JP2023085580A - Biomass gasification device - Google Patents

Abstract

To make a temperature of reformed gas approach a predetermined target temperature in a thermal decomposition gas reformer so as to stabilize reform reaction to stabilize hydrogen concentration.SOLUTION: A biomass gasification device includes: a preheater for preheating a heat carrier medium; a thermal decomposition device for receiving supply of the heat carrier medium having been preheated with the preheater and executing thermal decomposition of a biomass with heat of the heat carrier medium; and a thermal decomposition gas reformer for partially combusting a thermally decomposed gas generated by the thermal decomposition with air or oxygen to execute steam reform. Therein, the thermal decomposition gas reformer includes: a manual valve for always supplying a predetermined amount of oxygen to the thermal decomposition gas reformer; and an on-off valve for supplying in an on-off manner (intermittently) oxygen to the thermal decomposition gas reformer.SELECTED DRAWING: Figure 4

Description

The present invention relates to a biomass gasifier, more particularly, a biomass pyrolyzer for pyrolyzing biomass, preferably biomass with a relatively high ash content, and heat disposed above the biomass pyrolyzer. Equipped with a preheater for preheating the carrier medium, and a pyrolysis gas reformer for partially combusting and reforming the pyrolysis gas generated in the biomass pyrolyzer by mixing it with oxygen or air and steam. In a biomass gasification apparatus, the pyrolysis gas reformer has a manual valve that constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and a manual valve that supplies oxygen to the pyrolysis gas reformer by turning on and off. It relates to a biomass gasifier with a control device with a supply on-off valve.

After the Great East Japan Earthquake that occurred on March 11, 2011, renewable energy and distributed energy supply facilities were reviewed, and renewable energy such as solar power, wind power, geothermal power, hydro power, tidal power, biomass power, etc. Power generation facilities are attracting attention. Recently, attention has also been focused on the production of hydrogen through electrolysis of water using electricity generated by renewable energy.

Among renewable energies, photovoltaic power generation, wind power generation, and tidal power generation are expected as temporary power supply sources, but cannot be expected as stable power supply facilities because the amount of power generation is not stable. In addition, hydroelectric power generation and tidal power generation are expected to have a certain level of demand for small-scale facilities, but there is a problem that installation sites are limited in order to construct large-scale facilities.

On the other hand, biomass such as wood, sewage sludge, and livestock manure is evenly distributed in Japan. Among them, sewage sludge and livestock manure are considered to be stable biomass raw materials because they are generated continuously with little seasonal variation. In particular, the amount of sewage sludge generated is about 2.15 million tons (dry weight basis, amount generated in 2015, according to Ministry of Land, Infrastructure, Transport and Tourism materials), of which 75% by weight is unused, so effective utilization is expected. It is

However, sewage sludge contains nitrogen, phosphorus, potassium and other inorganic substances, as well as soil derived from rainwater. It has the disadvantage of low efficiency. In addition, nitrogen-derived N ₂ O is generated during combustion. The global warming potential of N ₂ O is 298 times that of CO ₂ (since 2013, the global warming potential of N ₂ O has been changed from 310 times to 298 times that of CO _2. Source: Ministry of the Environment) ), and in order to suppress the generation of N ₂ O, combustion must be performed at a high temperature of 850° C. or higher. Phosphorus, on the other hand, becomes diphosphorus pentoxide when burned. Since this diphosphorus pentoxide is highly sublimable and also deliquescent, it is known to cause a clogging effect at low temperature parts of piping. Besides diphosphorus pentoxide, potassium is also known to promote plugging and corrosion of piping. Therefore, when burning sewage sludge, it is necessary to perform combustion or heat treatment under conditions that suppress the volatilization of diphosphorus pentoxide and potassium while suppressing the generation of N ₂ O and diphosphorus pentoxide. .

For gasifiers for high-ash biomass, for example, after drying sewage sludge with an ash content of 20% by weight, it is thermally decomposed at 500 to 800 ° C in an air-blown fluidized bed pyrolysis furnace, and the pyrolysis gas is A method of burning with air at a high temperature of 1,000 to 1,250 ° C. and generating steam with the heat to generate turbine power (Patent Document 1), high ash biomass as a raw material, air blowing type circulating flow heating It is pyrolyzed in a furnace at a temperature of 450 to 850°C, and the char, which is a pyrolysis residue, is recovered by a cyclone, while the pyrolysis gas containing tar is reformed at 1,000 to 1,200°C in the presence of oxygen. In order to prevent the fluidized medium from sticking (Patent Document 2), after separating the char by pyrolysis in the same manner, the char is granulated and fed into the circulating fluidized reforming furnace, 900- A method of producing a granulated sintered body by sintering at a temperature of 1000° C. (Patent Document 3) and the like are disclosed.

A method using a heat carrier medium is also disclosed as a method for gasifying organic substances such as woody biomass. In this method, the heat carrier medium is preheated to a high temperature in the preheater, and dropped in the reformer and then in the thermal decomposer. The cracked gas and the heat carrier medium are brought into direct contact to reform the pyrolysis gas to achieve low tar and high hydrogen concentration in the gas, and then in the pyrolyzer, biomass and the heat carrier medium are brought into direct contact with each other to thermally decompose the biomass to generate pyrolysis gas.

In another method, a number of heat-bearing media such as alumina balls (approximately 10 mm in diameter) for transporting heat, a preheater for heating the heat-bearing media, and steam reforming of the pyrolysis gas. a reformer for performing the above, a pyrolyzer for pyrolyzing the woody biomass raw material, a separator for separating the heat carrier medium and the char, and a hot blast furnace for burning the char to generate hot air , and a device in which the preheater, reformer and thermal cracker are arranged vertically in order from the top (Patent Document 4).

In addition, based on the fact that the pyrolyzer in the pyrolysis zone and the gas reformer in the reaction zone are provided separately and independently, it is characterized by being able to configure either a series connection type or a parallel connection type. A device has also been proposed. For example, a circulating heat carrier medium passes through a heating zone of about 1,100° C., a reaction zone of 950-1,000° C., a pyrolysis zone of 550-650° C. and a separation step, and then returns to the heating zone to Immediately after leaving the cracking reactor, the pyrolysis coke obtained by separating the mixture of the pyrolysis coke and the heat carrier medium is burned in a combustion device, and the sensible heat generated thereby is used to produce heat in the heating zone. A method for producing a product gas with a high calorific value from organic substances and mixtures of substances by heating a heat carrier medium is disclosed in US Pat.

