JP2003226501A - Hydrogen production system - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a compact and highly efficient hydrogen production system using waste or the like as a raw material. <P>SOLUTION: The hydrogen production system is provided with a gasification chamber 1 in which a gasification fluidized bed is formed of a high temperature fluid medium (c1) and a combustible synthetic gas (b) containing hydrogen is produced by gasifying a material (a) to be treated, a char combustion chamber 2 in which a char combustion chamber fluidized bed is formed of a high temperature fluid medium (c2) and char (h) produced with the gasification in the gasification chamber 1 is burned in the char combustion chamber fluidized bed to heat the fluidized medium (c2) and a hydrogen separation apparatus 120 in which excess components is removed from the synthesis gas to obtain high purity hydrogen (j). The gasification chamber 1 and the char combustion chamber 2 are partitioned from each other to prevent the circulation of the gas in the vertical upper side of the boundary face of the fluidized bed, a communicating port 25 for allowing the gasification chamber 1 and the char combustion chamber 2 to communicate with each other is formed in the lower part of the partition to move the fluid medium (c2) heated in the char combustion chamber 2 to the gasification chamber 1 side from the char combustion chamber 2 side. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrogen production system, and more particularly to a hydrogen production system for obtaining hydrogen gas from a combustible synthesis gas obtained by thermally decomposing solid fuel, biomass, various wastes and the like as a raw material. It is a thing.

[0002]

2. Description of the Related Art In recent years, due to environmental problems, resource depletion, and demands for fossil fuel reduction, practical application of hydrogen production technology using solid fuels such as coal and biomass and organic wastes as raw materials is expected. For the production of hydrogen from solid fuels and wastes, the solid fuels and wastes are pyrolyzed and gasified by partial combustion to obtain synthesis gas (produced gas) mainly composed of hydrogen, carbon monoxide, etc. The general method is to obtain pure hydrogen.

In this case, since the synthesis gas obtained by gasification contains carbon monoxide and carbon dioxide,
A CO conversion device for converting carbon monoxide to hydrogen and a hydrogen separation device for separating surplus components such as carbon dioxide and pure hydrogen are required.

[0004]

However, in the conventional hydrogen gas production system as described above, when the carbon monoxide and carbon dioxide concentrations in the synthesis gas are high, the CO conversion device becomes large and the hydrogen separation device becomes In addition to decreasing efficiency,
There is a problem that equipment cost and operation cost increase due to an increase in the compression power of the syngas.

Therefore, the present invention uses a solid fuel such as coal or biomass, or an object to be treated represented by various wastes as a raw material to obtain a syngas containing a small amount of carbon monoxide or carbon dioxide, and relatively It is an object of the present invention to provide a hydrogen production system which is compact and enables efficient hydrogen production.

[0006]

In order to achieve the above object, the hydrogen production system according to the first aspect of the present invention, as shown in FIG. A gasification chamber 1 that forms a fluidized bed of a gasification chamber having an interface, and gasifies the object a to be treated a in the fluidized bed of the gasification chamber to generate a combustible synthesis gas b containing hydrogen; The medium c2 is fluidized inside to form a char combustion chamber fluidized bed having a second interface, and char h generated by gasification in the gasification chamber 1 is burned in the char combustion chamber fluidized bed to form a fluidized medium. a char combustion chamber 2 for heating c2; and a hydrogen separation device 120 for removing a surplus component k from the synthesis gas to obtain high-purity hydrogen j; the gasification chamber 1 and the char combustion chamber 2 are the same as those described above. Gas flow vertically above the fluidized bed interface It is partitioned by the first partition wall 15 so that it does not exist, and a communication port 25 that connects the gasification chamber 1 and the char combustion chamber 2 is provided below the first partition wall 15, and the height of the upper end of the communication port 25 is higher than that of the communication port 25. Is formed with a communication port 25 which is below the first interface and the second interface, and through the communication port 25,
The fluidized medium c2 heated in the char combustion chamber 2 is moved from the char combustion chamber 2 side to the gasification chamber 1 side.

When the term "hydrogen-containing combustible synthesis gas" is used herein, the synthesis gas typically contains hydrogen gas H ₂ . However, what is contained is not limited to hydrogen gas, but may be flammable gas such as hydrocarbon containing hydrogen as a constituent element, or both.

According to this structure, since the gasification chamber and the char combustion chamber are partitioned by the first partition wall, the gasification chamber and the char combustion chamber are separated from each other in the vertical direction above the interface of the fluidized bed. Since there is no flow, and a communication port that connects the gasification chamber and the char combustion chamber is formed in the lower part of the first partition wall, the flow heated in the char combustion chamber from the char combustion chamber side to the gasification chamber side The medium can be moved.

