrier is temporarily started. Thereby, the preheater 2 can be cooled by supplying the cooled heat carrier into the preheater 2.
(B) Temporarily or continuously, among the hot air supply amount and the supply hot air temperature to the preheater 2, the hot air supply amount is decreased while the supply hot air temperature is maintained. As a result, the amount of heat supplied to the preheater 2 can be reduced, and cooling can be performed using the cooling effect by heat radiation. When the hot air generator 1 performs an automatic operation using the temperature of the combustion exhaust gas as an index, the supply amount of the auxiliary fuel is automatically controlled, so that the temperature does not decrease by only reducing the amount of combustion air. The amount of heat decreases.
(C) Temporarily stop the supply of hot air to the preheater 2. Thereby, the amount of heat supplied to the preheater 2 can be eliminated, and cooling can be performed using the cooling effect by heat radiation to the maximum.
(D) Temporarily blow cooling air to the preheater 2. Thereby, forced cooling of the preheater 2 can be performed. As the cooling air, the combustion air supplied to the hot air generating device 1 can be used as it is (in the illustrated example, the temperature is close to the preheater exhaust gas temperature). This operation is applied in an emergency that cannot wait for heat radiation cooling.
By performing such an overheat suppression operation, it is possible to prevent overheating of the preheater 2 due to continued operation while suppressing a temperature drop of the preheater 2. It is desirable that this operation is applied in combination with a larger number of operations as the degree of excess is greater, and in this order (a) to (d), depending on the degree of excess of temperature. For example, when the circulation of the heat carrier (a) is resumed temporarily or continuously and the temperature in the preheater 2 does not decrease, the hot air supply amount to the preheater 2 is maintained and the hot air supply amount is reduced (B ) To (c) are performed to suppress overheating of the preheater 2 due to continuation of the preheater heating operation or the like. However, the temperature rise of the preheater 2 may still not be suppressed. Therefore, in such a case, it is preferable to perform the preheater cooling process as described in (2) above.

(E) Reset operation This system circulates a heat carrier in the system and uses heat storage in the preheater 2 and heat radiation in the reformer 3 and the thermal decomposer 4 to generate heat in the thermal decomposer 4. It is a system that performs thermal decomposition of organic substances and steam reforming in the reformer 3, but if the raw material is supplied too much to the thermal decomposer 4, the heat decomposer 4 is heated by an endothermic reaction and evaporation of moisture. When the temperature drop of the heat carrier occurs and this temperature drop exceeds the allowable range, as shown in FIG. 14, the heat carrier temperature enters a temperature drop spiral that decreases with each circulation. For example, in a normal case, the lower limit temperature allowable as the heat carrier temperature in the pyrolyzer 4 is about 500 ° C., and below this temperature, when returning to the preheater 2, it becomes 400 ° C. or less, and the temperature rises in the preheater 2. Due to the temperature limit, a vicious circle called a temperature lowering spiral occurs and the heat carrier cannot be returned to the steady operating temperature. And when it becomes such a low temperature state, the temperature of the reformer 3 is also not a temperature at which steam reforming can be performed, the steam reforming reaction disappears, and gas production only by simple thermal decomposition continues, The hydrogen concentration is low.

  Therefore, the following reset operation is also proposed as a method for getting out of such a vicious cycle of temperature decrease. That is, the temperature in the preheater 2, the temperature in the reformer 3, and the temperature in the thermal cracker 4 reach the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. When the temperature in the pyrolyzer 4 becomes less than the steady operating temperature of the pyrolyzer, particularly less than the lower limit temperature during steady operation in which hot air is supplied, heat carrier is circulated, and organic material feed is supplied. The raw material supply is stopped, the hot air is continuously blown, and the preheater heating operation is started. If the temperature in the preheater 2 is restored to the predetermined preheater steady operation temperature by this preheater heating operation, the heat carrier circulation is resumed, and the rapid heating operation is started. And the temperature in the pyrolyzer 4 are restored to a predetermined reformer steady-state operating temperature and thermal cracker steady-state operating temperature, respectively.