Furthermore, the pyrolysis gas introduction pipe for introducing the pyrolysis gas from the biomass pyrolyzer to the pyrolysis gas reformer is placed on the side of the biomass pyrolyzer by a preheated heat carrier medium formed in the biomass pyrolyzer. A gasification method is disclosed (US Pat. No. 6,300,008) which is installed on the side of the biomass pyrolyzer below the top of the bed. In this method, the gas inlet (gas inlet) of the pyrolysis gas introduction pipe is provided in the heat carrier medium layer, and the heat carrier medium in the biomass pyrolyzer is introduced into the pyrolysis gas introduction pipe, whereby heat is generated. A method is adopted in which the cracked gas passes through the heat carrier medium layer held in the pyrolysis gas introduction pipe, and the pyrolysis temperature of biomass, preferably biomass with a relatively high ash content, and the reforming of the generated pyrolysis gas. By optimizing the quality temperature and the atmosphere of these pyrolysis and reforming, finally a reformed gas containing a large amount of valuable gas such as hydrogen is generated, and the pentoxide contained in the ash in the biomass is generated. It is disclosed that it is possible to prevent clogging and corrosion of piping caused by volatilization of diphosphorus and potassium (potassium), suppress generation of N ₂ O, and reduce the amount of tar and dust generation. It is

In the gasification method comprising a preheater, a thermal decomposer, and a gas reformer as described above and utilizing the heat of the heat carrier medium heated by the preheater, the heat heated by the hot air in the preheater The carrier medium is dropped into a pyrolyzer and mixed with biomass such as wood chips to generate biogas. Control of the temperature of the reformed gas in the gas reformer was performed by varying the flow rate of the oxygen gas with an automatic valve through proportional control (see FIG. 2).

JP-A-2002-322902 JP-A-2004-51745 Japanese Patent No. 4155507 JP 2011-144329 A Japanese Patent No. 4264525 JP 2019-65160 A

However, in the oxygen supply system of the conventional pyrolysis gas reformer, when the biogas temperature rises from 600 ° C. to 1000 ° C. at the reformer outlet, it takes time for the thermometer to detect the predetermined temperature. . Although enough oxygen gas has already been supplied to reach the predetermined temperature of 1000° C., the temperature is not detected. There was a problem that the temperature became 1000° C. or higher. On the other hand, when the temperature exceeds 1000° C., the automatic valve begins to close and the oxygen gas supply begins to decrease. Since the temperature drop is not easily detected, even though the oxygen gas amount is sufficiently reduced when the temperature drops below 1000°C, the oxygen gas amount decreases further, and by the time the temperature is detected, the temperature drops significantly. There was a problem. As described above, since the temperature fluctuates greatly (see FIG. 3), the reforming reaction is affected and the hydrogen concentration fluctuates greatly.

As a result of repeated studies to solve the above-mentioned problems of the conventional technology, the inventors of the present invention divided the supply of oxygen gas into two, and the opening is always constant from the manual valve side, which is a fixed valve whose opening is variable. By supplying a large amount of oxygen gas and controlling the temperature of the reformed gas to around 1000°C by supplying oxygen gas through an on-off valve, the temperature of the pyrolysis gas reformer fluctuates greatly, which affects the reforming reaction. It has been found that the above-mentioned problems such as the inability to stably extract hydrogen due to large fluctuations in the hydrogen concentration can be solved.

That is, the present invention is as follows.
[1]
a preheater for preheating the heat carrier medium;
A pyrolyzer that is supplied with a heat carrier preheated by the preheater and performs pyrolysis of biomass using the heat of the heat carrier, and a pyrolysis gas generated by the pyrolysis is replaced by air or oxygen. a pyrolysis gas reformer that performs steam reforming with partial combustion by
In a biogas gasifier comprising
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier.
[2]
The biomass gasification apparatus according to [1], wherein the temperature of the reformed gas is raised to a predetermined temperature range of 900° C. or lower by supplying oxygen gas from the manual valve.
[3]
The biomass gasifier according to [2], wherein the predetermined temperature range is from 800°C to 900°C.
[4]
The biomass gasifier according to [2], wherein the predetermined temperature range is from 850°C to 880°C.
[5]
Biomass of [1] to [4], wherein the temperature of the reformed gas is raised to the target temperature by supplying oxygen gas from the on-off valve in addition to the temperature rise of the reformed gas by the manual valve. gasifier.
[6]
The biomass gasifier of [5], wherein the target temperature is 850°C to 1000°C.
[7]
The biomass gasifier of [5], wherein the target temperature is 880°C to 950°C.
[8]
The biomass gasifier of [5], wherein the target temperature is 900°C to 930°C.
[9]
The biomass gasifier according to [2] to [8], wherein the predetermined temperature range is adjusted based on the reached temperature of the reformed gas.
[10]
the biomass pyrolyzer comprises a biomass inlet and a non-oxidizing gas inlet and/or steam inlet;
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas provided between the biomass pyrolyzer and the pyrolysis gas reformer for introducing the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer including an introduction tube;
In addition, the biomass pyrolyzer and the pyrolysis gas reformer each further include an inlet and an outlet for a preheated heat carrier unit, and the heat possessed by the heat carrier unit thermally decomposes biomass and Execute reforming of pyrolysis gas generated by pyrolysis of biomass,
The biomass pyrolyzer and the pyrolysis gas reformer are provided in parallel with respect to the flow of the heat carrier medium, and the pyrolysis gas introduction pipe is connected to the biomass pyrolyzer and the heat said biomass pyrolyzer and said pyrolysis gas below the upper surface of said heat-carrying medium layer respectively formed in said biomass pyrolyzer and said pyrolysis gas reformer on both sides of the cracker gas reformer; A biomass gasification apparatus provided on the side of a reformer and having the pyrolysis gas introduction pipe substantially horizontal with respect to the direction of gravity,
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier.
[11]
the biomass pyrolyzer comprises a biomass inlet and a non-oxidizing gas inlet and/or steam inlet;
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas introduction pipe is provided between the biomass pyrolyzer and the pyrolysis gas reformer, and the pyrolysis gas generated in the biomass pyrolyzer is transferred to the pyrolysis gas reformer. and the biomass pyrolyzer further comprises an inlet and an outlet for a preheated heat carrier medium for carrying out pyrolysis of biomass with the heat of the heat carrier medium,
On the other hand, the pyrolysis gas reformer performs steam reforming of pyrolysis gas generated by pyrolysis of biomass,
The pyrolysis gas reformer further comprises an air or oxygen inlet, and steam reforming is performed by partially burning the pyrolysis gas generated by the pyrolysis of biomass with the air or oxygen,
The biomass gasifier, wherein the pyrolysis gas introduction pipe is provided on the side surface of the biomass pyrolyzer below the upper surface of the heat carrier medium layer formed in the biomass pyrolyzer. There is
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier.
[12]
A biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam, and reforming the gas generated in the biomass pyrolyzer in the presence of steam. A thermal decomposition gas reformer and a preheated heat support unit are introduced into the biomass pyrolyzer, and the heat of the heat support unit thermally decomposes biomass, and then, introducing the pyrolysis gas generated by pyrolysis of the biomass into the pyrolysis gas reformer to perform steam reforming of the pyrolysis gas;
A pyrolysis gas introduction pipe provided on a side surface of the biomass pyrolyzer below the upper surface of the heat-supporting single layer, in which pyrolysis gas generated by pyrolysis of the biomass is formed in the biomass pyrolyzer. The introduced pyrolysis gas is partially oxidized by air or oxygen separately introduced into the pyrolysis gas reformer through At the same time, in the biomass gasification method, wherein the biomass is reformed by steam introduced at the same time as the air or oxygen,
The temperature of the reformed gas is raised to a predetermined temperature region by oxygen from a manual valve provided in the pyrolysis gas reformer, which constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and A biomass gasification method, wherein the temperature of the reformed gas is raised to a predetermined target temperature by oxygen from an on-off valve that supplies oxygen to a pyrolysis gas reformer in an on-off state.