Further, a high-temperature fluidizing medium is fluidized inside,
Gasification chamber having a first interface Since the gasification chamber forming a fluidized bed is provided, it is possible to gasify an object to be processed and generate a combustible synthesis gas containing hydrogen, and to generate a high temperature fluidized medium inside. Is provided with a char combustion chamber that forms a char combustion chamber fluidized bed having a second interface and burns the char generated by gasification in the gasification chamber in the char combustion chamber fluidized bed. Since the hydrogen separator 120 that can be heated and removes excess components from the synthesis gas is provided, high-purity hydrogen can be obtained.

Further, as described in claim 2, in the hydrogen production system according to claim 1, the synthesis gas b generated in the gasification chamber 1 further contains carbon monoxide CO, and carbon monoxide CO gas the may include a CO conversion unit for converting the hydrogen gas H ₂ is reacted with water vapor H _{2 O.}

According to this structure, since the CO converter is provided, carbon monoxide gas can be converted into hydrogen gas.

Further, as described in claim 3, in the hydrogen production system according to claim 1 or 2, the hydrogen separation device 120 includes the adsorbents 121d, 1d for adsorbing the excess component k.
22d and 123d, and a container 121 that stores the adsorbent
e, 122e, 123e, and the adsorption and desorption of the excess component k by introducing the synthesis gas into the container and changing the pressure in the container between a relatively high pressure and a low pressure. It may be configured to repeat.

Further, as described in claim 4, in the hydrogen production system according to any one of claims 1 to 3, a return path 129 for returning the removed excess component k to the char combustion chamber 2 is provided. It may be provided.

The surplus component is typically surplus gas,
In the char combustion chamber, this is combusted to heat the fluidized medium c2. For example, a burner is installed in the char combustion chamber as a combustion device for the excess component gas. As a result, a part or all of the reaction heat necessary for the pyrolysis gasification of the object to be treated a is covered.

[0015]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings. In each drawing, the same or corresponding members are designated by the same reference numerals or similar reference numerals, and redundant description will be omitted. FIG. 1 is a flowchart of a hydrogen production system according to an embodiment of the present invention. The hydrogen production system in the present embodiment is
Synthetic gas (produced gas) b by subjecting the object a to pyrolysis gasification
It is configured to include an integrated gasification furnace 101 for obtaining the above, and a gas purification device 102 for separating the synthetic gas b into hydrogen and surplus gas.

The gas refining device 102 includes a cleaning device 103 for cleaning the synthesis gas b, a desulfurization device 105 for desulfurizing the synthesis gas b, and a gas compression device 107 for increasing the pressure of the synthesis gas b.
And carbon monoxide gas CO in the synthesis gas b with steam H ₂ O
CO conversion device 10 that reacts with hydrogen gas to convert it to hydrogen gas H ₂
4 and a hydrogen separator 120 for removing the excess component k from the CO-converted synthesis gas i to obtain pure hydrogen.

The hydrogen production system of this embodiment further includes a waste heat boiler 201 for recovering heat from the waste gas discharged from the integrated gasification furnace 101, and a solid content accompanying the exhaust gas from the waste heat boiler 201. Device 202 for removing dust and a chimney 20 for discharging the gas removed by the dust device 202
Equipped with 3.

The gas cleaning device 103 is constructed as a cleaning tower in which a tank-shaped container is erected. The water accumulated at the bottom of the tower is sent by a circulation pump 103a to a spray nozzle arranged at the top of the tower and sprayed into the tower. Integrated gasifier 1
The synthesis gas b supplied from 01 is introduced from the lower part of the washing tower, and is countercurrently contacted with the sprayed water for washing.
In particular, solids such as char and chlorine gas that are entrained in the gas b are removed.

The exhaust port at the top of the tower of the gas scrubber 103 is
It is connected to the desulfurizer 105. The desulfurizer 105 is
This is an apparatus in which a tank-shaped container is filled with a desulfurization catalyst, and particularly for removing H ₂ S gas.

The desulfurized synthesis gas is compressed by a gas compression device 107 installed on the downstream side of the desulfurization device 105. Especially the pressure required for CO converter and hydrogen separator,
It is set to 1.5 MPa or more. More preferably 2.0MP
It is a or more. The compressor 107 is preferably a positive displacement compressor when the handled gas flow rate is large and a positive displacement compressor such as a reciprocating compressor when the treated gas flow rate is small.