  When the temperature of each unit is restored to the steady operation temperature by this reset operation, the settings of the material supply systems 14 and 17 are changed so that the supply amount of the material that has caused the vicious cycle of the temperature decrease is less than that before the reset operation. After that, supply of raw materials is resumed. How much to reduce the amount of raw material supply can be determined as appropriate, but at first it will be greatly reduced (generally reduced from one-third to one-fourth), then gradually increase the supply amount and continue raw material supply However, it is preferable to adjust the temperature of the pyrolyzer 4 to an appropriate raw material supply amount that does not drop below the lower limit temperature.

(F) Post-processing operation When the system is stopped, if the heat carrier circulation is stopped immediately, a large number of heat carriers are solidified by the solidification of the tar dripped onto the pyrolyzer 4, and the next system start is started. In some cases, the heat carrier may be circulated. Therefore, when the system is stopped, the post-processing operation for continuing the circulation of the heat carrier and the supply of hot air to the preheater 2 in a state where the supply of the organic material raw material to the thermal decomposer 4 is stopped is performed for a predetermined time (for example, 2 hours). It is also proposed to stop the circulation of the heat carrier and the supply of hot air to the preheater 2 after the above. By performing this post-processing operation, even if tar is dripped in the pyrolyzer 4, the heat carrier heated by the hot air circulates, so that it is difficult to cause a solidified state.

  The present invention can be used for gasification of organic substances such as woody biomass.

  DESCRIPTION OF SYMBOLS 1 ... Hot air production | generation apparatus, 2 ... Preheater, 3 ... Reformer, 4 ... Thermal decomposition device, 5 ... Separator, 6 ... Transfer device.

Claims (9)