According to the present invention, a preheater for preheating a heat carrier medium, a pyrolyzer for receiving a supply of the heat carrier medium preheated by the preheater and thermally decomposing biomass with the heat of the heat carrier medium, and In a biogas gasification apparatus including a pyrolysis gas reformer that performs steam reforming by partially combusting the pyrolysis gas generated by the pyrolysis with air or oxygen, By incorporating a manual valve for supplying a predetermined amount of oxygen and an on-off valve for supplying oxygen to the pyrolysis gas reformer in an on-off state into the pyrolysis gas reformer, reforming in the pyrolysis gas reformer It is possible to provide a biomass gasifier capable of stably supplying hydrogen by bringing the temperature of the gas closer to the predetermined target temperature, stabilizing the reforming reaction and stabilizing the hydrogen concentration.

FIG. 1 is a schematic diagram showing one form of a biomass gasifier. FIG. 2 is a diagram showing an oxygen supply system of a pyrolysis gas reformer in a biomass gasifier. FIG. 3 is a diagram showing the temperature of the pyrolysis gas over time in the oxygen supply system of the pyrolysis gas reformer in the biomass gasifier. FIG. 4 is a schematic diagram showing an embodiment of the oxygen supply system of the pyrolysis gas reformer in the biomass gasifier of the present invention. FIG. 5 is a diagram showing an oxygen supply control device for the pyrolysis gas reformer in the biomass gasifier of the present invention.

(I) Pyrolysis gas reformer in the biomass gasifier according to the present invention The biomass gasifier of the present invention includes a preheater for preheating a heat carrier medium, and a heat carrier medium preheated by the preheater. A pyrolyzer that thermally decomposes biomass using the heat of the heat carrier medium, and partially combusts the pyrolysis gas generated by the thermal decomposition with air or oxygen to perform steam reforming. A biomass gasification apparatus comprising a cracked gas reformer, wherein the pyrolysis gas reformer constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer; and an on/off valve for supplying oxygen to the vessel in an on/off state. As a result, the temperature of the reformed gas in the pyrolysis gas reformer is brought closer to the predetermined target temperature, the reforming reaction is stabilized, and the hydrogen concentration is stabilized, thereby stably supplying hydrogen.

The heat carrier medium (also referred to as "heat carrier") is a plurality of particulates and/or lumps, preferably made of one or more materials selected from the group consisting of metals and ceramics. The metal is preferably selected from the group consisting of iron, stainless steel, nickel alloy steel, and titanium alloy steel, and more preferably stainless steel. The ceramic is selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia and silicon nitride, more preferably alumina.

The shape of the heat carrier medium is preferably spherical (ball), but does not necessarily have to be a true sphere, and may be a sphere having an elliptical or oval cross-sectional shape. The diameter (maximum diameter) of the sphere is preferably 3 to 25 mm, more preferably 8 to 15 mm. If the above upper limit is exceeded, the fluidity inside the biomass pyrolyzer, that is, the free-falling property may be impaired, and as a result, the spherical objects may stop inside the biomass pyrolyzer and cause clogging. be. On the other hand, below the above lower limit, in the biomass pyrolyzer, the spheroids themselves may stick due to tar, dust, etc. adhering to the spheroids, which may cause clogging. For example, if the diameter of the spherical object is less than 3 mm, the spherical object adheres to the inner wall of the biomass pyrolyzer and grows due to the influence of tar and dust attached to the spherical object, and in the worst case, biomass pyrolysis. There is concern that the device may be clogged. In addition, when the tar-adhered spherical objects are extracted from the valve at the bottom of the biomass pyrolyzer, the spherical objects less than 3 mm are light and adhere to the inside of the valve without falling due to the tar. may contribute to obstruction.

The biomass of the present invention refers to so-called biomass resources. Here, biomass resources refer to plant-based biomass, for example, thinned wood discarded from forestry, lumber waste, pruned branches, forestry residue, unused trees, etc., agricultural crops such as vegetable residues and fruit tree residues discarded from agriculture. , rice straw, wheat straw, rice husks, etc., other marine plants, construction waste wood, etc.; biological biomass, such as livestock manure and biological manure represented by sewage sludge; etc. The apparatus of the invention is preferably suitable for gasification of plant biomass and biological biomass. Among them, high-ash biomass having an ash content of preferably 5.0% by mass or more, more preferably 10.0 to 30.0% by mass, and even more preferably 15.0 to 20.0% by mass on a dry basis; It is especially suitable for gasification of sewage sludge and livestock manure.