A CO conversion device 104 is installed downstream of the gas compression device 107. This is constructed as a tower in which tank-shaped containers are erected. C in the container
It is filled with O conversion catalyst. Also, the CO converter has
A steam supply pipe for supplying steam 1 is connected.

The CO conversion reaction is a reaction for converting CO in the synthesis gas into H2 by the following reaction. The CO conversion reaction is generally classified into a high temperature CO conversion reaction and a low temperature CO conversion reaction depending on the type of catalyst used. CO + H ₂ O → H ₂ + CO _{2 The} high temperature CO conversion reaction uses an iron + chromium-based catalyst and is carried out at a temperature of 350 to 400 ° C. and a pressure of up to about 3 MPa. When the synthesis gas contains 10 to 20% of CO gas, the CO concentration becomes 2 to 3 due to the high temperature CO conversion reaction.
It is reduced to about 5%.

The low temperature CO conversion reaction is carried out at a temperature of 200 to 240 ° C. and a pressure of about 3 MPa using a copper + zinc catalyst. Since a steel + zinc type catalyst is extremely sensitively deteriorated by sulfur, it is usual to install a desulfurization catalyst at the inlet of the catalytic reactor for protection.

For both the high temperature CO conversion reaction and the low temperature CO conversion reaction, a fixed bed type apparatus in which a catalyst is packed in a column is generally used as a reaction apparatus, and the reaction is carried out by passing a synthesis gas to which steam is added. Be seen. Further, since the CO conversion reaction is an exothermic reaction, the post-reaction synthesis gas is heat-exchanged with the pre-reaction synthesis gas by a heat exchanger (not shown), or a boiler (not shown) is installed immediately after the reactor to generate steam. You may devise to improve heat efficiency by performing heat recovery.

Next, the integrated gasification furnace 101 according to the present embodiment will be described with reference to the conceptual sectional view of FIG. The integrated gasification furnace 101 includes a gasification chamber 1, a char combustion chamber 2 and a heat recovery chamber 3 which are respectively in charge of three functions of pyrolysis, that is, gasification, char combustion, and heat recovery, and for example, has an overall cylindrical shape. Alternatively, it is housed in a rectangular furnace body.
Gasification chamber 1, char combustion chamber 2 and heat recovery chamber 3 are partition walls 1
It is divided into 1, 12, 13, 14, and 15, and a fluidized bed, which is a dense layer containing a fluidized medium, is formed at the bottom of each of them. In order to fluidize the fluidized bed of each chamber, that is, the gasification chamber fluidized bed, the char combustion chamber fluidized bed, and the heat recovery chamber fluidized bed, the furnace bottom, which is the bottom of each chamber 1, 2, and 3, is fluidized. An air diffuser for injecting fluidizing gas into the medium is provided. The air diffuser is configured to include, for example, a perforated plate laid on the bottom of the furnace, and the perforated plate is divided into a plurality of chambers in the width direction to change the superficial velocity of each part in each chamber. In addition, the flow velocity of the fluidizing gas blown out from each room of the air diffuser through the perforated plate is changed. Since the superficial velocity is relatively different in each part of the chamber, the fluidized medium in each chamber also has a different flow state in each part of the chamber, so that an internal swirl flow is formed. The internal swirl flow circulates in each chamber in the furnace because the flow state is different in each part of the chamber. In the figure, the size of the hatched arrow shown in the air diffuser indicates the flow velocity of the fluidizing gas blown out. For example, the thick arrow at the location indicated by 2b has a higher flow velocity than the thin arrow at the location indicated by 2a.

The gasification chamber 1 and the char combustion chamber 2 are partitioned by a partition wall 11 and a partition wall 15, and the char combustion chamber 2 and the heat recovery chamber 3 are partitioned by a partition wall 12 to separate the gasification chamber 1 from the gasification chamber 1. The space between the heat recovery chambers 3 is partitioned by a partition wall 13 (this drawing shows the furnace in a plan view, so the partition wall 1
1 is shown as if it is not between the gasification chamber 1 and the char combustion chamber 2 and the partition wall 13 is not as between the gasification chamber 1 and the heat recovery chamber 3). That is, in the integrated gasification furnace 101, each chamber is not configured as a separate furnace but is integrally configured as one furnace. Further, a settling char combustion chamber 4 is provided near the surface of the char combustion chamber 2 in contact with the gasification chamber 1 so that the fluidized medium descends. That is, the char combustion chamber 2 is divided into a settling char combustion chamber 4 and a char combustion chamber main body other than the settling char combustion chamber 4. Therefore, a partition wall 14 is provided for partitioning the settled char combustion chamber 4 from the other part of the char combustion chamber 2 (char combustion chamber main body). The settling char combustion chamber 4 and the gasification chamber 1 are separated by the partition wall 1.
It is divided by 5.