A number of heat carriers for carrying heat, a preheater for heating the heat carrier, a reformer for performing steam reforming of the pyrolysis gas, and pyrolysis for pyrolyzing the organic material raw material And a hot air generator for generating hot air,
The heat carrier is passed through the preheater, the reformer, and the thermal decomposer in this order, and then returned to the preheater by the transfer device and circulated, and the organic material raw material is supplied into the thermal decomposer, Supplying steam directly or indirectly into the reformer,
In the pyrolyzer, the organic material is pyrolyzed into char and pyrolysis gas by bringing it into contact with a heated heat carrier, and the pyrolysis gas is reformed in countercurrent contact with the heat carrier. Supply
In the reformer, a gas having an improved hydrogen-containing concentration is produced by bringing the pyrolysis gas into contact with the water vapor while being heated by the heat carrier,
In the hot air generator, hot air is generated and supplied to the preheater,
In the preheater, the hot air supplied from the hot air generator is passed between the heat carriers passing through the preheater in a deposited state, and the heat carrier is heated by directly contacting the heat carrier.
A method of fast heating in an organic material gasification system configured as follows:
In the state where supply of the organic material raw material to the pyrolyzer and circulation of the heat carrier are stopped, hot air is supplied from the hot air generator to the preheater, and a preheater heating operation is performed.
After the temperature in the preheater reaches a predetermined preheater steady operation temperature, the rapid heating operation for circulating the heat carrier while continuing the supply stop state of the organic material and the hot air supply state, Until the temperature in the reformer and the temperature in the pyrolyzer reach the predetermined reformer steady-state operating temperature and the thermal cracker steady-state operating temperature, respectively.
A method for rapidly raising temperature in a gasification system for organic substances.   2. The organic substance gas according to claim 1, wherein the preheater steady operation temperature is 1000 ° C. or more, the reformer steady operation temperature is 950 ° C. or more, and the pyrolyzer steady operation temperature is 550 ° C. or more. Method for rapid temperature increase in a computer system. At the time of cold start, the preheater, the reformer, and the thermal cracker are heated from the air temperature state to the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively.
Without supplying the organic material raw material and circulating the heat carrier, start supplying hot air to the preheater, and the hot air supply continues after the preheater temperature exceeds a predetermined temperature. Started circulating the heat carrier,
After the temperature inside the pyrolyzer reaches the pyrolyzer steady operation temperature due to the circulation of the heat carrier, the preheater heating operation is started,
After the preheater temperature increasing operation, the temperature in the preheater reaches the predetermined preheater steady operation temperature, and then the temperature in the reformer and the temperature in the pyrolyzer are the predetermined reformer steady operation temperature. 3. The high-speed heating method in the organic material gasification system according to claim 1, wherein the rapid heating operation is performed until reaching a steady operation temperature of the pyrolyzer, and then the supply of the organic material raw material is started. The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. From the steady operation of supplying hot air to the preheater, circulating the heat carrier, and supplying the organic material raw material,
In a state where the supply of the organic material raw material is stopped, at least one of increase / decrease in the amount of heat supplied to the preheater and increase / decrease in the circulation rate of the heat carrier is performed, and at least one of the hot air supply amount and the supply hot air temperature to the preheater is performed. The temperature in the preheater is lower than the steady operation temperature of the preheater and equal to or higher than a predetermined lower limit temperature, and the temperature in the thermal decomposer is lower than the steady operation temperature of the thermal decomposer and a predetermined lower limit temperature. After shifting to the heat retention operation, the temperature inside the reformer is lower than the reformer steady operation temperature and at or above a predetermined lower limit temperature,
After the temperature maintaining operation is shifted to the preheater temperature increasing operation and the temperature in the preheater reaches a predetermined preheater steady operation temperature, the temperature in the reformer and the temperature in the thermal decomposer are set to a predetermined value. The organic substance according to claim 1, wherein the rapid heating operation is performed until the steady state temperature of the reformer and the steady state temperature of the pyrolyzer are respectively reached, and then the supply of the organic material raw material is resumed, and a hot start is performed. Fast heating method in the gasification system. The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. From the state where the raw material supply is stopped until the raw material supply is started,
(Ii) Temporary or continuous stop of circulation of the heat carrier,
(B) Temporary or continuous execution of circulation of the heat carrier, and (ha) increase or decrease of at least one of hot air supply amount and supply hot air temperature to the preheater,
The temperature in the preheater, the temperature in the reformer, and the temperature in the pyrolyzer are changed to the preheater steady operation temperature, the reformer steady operation temperature, and the heat by the at least one operation of The high-speed temperature rising method in the gasification system of any one of Claims 1-4 which performs standby operation | maintenance each maintained to a cracker steady operation temperature. The temperature in the preheater, the temperature in the reformer, and the temperature in the thermal decomposer are the preheater steady operation temperature, the reformer steady operation temperature, and the thermal cracker steady operation temperature, respectively. When the temperature inside the pyrolyzer becomes less than the steady operation temperature of the pyrolyzer during steady operation in which the hot air is supplied, the heat carrier is circulated, and the organic material raw material is supplied. ,
After the preheater temperature increasing operation is performed and the temperature in the preheater reaches a predetermined preheater steady operation temperature, the temperature in the reformer and the temperature in the pyrolyzer are in a predetermined reformer steady operation. The rapid heating operation is performed until the temperature and the pyrolyzer steady operation temperature are reached, respectively, a reset operation is performed, and after the reset operation, the supply of the organic material raw material is resumed with a smaller supply amount than before the reset operation.
The high-speed temperature rising method in the gasification system of the organic substance of any one of Claims 1-5. When the preheater internal temperature reaches the preheater steady operation temperature and the exhaust gas temperature of the preheater exceeds the equipment limit temperature, the following:
(I) When the circulation of the heat carrier is stopped, the circulation of the heat carrier is temporarily started.
(B) Temporarily or continuously, among the hot air supply amount and supply hot air temperature to the preheater, the supply hot air temperature is maintained and the hot air supply amount is decreased.
(C) Temporarily stopping the supply of hot air to the preheater,
(D) Temporarily blow cooling air to the preheater,
Performing at least one overheat suppression operation of
The high-speed temperature rising method in the gasification system of the organic substance of any one of Claims 1-6.   8. The method according to claim 1, wherein at least one of a hot air supply amount and a supply hot air temperature to the preheater is increased simultaneously with, immediately before or immediately after the start of circulation of the heat carrier in the rapid heating operation. Fast heating method in organic material gasification system.   In stopping the system, in a state where the supply of the organic material raw material to the pyrolyzer is stopped, the heat carrier circulation and the hot air supply to the preheater are continued, and a post-processing operation is performed for a predetermined time. The high-speed temperature raising method in the organic material gasification system according to claim 1, wherein the circulation of the heat carrier and the supply of hot air to the preheater are stopped later.

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