One embodiment of a biomass gasifier comprises a preheater, a pyrolyzer, and a pyrolysis gas reformer, as shown in FIG. The heat carrier medium preheated in the preheater is supplied by free fall from the preheater through a valve to the heater. Within the heater, the heat carrier medium causes pyrolysis of the biomass fed into the heater with its own heat. The generated pyrolysis gas passes through the pyrolysis gas introduction pipe and is introduced into the pyrolysis gas reformer. The heat carrier medium in the pyrolyser is discharged from the pyrolyser by free fall through a valve and preferably recirculated to the preheater.

A pyrolysis gas produced by pyrolyzing biomass in the biomass pyrolyzer is introduced into the pyrolysis gas reformer through a pyrolysis gas introduction pipe. The pyrolysis gas introduced into the pyrolysis gas reformer is partially oxidized by air or oxygen, thereby heating the inside of the pyrolysis gas reformer. As a result, the pyrolysis gas and steam react to reform the pyrolysis gas into hydrogen-rich gas.

In addition, oxygen or air is used at one or more locations selected from the group consisting of the pyrolysis gas reformer and its vicinity, and the pyrolysis gas introduction pipe between the biomass pyrolyzer and the pyrolysis gas reformer. It is introduced from the oxygen or air supply port provided in the.

The gas phase temperature in the pyrolysis gas reformer has an upper limit of preferably 1,000°C, more preferably 950°C, and still more preferably 930°C, and a lower limit of preferably 850°C, more preferably 880°C. More preferably, it is 900°C. Below the above lower limit, the reforming reaction may not progress. It can also be a factor that generates N ₂ O. On the other hand, even if the above upper limit is exceeded, a significant increase in the effect cannot be expected, and the amount of heat required for heating increases, leading to an increase in cost.

When the gas phase temperature in the pyrolysis gas reformer is 850° C. or higher, which is the preferred lower limit value, the reforming of carbon monoxide by steam becomes remarkable, and when the gas phase temperature is 880° C. or higher, which is the more preferred lower limit value, methane is converted by steam. The modification of becomes remarkable. Therefore, in order to efficiently reform both carbon monoxide and methane, it is more preferable that the gas phase temperature in the pyrolysis gas reformer is 880° C. or higher. A more preferable upper limit of the gas phase temperature in the pyrolysis gas reformer is 950°C, and the pyrolysis gas can be sufficiently reformed at this temperature or lower. It is even more preferable to have

Here, the gas phase temperature of the pyrolysis gas reformer means the temperature of the pyrolysis gas introduced into the pyrolysis gas reformer and the mixture of steam and air or oxygen. This is the vapor phase temperature inside the reformer. The gas phase temperature of the pyrolysis gas reformer can be appropriately controlled by the amount of air or oxygen supplied.

(II) Oxygen supply in the pyrolysis gas reformer of the present invention In the pyrolysis gas reforming of the biomass gasifier of the present invention, the supply of oxygen gas is divided into two, and a constant amount of oxygen is always supplied from the manual valve. Gas is supplied to raise the temperature of the reformed gas to a predetermined temperature range, preferably 800° C. to 900° C., and the temperature of the reformed gas is controlled to around 1000° C. of the target temperature by supplying oxygen gas from the on-off valve. can be done. The manual valve refers to a valve whose degree of opening is variable and fixed after adjustment, and may be an automatic valve or a manual valve. Anything is fine. The on-off valve refers to a valve such as a solenoid valve, an electric valve, an air valve, etc., which has only two positions of valve opening, fully open/fully closed.

That is, by supplying oxygen gas from a manual valve, the temperature of the reformed gas is raised to a predetermined temperature, preferably from 800° C. to 900° C., the difference from the target temperature is reduced in advance, and the time required to reach the target temperature is decrease. As a result, excessive supply of oxygen gas by the on/off valve can be prevented, and the temperature exceeding the target temperature of 1000° C. can be suppressed as much as possible. Further, even if the temperature exceeds the target temperature of 1000° C. and the on-off valve closes and the temperature drops, the automatic valve keeps supplying the oxygen gas constantly, so the temperature does not drop below the maintained temperature. By doing so, the temperature of the reformed gas can be controlled to the vicinity of the predetermined target temperature of 1000.degree.

In the supply of oxygen gas by the manual valve, the predetermined temperature range of 900°C or lower is preferably 800°C to 900°C, more preferably 850°C to 880°C. By setting the temperature range close to 900° C., it becomes possible to reach the target temperature around 1000° C. by the on/off valve.

In addition to the temperature rise of the reformed gas by the manual valve, the supply of oxygen gas from the on-off valve can raise the temperature of the reformed gas to the target temperature. The target temperature is preferably 850°C to 1000°C, more preferably 880°C to 950°C, even more preferably 900°C to 930°C. A target temperature in the vicinity of 1000° C., which does not exceed 1000° C. as much as possible, prevents excessive supply of oxygen by the on/off valve and enables stable supply of hydrogen.

It is also possible to feed back and adjust the predetermined temperature range based on the actual temperature attained through adjustment by the manual valve and the on/off valve. This adjustment brings the temperature of the reformed gas in the cracked gas reformer closer to the target temperature, stabilizes the reforming reaction, and stabilizes the hydrogen concentration, thereby stably supplying hydrogen.

The biomass gasifier of the present invention can be provided with a control device for adjusting the pyrolysis gas reformer. The control device includes a detector that detects the temperature of the reformed gas in the pyrolysis gas reformer, a temperature detector that detects the temperature from the detector, an on-off valve adjuster that adjusts the opening and closing of the on-off valve, and the opening and closing of the manual valve. An automatic valve regulator for adjusting the degree of flow, a control unit for commanding the operation of the switch and the regulator, and a calculation unit for performing calculations for the feedback control can be provided.

The above aspects of the feed control device in the biomass gasifier of the present invention can be incorporated into a conventional biomass gasifier.