Here, the fluidized bed and the interface will be described.
The fluidized bed consists of a concentrated layer in the vertically lower part, which contains a fluidized medium (for example, silica sand) in a fluidized state by the fluidizing gas, and a fluidized medium in the vertically upper part of the concentrated layer. It consists of a splash zone where a large amount of gas coexists and the fluid medium is vigorously splashing. Above the fluidized bed, that is, above the splash zone, there is a freeboard section containing almost no fluidized medium and mainly gas.
The interface refers to the splash zone having a certain thickness, but may also be regarded as a virtual surface intermediate between the upper surface and the lower surface of the splash zone (the upper surface of the rich layer).

Further, "partitioned by a partition wall so that gas does not flow above the interface of the fluidized bed in the vertical direction."
In that case, it is preferable that the gas does not flow above the upper surface of the dense layer below the interface.

The partition wall 11 between the gasification chamber 1 and the char combustion chamber 2 is almost entirely partitioned from the furnace ceiling 19 to the furnace bottom (perforated plate of the air diffuser), but the lower end is the furnace. There is a second opening 21 near the bottom of the furnace without contacting the bottom.
However, the upper end of the opening 21 does not reach above the interface between the fluidized bed interface of the gasification chamber and the fluidized bed interface of the char combustion chamber. More preferably, the upper end of the opening 21 does not reach above the upper surface of the rich layer of the gasification chamber fluidized bed or the upper surface of the rich layer of the char combustion chamber fluidized bed. In other words, it is preferable that the opening 21 is always formed so as to be submerged in the dense layer. That is, the gasification chamber 1 and the char combustion chamber 2 are separated from each other by a partition wall so that there is no gas flow at least in the freeboard portion, that is, above the interface, and more preferably above the upper surface of the rich layer. It will be partitioned.

The partition wall 12 between the char combustion chamber 2 and the heat recovery chamber 3 has its upper end in the vicinity of the interface, that is, above the upper surface of the rich layer, but below the upper surface of the splash zone. The lower end of the partition wall 12 is up to the vicinity of the furnace bottom, and like the partition wall 11, the lower end does not contact the furnace bottom, and there is an opening 22 near the furnace bottom that does not reach above the upper surface of the rich layer. In other words, only the fluidized bed portion between the char combustion chamber 2 and the heat recovery chamber 3 is partitioned by the partition wall 12, and the partition wall 12 has an opening 22 near the hearth surface. The fluidized medium of No. 2 flows into the heat recovery chamber 2 from the upper portion of the partition wall 12 and is returned to the char combustion chamber 2 again through the opening 22 near the hearth surface of the partition wall 12.

Partition wall 13 between the gasification chamber 1 and the heat recovery chamber 3
Is completely partitioned from the furnace bottom to the furnace ceiling. The partition wall 14 for partitioning the inside of the char combustion chamber 2 to provide the sedimentation char combustion chamber 4 has an upper end near the interface of the fluidized bed and a lower end in contact with the furnace bottom. The relationship between the upper end of the partition wall 14 and the fluidized bed is
This is the same as the relationship between the partition wall 12 and the fluidized bed. The partition wall 15 for partitioning the settling char combustion chamber 4 and the gasification chamber 1 is the partition wall 1
Similar to No. 1, it is partitioned almost entirely from the furnace ceiling to the furnace bottom, the lower end does not contact the furnace bottom, there is a first opening 25 near the furnace bottom, and the upper end of this opening Is below the top surface of the dense layer. That is, the relationship between the first opening 25 and the fluidized bed is the same as the relationship between the opening 21 and the fluidized bed.

The waste or solid fuel a put into the gasification chamber 1 receives heat from the fluidized medium c1 and is thermally decomposed and gasified. Typically, the waste or fuel a does not burn in the gasification chamber 1 and is so-called carbonization. Remaining dry char h
Is the opening 2 at the bottom of the partition wall 11 together with the fluid medium c1.
From 1 to the char combustion chamber 2. In this way, the char h introduced from the gasification chamber 1 burns in the char combustion chamber 2 to heat the fluidized medium c2. The fluidized medium c2 heated by the combustion heat of the char h in the char combustion chamber 2 is the partition wall 1
2 passes over the upper end of 2 and flows into the heat recovery chamber 3, and is arranged in the heat recovery chamber 3 so as to be below the interface in the layer heat transfer tube 41.
After the heat is collected by and is cooled, it again flows into the char combustion chamber 2 through the lower opening 22 of the partition wall 12.

Here, the heat recovery chamber 3 is not essential in the gas supply device according to the embodiment of the present invention. That is, if the amount of char h mainly consisting of carbon remaining after gasification of the volatile components in the gasification chamber 1 and the amount of char required to heat the fluidized medium c2 in the char combustion chamber 2 are substantially equal to each other. The heat recovery chamber 3 that removes heat from the fluid medium is unnecessary. If the difference in the amount of the char is small, for example, the gasification temperature in the gasification chamber 1 becomes high, and the amount of CO gas generated in the gasification chamber 1 increases, so that the balance state is maintained. Be done.

However, as shown in FIG. 2, the heat recovery chamber 3
When equipped with, it is possible to deal with a wide variety of wastes or fuels, from coal that generates a large amount of char to municipal waste that hardly generates char. That is,
Regardless of what kind of waste or fuel, by adjusting the heat recovery amount in the heat recovery chamber 3, the char combustion chamber 2
The temperature of the fluidized medium can be maintained appropriately by appropriately adjusting the combustion temperature of the.

On the other hand, the fluidized medium c2 heated in the char combustion chamber 2 flows into the settling char combustion chamber 4 over the upper end of the partition wall 14 and then into the gasification chamber 1 through the opening 25 at the bottom of the partition wall 15. Inflow.

Here, the flow state and movement of the flowing medium between the chambers will be described. In the vicinity of the surface in contact with the partition wall 15 between the sedimentation char combustion chamber 4 and the inside of the gasification chamber 1, a strong fluidization region 1b in which a stronger fluidization state is maintained as compared with the fluidization of the sedimentation char combustion chamber 4. It has become. As a whole, it is preferable to change the superficial velocity of the fluidizing gas depending on the location so that the mixed diffusion of the injected fuel and the fluidized medium is promoted. As an example, as shown in FIG. In addition to this, a weak fluidization region 1a is provided so that a swirling flow is formed.

The char combustion chamber 2 has a weak fluidization region 2 at the center.
a, it has a strong fluidization region 2b in the peripheral portion, and the fluidizing medium and the char form an internal swirling flow. It is preferable that the fluidization rate in the strong fluidization zone in the gasification chamber 1 and the char combustion chamber 2 is 5 Umf or more and the fluidization rate in the weak fluidization zone is 5 Umf or less, but the weak fluidization zone and the strong fluidization If there is a clear relative difference in the chemical range, there is no problem in exceeding this range. Heat recovery chamber 3 in char combustion chamber 2 and settling char combustion chamber 4
It is preferable to dispose the strong fluidization region 2b in the portion in contact with. If necessary, it is preferable to provide a gradient on the bottom of the furnace so that it goes down from the weak fluidization zone side to the strong fluidization zone side (not shown). Here, Umf is a unit in which the minimum fluidization speed (speed at which fluidization is started) is 1 Umf. That is, 5 Umf is 5 times the minimum fluidization rate.

In this way, the char combustion chamber 2 and the heat recovery chamber 3
By keeping the fluidized state on the side of the char combustion chamber near the partition wall 12 relatively stronger than the fluidized state on the side of the heat recovery chamber 3, the fluidized medium is the interface of the fluidized bed of the partition wall 12. The fluid medium flowing from the side of the char combustion chamber 2 to the side of the heat recovery chamber 3 over the upper end in the vicinity, and the inflowing fluid medium moves downward due to a relatively weak fluidized state in the heat recovery chamber 3, that is, a high-density state. It moves to the char combustion chamber 2 side from the heat recovery chamber 3 side through the lower end (opening 22) of the partition wall 12 near the furnace bottom.

Similarly, the fluidization state on the char combustion chamber body side near the partition wall 14 between the body of the char combustion chamber 2 and the sedimentation char combustion chamber 4 is more relative to that on the side of the sedimentation char combustion chamber 4 side. By maintaining an extremely strong fluidized state, the fluidized medium moves and flows from the side of the main body of the char combustion chamber 2 to the side of the settled char combustion chamber 4 over the upper end near the interface of the fluidized bed of the partition wall 14. The fluidized medium flowing into the settling char combustion chamber 4 moves downward (toward the furnace bottom) due to the relatively weak fluidized state in the settling char combustion chamber 4, that is, the high density state, and the furnace of the partition wall 15 is moved. It moves from the settling char combustion chamber 4 side to the gasification chamber 1 side through the lower end (opening 25) near the bottom. Here, the fluidized state on the gasification chamber 1 side near the partition wall 15 between the gasification chamber 1 and the sedimentation char combustion chamber 4 is relatively stronger than the fluidized state on the sedimentation char combustion chamber 4 side. Is kept at. This assists the movement of the fluidized medium from the settling char combustion chamber 4 to the gasification chamber 1 by an attractive action.