(III) one aspect of the biomass gasification apparatus according to the present invention, wherein the biomass pyrolyzer has a biomass supply port and a non-oxidizing gas supply port and/or steam inlet;
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas provided between the biomass pyrolyzer and the pyrolysis gas reformer for introducing the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer including an introduction tube;
Further, the biomass pyrolyzer and the pyrolysis gas reformer each further comprise an inlet and an outlet for a preheated heat carrier medium, and the heat possessed by the heat carrier medium thermally decomposes biomass and Execute reforming of pyrolysis gas generated by pyrolysis of biomass,
The biomass pyrolyzer and the pyrolysis gas reformer are provided in parallel with respect to the flow of the heat carrier medium, and the pyrolysis gas introduction pipe is connected to the biomass pyrolyzer and the heat said biomass pyrolyzer and said pyrolysis gas below the upper surface of said heat-carrying medium layer respectively formed in said biomass pyrolyzer and said pyrolysis gas reformer on both sides of the cracker gas reformer; A biomass gasification apparatus provided on the side of a reformer and having the pyrolysis gas introduction pipe substantially horizontal with respect to the direction of gravity,
The pyrolysis gas reformer may include a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer in an on-off state. can.

(IV) One aspect of the biomass gasifier according to the present invention The biogas gasifier according to the present invention is characterized in that the biomass pyrolyzer has a biomass supply port and a non-oxidizing gas supply port and/or steam. Equipped with an air outlet,
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas introduction pipe is provided between the biomass pyrolyzer and the pyrolysis gas reformer, and the pyrolysis gas generated in the biomass pyrolyzer is transferred to the pyrolysis gas reformer. introduced into
and the biomass pyrolyzer further comprises an inlet and an outlet for a preheated heat carrier medium, and uses the heat of the heat carrier medium to carry out pyrolysis of biomass,
On the other hand, the pyrolysis gas reformer performs steam reforming of pyrolysis gas generated by pyrolysis of biomass,
The pyrolysis gas reformer further comprises an air or oxygen inlet, and steam reforming is performed by partially burning the pyrolysis gas generated by the pyrolysis of biomass with the air or oxygen,
The biomass gasification apparatus, wherein the pyrolysis gas introduction pipe is provided on a side surface of the biomass pyrolyzer below an upper surface of the heat carrier medium layer formed in the biomass pyrolyzer. ,
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier.
Since the biomass pyrolyzer and the pyrolysis gas reformer are separated from the flow of the heat carrier medium, their respective temperatures can be controlled separately.

(V) Biomass gasification method according to the present invention Another aspect of the present invention is a biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or in a mixed gas atmosphere of non-oxidizing gas and steam. and a pyrolysis gas reformer that reforms the gas generated in the biomass pyrolyzer in the presence of steam, and a preheated heat carrier medium is introduced into the biomass pyrolyzer. , pyrolysis of biomass is performed by the heat of the heat carrier medium, and then the pyrolysis gas generated by the pyrolysis of the biomass is introduced into the pyrolysis gas reformer to produce the pyrolysis gas. perform steam reforming,
A pyrolysis gas introduction pipe provided on a side surface of the biomass pyrolyzer below the upper surface of the heat carrying medium layer, in which pyrolysis gas generated by pyrolysis of the biomass is formed in the biomass pyrolyzer. The introduced pyrolysis gas is partially oxidized by air or oxygen separately introduced into the pyrolysis gas reformer through At the same time, in the biomass gasification method, wherein the biomass is reformed by steam introduced at the same time as the air or oxygen,
The temperature of the reformed gas is raised to a predetermined temperature region by a manual valve provided in the pyrolysis gas reformer, which constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and in addition, the pyrolysis gas This is a biomass gasification method in which the temperature of the reformed gas is raised to a target temperature by an on-off valve that supplies oxygen to the reformer in an on-off state.

The biomass gasifier of the present invention will be described below with reference to the accompanying drawings.

FIG. 1 is a schematic diagram showing the form (III) of the biomass gasifier according to the present invention. In the biomass gasifier, a biomass pyrolyzer (20) for carrying out pyrolysis of biomass with the heat of a heat carrier (30) preheated in a preheater (10), i.e. a heat carrier; A pyrolysis gas reformer ( 40) are provided. A preheater (10) for preheating the heat carrier medium (30) is provided above the biomass pyrolyzer (20).

In the biomass gasifier of the present invention, the heat carrier medium (30), ie the heat carrier, is preheated in the preheater (10) before being introduced into the biomass pyrolyzer (20). The heat carrier medium (30) is preferably heated to 650-800°C, more preferably 700-750°C. Below the above lower limit, biomass, for example, high-ash biomass cannot be sufficiently pyrolyzed in the biomass pyrolyzer (20), and the amount of pyrolysis gas generated decreases. On the other hand, if the above upper limit is exceeded, volatilization of phosphorus and potassium (potassium) is caused, which causes clogging and corrosion of piping due to diphosphorus pentoxide and potassium (potassium). In addition, it only provides extra heat, and a remarkable increase in effect cannot be expected. Moreover, it also causes the thermal efficiency of the equipment to decrease.

The heat carrier medium (30) heated to the predetermined temperature in the preheater (10) is then introduced into the biomass pyrolyzer (20). In the biomass pyrolyzer (20), the heat carrier medium (30) is separately contacted with biomass supplied to the biomass pyrolyzer (20) through a biomass feed port (220). The contact of the heat carrier medium (30) with the biomass heats and pyrolyzes the biomass to produce pyrolysis gases. The generated pyrolysis gas passes through the pyrolysis gas introduction pipe (200) and is introduced into the pyrolysis gas reformer (40). At this time, the tar, dust, etc. contained in the generated pyrolysis gas are captured by the heat carrier medium (30) held in the pyrolysis gas introduction pipe (200), and part or most of the tar is thermally carried. The medium (30) is manually heated and gasified, and the remaining tar, dust, etc. are discharged from the bottom of the biomass pyrolyzer (20) while adhering to the heat carrier medium (30).

The pyrolysis gas produced by pyrolyzing biomass in the biomass pyrolyzer (20) is introduced into the pyrolysis gas reformer (40) through the pyrolysis gas introduction pipe (200). The pyrolysis gas introduced into the pyrolysis gas reformer (40) is partially oxidized by air or oxygen, thereby heating the inside of the pyrolysis gas reformer (40). As a result, the pyrolysis gas and steam react to reform the pyrolysis gas into hydrogen-rich gas.

In the gasifier of the present invention, as already described, the pyrolysis gas introduced into the pyrolysis gas reformer is partially oxidized by the air or oxygen supplied from the air or oxygen inlet. Since steam reforming is performed by the heat generated thereby, the pyrolysis gas reformer is usually heated from outside and/or inside the pyrolysis gas reformer by a heating device such as steam or an electric heater. It is not equipped with a heating device or the like to supply heat.

In the pyrolysis gas reformer (40), the supply of oxygen gas is divided into two, and a constant amount of oxygen gas is always supplied from the manual valve (41) to keep the temperature of the reformed gas in a predetermined temperature range, preferably By raising the temperature to 800° C. to 900° C. and supplying oxygen gas from the on/off valve (42), the temperature of the reformed gas can be controlled to around 1000° C. of the target temperature.

That is, by supplying oxygen gas from the manual valve (41), the temperature of the reformed gas is raised to a predetermined temperature, preferably from 800°C to 900°C. reduce the time required for As a result, excessive supply of oxygen gas by the on/off valve (42) can be prevented, and the temperature exceeding the target temperature of 1000° C. can be suppressed as much as possible. Even if the target temperature exceeds 1000°C and the on/off valve closes and the temperature drops, the manual valve (41) supplies a constant amount of oxygen gas, so the temperature does not drop below the maintained temperature. By doing so, the temperature of the reformed gas can be controlled to the vicinity of the predetermined target temperature of 1000.degree.

As shown in FIG. 5, the pyrolysis gas reformer (40) of the biomass gasifier of the present invention further comprises a control device (43) for adjusting the pyrolysis gas reformer. be able to.

In the control device (43), the predetermined temperature range is adjusted by feedback based on the actual reached temperature obtained by the adjustment by the manual valve (41) and the on/off valve (42). A control device (43) for adjusting the pyrolysis gas reformer (40) can be provided. The control device (43) includes a detector (44) for detecting the temperature of the reformed gas in the reformer, a temperature detector (45) for detecting the temperature from the detector, and an on/off valve switch ( 46), a manual valve regulator (47) for adjusting the opening/closing degree of the manual valve (41), a controller (48) for commanding the operation of the switch and the regulator, and an arithmetic operation for executing the arithmetic operation for the feedback control. A part (49) is provided.

EXAMPLES The present invention will be described in more detail below with reference to examples, but the present invention is not limited to these examples. The present example illustrates an example of the form (III).

(Example 1)
The biomass raw material used in Example 1 and the gasifier used for thermal decomposition and gas reforming of the biomass raw material are as follows.

As a biomass raw material, granulated sewage sludge was used. The maximum size of the sewage sludge after granulation was about 6 to 15 mm. Table 1 shows the properties of the sewage sludge. Table 2 shows the composition of the ash obtained by burning the sewage sludge.

Regarding each value in Table 1, the moisture content, volatile content and fixed carbon were measured according to JIS M8812, the ash content was measured according to JIS Z 7302-4:2009, and the higher calorific value was measured according to JIS M8814. It is what I did. In addition, among the elemental compositions, carbon (C), hydrogen (H) and nitrogen (N) all conform to JIS Z 7302-8: 2002, and sulfur (S) conforms to JIS Z 730-7: 2002. and chlorine (Cl) is measured in accordance with JIS Z 7302-6:1999. Oxygen (O) is obtained by subtracting each mass % of C, H, N, S, Cl and ash from 100 mass %. Here, the ash content, volatile content, fixed carbon and elemental composition are all calculated on a dry basis. Also, the water content is that at the time of receiving the biomass raw material (sewage sludge).

Regarding each value in Table 2, silicon dioxide, aluminum oxide, ferric oxide, magnesium oxide, calcium oxide, sodium oxide, potassium oxide, diphosphorus pentoxide and manganese oxide were measured in accordance with JIS M8815. . Mercury, chromium, cadmium, copper oxide, lead oxide, zinc oxide and nickel were measured according to JIS Z 7302-5:2002.

As a gasifier used for pyrolyzing the biomass raw material and reforming the generated pyrolysis gas, the one shown in FIG. 1 is used. The gasifier basically comprises a biomass pyrolyzer (20), a pyrolysis gas reformer (40) and a preheater (10). The gas reformer (40) is connected by a pyrolysis gas introduction pipe (200) for introducing the pyrolysis gas generated in the biomass pyrolyzer (20) into the pyrolysis gas reformer (40). there is

Here, a preheater (10) is provided above the biomass pyrolyzer (20), and the preheater (10) supplies a heat carrier medium (30) to the biomass pyrolyzer (20). The heated heat carrier medium (30) is supplied to the biomass pyrolyzer (20) to supply the heat required for pyrolysis of the biomass and then withdrawn from the bottom. , is returned to the preheater (10) again. On the other hand, the pyrolysis gas generated in the biomass pyrolyzer (20) is introduced into the pyrolysis gas reformer (40) through the pyrolysis gas introduction pipe (200).

Here, air or oxygen is separately introduced into the pyrolysis gas reformer (40) from the air or oxygen introduction pipes (261, 262), thereby partially combusting the pyrolysis gas, and At the same time, steam is introduced through the steam inlet (242) to reform the pyrolysis gas by the steam, and the resulting reformed gas is taken out through the reformed gas outlet (230). In addition, air or oxygen and steam are provided in the pyrolysis gas introduction pipe (200) instead of the air or oxygen introduction pipe (261) and the steam inlet (242). 262) and steam inlets (243), or all air or oxygen inlets (261, 262) and steam inlets (242, 243).

The inner diameter of the straight body portion of the biomass pyrolyzer (20) is about 550 mm, the height is about 1,100 mm, and the internal volume is about 260 liters. The straight body portion of the pyrolysis gas reformer (40) has an inner diameter of approximately 600 mm, a height of approximately 1200 mm, and an internal volume of approximately 340 liters.