Similarly, the fluidization state on the side of the char combustion chamber 2 near the partition wall 11 between the gasification chamber 1 and the char combustion chamber 2 is relatively stronger than that on the side of the gasification chamber 1. It has been kept in an activated state. Therefore, the fluidized medium is the partition wall 11
Flowing into the char combustion chamber 2 side through an opening 21 (submerged in the rich layer) below the interface of the fluidized bed, preferably below the upper surface of the rich layer.

The entire heat recovery chamber 3 is uniformly fluidized, and is usually maintained so as to be a fluidized state weaker than the fluidized state of the char combustion chamber 2 which is in contact with the heat recovery chamber. Therefore, the superficial velocity of the fluidizing gas in the heat recovery chamber 3 is controlled within the range of 0 to 3 Umf, and the fluidizing medium forms a sedimenting fluidized bed while gently flowing. Here, 0 Umf is a state in which the fluidizing gas is stopped. With such a state, heat recovery in the heat recovery chamber 3 can be minimized. That is,
In the heat recovery chamber 3, the amount of recovered heat can be arbitrarily adjusted within the maximum to minimum range by changing the fluidization state of the fluidized medium. Further, in the heat recovery chamber 3, the fluidization may be uniformly started or stopped or the strength may be adjusted in the entire chamber, but it is also possible to stop the fluidization in a part of the region and place the other in the fluidized state. However, the strength of the fluidized state in a part of the area may be adjusted.

The relatively large incombustibles contained in the waste or fuel are incombustibles discharge port 33 provided at the bottom of the gasification chamber 1.
Discharge from. Also, the furnace bottom of each room may be horizontal,
In order not to make a stagnant part of the flow of the fluid medium,
The furnace bottom may be inclined according to the flow of the fluidized medium near the furnace bottom. The incombustibles outlet 33 may be provided not only on the bottom of the gasification chamber 1 but also on the bottom of the char combustion chamber 2 or the heat recovery chamber 3.

The most preferable fluidized gas in the gasification chamber 1 is to pressurize the produced gas b for recycling. In this way, the gas emitted from the gasification chamber 1 is purely the gas generated from the fuel, and a very high quality gas can be obtained. Water vapor if that is not possible,
It is preferable to use a gas containing as little oxygen as possible (oxygen-free gas) such as carbon dioxide gas (CO ₂ ) or combustion exhaust gas obtained from the char combustion chamber 2. If the bed temperature of the fluidized medium decreases due to the endothermic reaction during gasification, flue gas having a temperature higher than the thermal decomposition temperature is supplied as necessary, or oxygen or oxygen is added to the oxygen-free gas. A gas such as air may be supplied to burn a part of the produced gas. The fluidizing gas supplied to the char combustion chamber 2 supplies a gas containing oxygen necessary for char combustion, for example, air, a mixed gas of oxygen and water vapor. When the calorific value (calorie) of the fuel a is low, it is preferable to increase the oxygen amount, and oxygen is supplied as it is. As the fluidizing gas supplied to the heat recovery chamber 3, air, steam, combustion exhaust gas, or the like is used.

The upper part (upper surface of the splash zone) of the fluidized bed of the gasification chamber 1 and the char combustion chamber 2, that is, the freeboard part is completely partitioned by the partition walls 11 and 15. Furthermore, since the portion above the upper surface of the dense bed of the fluidized bed, that is, the splash zone and the freeboard portion is completely partitioned by the partition wall, the char combustion chamber 2
Even if the balance of the pressures of the freeboard portions of the gasification chamber 1 and
Alternatively, the turbulence can be absorbed only by a slight difference in the position difference of the upper surface of the dense layer, that is, the layer height difference. That is, since the gasification chamber 1 and the char combustion chamber 2 are partitioned by the partition walls 11 and 15, even if the pressure in each chamber fluctuates, this pressure difference can be absorbed by the bed height difference. Layer 2 is opening 2
It can be absorbed until it descends to the upper ends of 1, 25. Therefore, the upper limit of the pressure difference between the freeboards of the char combustion chamber 2 and the gasification chamber 1 that can be absorbed by the bed height difference is the gasification from the upper ends of the openings 21 and 25 in the lower portions of the partition walls 11 and 15 that partition each other. It is almost equal to the head difference between the head of the chamber fluidized bed and the head of the char combustion chamber fluidized bed.