In addition, the pyrolysis gas introduction pipe (200), on the side of the biomass pyrolyzer (20), is used for pyrolysis of biomass below the upper surface of the heat carrier medium (30) layer formed in the biomass pyrolyzer (20). On the side of the pyrolysis gas reformer (40), on the side of the pyrolysis gas reformer (40). Also, the pyrolysis gas introduction pipe (200) is provided substantially horizontally with respect to the direction of gravity. As the pyrolysis gas introduction pipe (200), a pipe having a length of about 1,000 mm and an inner diameter of about 80 mm is used, the inside of which is covered with a heat insulating material, and the projecting portion is also formed of the heat insulating material. ing. A substantially spherical alumina ball having a diameter (maximum diameter) of 10 to 12 mm is used as the heat carrier medium (30).

The biomass pyrolyzer (20) and the preheater (10) are filled in advance with a heat carrier medium (30) to a height of about 70% of each container, and then the heat carrier medium (30) is filled with It was heated to a temperature of approximately 700° C. in the preheater (10). Then, the heat carrier medium (30) is introduced from the top of the biomass pyrolyzer (20) in an amount of 200 kg/hr, and an appropriate amount is withdrawn from the bottom of the biomass pyrolyzer (20), and the heat carrier medium is Start the circulation of (30).

The circulation of the heat carrier medium (30) gradually increases the gas phase temperature inside the biomass pyrolyzer (20) and the temperature of the vessel itself. While continuing such circulation of the heat carrier medium (30), the temperature of the heat carrier medium (30) inside the preheater (10) is gradually increased to 800°C. After the heat carrier medium (30) reaches the temperature, the circulation is continued to gradually increase the gas phase temperature inside the biomass pyrolyzer (20), and the gas phase of the biomass pyrolyzer (20) When the temperature exceeds 550° C., the biomass raw material and nitrogen gas are supplied from the biomass feed port (220), the non-oxidizing gas feed port (250) and the steam inlet (241) to the biomass thermal cracker (20), respectively. And steam is introduced, and the temperature of the biomass thermal cracker (20) is controlled to 600°C.

At this time, the heat carrier medium (30) is deposited in layers in the biomass pyrolyzer (20), and the deposition amount is about 60% by volume of the internal volume of the biomass pyrolyzer (20). The withdrawal rate of the heat carrier medium (30) from the biomass pyrolyzer (20) is the same as the feed rate, which is 200 kg/h in the biomass pyrolyzer (20). Also, the temperature of the heat carrier medium (30) at the time of extraction is 650°C. however. The amount of the heat carrier medium (30) withdrawn from the biomass pyrolyzer (20) can be appropriately controlled according to the temperature conditions.

In the above operation, sewage sludge as a biomass raw material is gradually increased from the biomass supply port (220) to the biomass pyrolyzer (20) using a constant feeder, and finally about 22 kg. / hour (dry basis).

The temperature of the biomass pyrolyzer (20) gradually decreases as the biomass raw material is introduced, while at the same time nitrogen gas and superheated steam are introduced into the biomass pyrolyzer (20) while adjusting their supply amounts. This keeps the temperature of the biomass pyrolyzer (20) at 600°C. Also, the pressure inside the biomass pyrolyzer (20) is kept at 101.3 kPa.

Here, nitrogen gas is finally introduced at a constant rate of 1,000 liters/hour from the non-oxidizing gas supply port (250) provided at the top of the biomass pyrolyzer (20). As steam, superheated steam (160° C., 0.6 MPa) is used, and finally 1 kg / hour of Introduced in fixed quantities. The residence time of the biomass feedstock in the biomass pyrolyzer (20) is about 1 hour. This gives 15 kg/h of gas produced by pyrolysis in the biomass pyrolyzer (20). A total of 6.5 kilograms/hour of char and ash are also discharged from the pyrolysis residue (char) outlet (210).

The pyrolysis gas obtained in the biomass pyrolyzer (20) then passes through the pyrolysis gas introduction pipe (200) from the lower side of the biomass pyrolyzer (20) to the pyrolysis gas reformer ( 40).

At the beginning of the introduction of the pyrolysis gas, the temperature inside the pyrolysis gas reformer (40) becomes unstable. By adjusting the amount of superheated steam supplied and the amount of oxygen introduced from the air or oxygen introduction pipe (261), the pyrolysis gas is partially combusted and the inside of the pyrolysis gas reformer (40) Adjust the temperature to 1,000°C. At this time, the pyrolysis gas reformer (40) is kept at a pressure of 101.3 kPa. Superheated steam from the steam inlet (242) provided at the bottom of the pyrolysis gas reformer (40) is finally introduced at a constant rate of 3.7 kg/hour. Air or oxygen from the oxygen inlet (261) is finally introduced at a constant rate of 2.3 m3-normal/hour. However, this amount of oxygen is appropriately increased or decreased according to the degree of temperature rise inside the pyrolysis gas reformer (40).

By the above operation, the biomass pyrolyzer (20) is maintained at a temperature of 600° C. and a pressure of 101.3 kPa, and the pyrolysis gas reformer (40) is maintained at a temperature of 950° C. and a pressure of 101.3 kPa. This results in a reformed gas outlet (230) at a temperature of 1,000° C. in an amount of 31 kg/hr.

The resulting reformed gas is collected in a rubber bag, and the gas composition is measured by gas chromatography. Table 3 shows the composition of the obtained reformed gas. Also, the operation can be carried out continuously for 3 days. During the operating period, good continuous operation can be maintained without troubles, especially troubles caused by tar. In addition, during operation, the heat carrier medium (30) in the pyrolysis gas introduction pipe (200) is not clogged with tar or the like. Smooth introduction of pyrolysis gases to (40) is maintained. Further, the amount of tar in the reformed gas taken out from the outlet of the pyrolysis gas reformer (40) is approximately 10 mg/m3-normal.

In this way, the reformed gas can be obtained, and by realizing a stable and continuous supply of the heat carrier medium in the gasifier, pressure fluctuations in the pyrolyzer can be suppressed, and the problem of a decrease in separation performance in gas separation. can be solved to provide gas with stable quality.