In the integrated gasification furnace 101 described above,
Inside a single fluidized bed furnace, three gasification chambers, a char combustion chamber, and a heat recovery chamber are installed through partition walls, and the char combustion chamber and gasification chamber, and the char combustion chamber and heat recovery chamber are respectively separated. Adjacent to each other. This integrated gasifier 101
Since a large amount of fluidized medium can be circulated between the char combustion chamber and the gasification chamber, a sufficient amount of heat for gasification can be supplied only by the sensible heat of the fluidized medium.

Furthermore, in the above integrated gasification furnace, since the seal between the char combustion gas and the produced gas is perfected,
The pressure balance between the gasification chamber and the char combustion chamber is well controlled, the combustion gas and the produced gas are not mixed, and the property of the produced gas is not deteriorated.

The fluid medium c1 as a heat medium and the char h flow from the gasification chamber 1 side to the char combustion chamber 2 side, and the same amount of the fluid medium c2 is supplied from the char combustion chamber 2 side. Since it is configured to return to the gasification chamber 1 side, it is naturally mass-balanced and mechanically conveyed using a conveyor or the like to return the fluidized medium from the char combustion chamber 2 side to the gasification chamber 1 side. There is also no problem that handling of high-temperature particles is difficult and sensible heat loss is large.

Integrated gasification furnace 101 according to the present embodiment
Is further provided with a surplus gas burner 101d for combusting the surplus gas k separated from hydrogen in the hydrogen separation device 120. Combustion by the surplus gas burner 101d is performed in the char combustion chamber 2 or the heat recovery chamber 3. The surplus gas is mixed with air before the burner 101d and burns in the char combustion chamber 2. The surplus gas k will be described in detail later.

As an example of the hydrogen separator, a pressure swing type hydrogen separator (hydrogen PSA) used in the present embodiment will be described with reference to the flowchart of FIG. The pressure swing type hydrogen separation device 120 includes three adsorption towers 121,
122, 123 and a surplus gas holder 124 are provided.

The adsorption towers 121, 122, 123 are the containers 1
21e, 122e, 123e, and the adsorbents 121d, 122d, 123d filled therein, respectively. In this embodiment, the adsorbent is made of a synthetic zeolite material.

The pipe for introducing the synthesis gas i is branched toward the three adsorption towers, and valves 121a, 122a,
Via 123a, the adsorption tower vessels 121e, 122e,
It is connected to 123e. Valves 121a, 122a, 1
The pipes between 23a and the adsorption towers 121, 122, 123 are branched and valves 121c, 122c,
After joining through 123c, the joined pipes are connected to the surplus gas holder 124.

A pipe 129 for leading out the surplus gas k is connected to the surplus gas holder 124, and a valve 124a is provided in this pipe.

On the other hand, three adsorption tower vessels 121e, 12
2e and 123e are connected to pipes for leading out high-purity hydrogen j, and valves 121b and 1 are connected to the pipes, respectively.
22b and 123b are provided. Each pipe has a valve 12
It merges into one pipe on the downstream side of 1b, 122b, 123b.

Hereinafter, this pressure swing type hydrogen separator 12 will be described.
The action of 0 will be described. The hydrogen separation device 120 is a device that separates gas components contained in the gas i by utilizing the difference in the speed at which each gas component is physically adsorbed by the adsorbent. The raw material synthesis gas (mixed gas) i is introduced into the adsorption tower after being compressed to a pressure necessary for adsorbing the surplus gas component k. The adsorbent filled in the adsorption tower preferentially adsorbs the gas components contained in the mixed gas i having a large molecular weight.

Therefore, the hydrogen gas having the smallest molecular weight has the slowest rate of being adsorbed by the adsorbent, and therefore the residence time of the mixed gas in the adsorption tower, that is, the contact time between the mixed gas and the adsorbent has an appropriate value. By designing in this way, almost all surplus components other than hydrogen contained in the mixed gas are adsorbed by the adsorbent, and the product gas at the outlet of the adsorption tower becomes almost pure hydrogen. In general, since a part of hydrogen gas is also adsorbed by the adsorbent, about 80% of the hydrogen gas in the raw material mixed gas is recovered as product gas (pure hydrogen). A hydrogen purity of 99.99% or more can be easily obtained.

Since the amount of the adsorbent capable of adsorbing the surplus gas component is limited, if the mixed gas i is continuously passed for a certain time, the surplus gas component k is not adsorbed, and the product gas (pure hydrogen) is not adsorbed. The purity of j decreases. Therefore, it is necessary to desorb the excess gas component k adsorbed on the adsorbent after passing the mixed gas for a certain period of time.