The biomass gasification apparatus of the present invention comprises a preheater, a biomass pyrolyzer, and a pyrolysis gas reformer. By incorporating a manual valve for supplying oxygen and an on-off valve for supplying oxygen to the pyrolysis gas reformer in an on-off state, the temperature of the reformed gas in the pyrolysis gas reformer approaches a predetermined target temperature, and the reforming reaction is stabilized to stabilize the hydrogen concentration, stable hydrogen can be supplied.

REFERENCE SIGNS LIST 10 preheater 20 biomass pyrolyzer 30 heat carrier medium 40 pyrolysis gas reformer 41 manual valve 42 on/off valve 43 controller 44 detector 45 detector 46 on/off valve adjuster 47 manual valve adjuster 48 controller 49 calculator 50 First valve 60 Hopper 70 Second valve 90 Third valve 200 Pyrolysis gas introduction pipe 201 Pyrolysis gas reformer side gas introduction port (gas outlet) of the pyrolysis gas introduction pipe
202 Biomass pyrolyzer side gas intake (gas inlet) of pyrolysis gas introduction pipe
210 pyrolysis residue (char) outlet 220 biomass supply port 230 reformed gas outlet 240 waste treatment device 241, 242, 243 steam inlet 250 non-oxidizing gas supply 260 upper surface of the heat-bearing medium layer formed in the biomass pyrolyzer 261, 262 air or oxygen inlet tube

Claims (12)

a preheater for preheating the heat carrier,
A pyrolyzer that is supplied with a heat carrier preheated by the preheater and performs pyrolysis of biomass using the heat of the heat carrier, and a pyrolysis gas generated by the pyrolysis is replaced by air or oxygen. In a biogas gasifier comprising a pyrolysis gas reformer that performs steam reforming by partial combustion with
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier. 2. The biomass gasifier according to claim 1, wherein the temperature of the reformed gas is raised to a predetermined temperature range of 900[deg.] C. or less by supplying oxygen gas from the manual valve. The biomass gasifier according to claim 2, wherein the predetermined temperature range is from 800°C to 900°C. The biomass gasifier according to claim 2, wherein the predetermined temperature range is from 850°C to 880°C. 5. The temperature of the reformed gas is raised to the target temperature by supplying oxygen gas from the on-off valve in addition to the temperature rise of the reformed gas by the manual valve. The biomass gasifier according to . The biomass gasifier according to claim 5, wherein the target temperature is 850°C to 1000°C. The biomass gasifier according to claim 5, wherein the target temperature is 880°C to 950°C. The biomass gasifier according to claim 5, wherein the target temperature is 900°C to 930°C. The biomass gasifier according to any one of claims 2 to 8, wherein the predetermined temperature range is adjusted based on the reached temperature of the reformed gas. the biomass pyrolyzer comprises a biomass inlet and a non-oxidizing gas inlet and/or steam inlet;
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas provided between the biomass pyrolyzer and the pyrolysis gas reformer for introducing the pyrolysis gas generated in the biomass pyrolyzer into the pyrolysis gas reformer including an introduction tube;
In addition, the biomass pyrolyzer and the pyrolysis gas reformer each further include an inlet and an outlet for a preheated heat carrier unit, and the heat possessed by the heat carrier unit thermally decomposes biomass and Execute reforming of pyrolysis gas generated by pyrolysis of biomass,
The biomass pyrolyzer and the pyrolysis gas reformer are provided in parallel with respect to the flow of the heat carrier medium, and the pyrolysis gas introduction pipe is connected to the biomass pyrolyzer and the heat said biomass pyrolyzer and said pyrolysis gas below the upper surface of said heat-carrying medium layer respectively formed in said biomass pyrolyzer and said pyrolysis gas reformer on both sides of the cracker gas reformer; A biomass gasification apparatus provided on the side of a reformer and having the pyrolysis gas introduction pipe substantially horizontal with respect to the direction of gravity,
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier. the biomass pyrolyzer comprises a biomass inlet and a non-oxidizing gas inlet and/or steam inlet;
the pyrolysis gas reformer comprises a steam inlet and a reformed gas outlet;
Furthermore, a pyrolysis gas introduction pipe is provided between the biomass pyrolyzer and the pyrolysis gas reformer, and the pyrolysis gas generated in the biomass pyrolyzer is transferred to the pyrolysis gas reformer. introduced into
and the biomass pyrolyzer further comprises an inlet and an outlet for a preheated heat carrier medium, and uses the heat of the heat carrier medium to carry out pyrolysis of biomass,
On the other hand, the pyrolysis gas reformer performs steam reforming of pyrolysis gas generated by pyrolysis of biomass,
The pyrolysis gas reformer further comprises an air or oxygen inlet, and steam reforming is performed by partially burning the pyrolysis gas generated by the pyrolysis of biomass with the air or oxygen,
The biomass gasifier, wherein the pyrolysis gas introduction pipe is provided on the side surface of the biomass pyrolyzer below the upper surface of the heat carrier medium layer formed in the biomass pyrolyzer. There is
Biomass, wherein the pyrolysis gas reformer comprises a manual valve that always supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and an on-off valve that supplies oxygen to the pyrolysis gas reformer by turning on and off gasifier. A biomass pyrolyzer that heats biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of non-oxidizing gas and steam, and reforming the gas generated in the biomass pyrolyzer in the presence of steam. A thermal decomposition gas reformer and a preheated heat support unit are introduced into the biomass pyrolyzer, and the heat of the heat support unit thermally decomposes biomass, and then, introducing the pyrolysis gas generated by pyrolysis of the biomass into the pyrolysis gas reformer to perform steam reforming of the pyrolysis gas;
A pyrolysis gas introduction pipe provided on a side surface of the biomass pyrolyzer below the upper surface of the heat-supporting single layer, in which pyrolysis gas generated by pyrolysis of the biomass is formed in the biomass pyrolyzer. The introduced pyrolysis gas is partially oxidized by air or oxygen separately introduced into the pyrolysis gas reformer through At the same time, in the biomass gasification method, wherein the biomass is reformed by steam introduced at the same time as the air or oxygen,
The temperature of the reformed gas is raised to a predetermined temperature region by oxygen from a manual valve provided in the pyrolysis gas reformer, which constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer, and A biomass gasification method, wherein the temperature of the reformed gas is raised to a predetermined target temperature by oxygen from an on-off valve that supplies oxygen to a pyrolysis gas reformer in an on-off state.

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