The amount of the surplus gas component k adsorbed on the adsorbent largely varies depending on the pressure. The higher the pressure, the more the gas component k is adsorbed. By utilizing this property, the pressure in the adsorption tower is changed between a high pressure and a low pressure (pressure swing), so that adsorption and desorption of the excess gas component k on the adsorbent can be repeated.

The larger the pressure difference at the time of adsorption and the pressure at the time of desorption, the higher the efficiency of gas separation can be made, but the power consumption at the time of performing compression adsorption of the raw material gas i becomes large, and therefore the pressure difference becomes excessive. It is not always appropriate to increase. Generally, the pressure in the adsorption tower is preferably 1.5 MPa or more, more preferably 2.0 MPa.
That is all. Further, the desorption is performed at a pressure around atmospheric pressure, but when considering the use of the surplus gas k as described later, it is desirable to perform the desorption under a slightly increased pressure of about 0.1 to 0.2 MPa.

The temperature for adsorption and desorption is from room temperature to 50.
It is performed at a temperature of about ℃. Since the raw material mixed gas i cannot be processed during the desorption of the surplus gas k, a plurality of adsorption towers 121, 122, 123 are installed as shown in FIG.
It is configured such that the adsorption tower for performing the desorption operation is switched and the adsorption operation is always performed in one of the adsorption towers.

The surplus gas holder 124 is a tank for temporarily storing the surplus gas k after desorption.
Since the desorption process is performed intermittently, excess gas after desorption k
This is because it is preferable to temporarily store the gas k after desorption as described above when using as a fuel gas. By doing so, the gas can be continuously supplied. Depending on the use of the gas k, the surplus gas holder may not be installed.

Further referring to FIG. 3, three adsorption towers 12
A specific operation of the pressure swing type hydrogen separation device 120 including 1, 122 and 123 will be described. Here, in the three adsorption towers 121, 122, 123,
The case where the adsorption, desorption, and pressurization operations are performed will be described.

The raw material mixed gas i is pressurized to a required pressure in the apparatus 120. In addition, the surplus gas holder 1
24 is by adjusting the opening of the valve 124a,
A constant flow rate of the surplus gas k is constantly discharged to the outside, and the inside of the holder 124 is kept at a low pressure of about atmospheric pressure.

First, the adsorption operation is performed in the adsorption tower 121. Valves 121a and 121b open, valve 1
21c is closed, the pressurized raw material mixed gas i passes through the tower 121, and the surplus gas component k in the mixed gas i is adsorbed by the adsorbent 121d. At this time, the hydrogen gas remaining without being adsorbed is discharged to the outside as a product gas (pure hydrogen) j via the valve 121b.

At this time, a desorption operation is performed in the adsorption tower 122. Valves 122a and 122b closed, valve 122
c is open, and the pressure in the column 122 is reduced until the pressure in the surplus gas holder 124 becomes almost equal to the pressure in the surplus gas holder 124. In this way, the surplus gas component k adsorbed by the adsorbent 122d in the previous adsorption operation is released to the surplus gas holder 124 via the valve 122c.

At this time, in the adsorption tower 123, the valve 123
Since a is opened, valve 123b is closed, and valve 123c is closed, the pressurized raw material mixed gas i is introduced into the column 123, and the inside of the column is pressurized. Until the inside of the tower 123 is sufficiently pressurized, the adsorption of the excess gas component k by the adsorbent 123d is not sufficient. Therefore, by closing the valve 123b, the excess gas component k becomes the product gas (pure hydrogen).
It is prevented from being mixed in j.

By repeating the above three operations in the three adsorption towers 121, 122, 123 in sequence, hydrogen can be continuously separated from the raw material mixed gas i.

As the number of towers is increased, the interval for desorption operation in one adsorption tower can be extended, so that a sufficient adsorption time can be secured and the product hydrogen recovery efficiency can be increased. . Generally, as shown in the figure, the number of towers may be 3 or more, but it is preferably 4 to 10.

In the above embodiments, the case where a zeolite-based material that adsorbs an excess gas component is used as an adsorbent has been described, but conversely, it is also possible to use a hydrogen storage alloy that adsorbs hydrogen. Swinging pressure causes adsorption and desorption of hydrogen. In this case holder 1
Hydrogen flows to the 24 side, and valves 121b, 122b, 123b
Excess gas flows to the side. Therefore, the valves 121b, 12
It is preferable to provide a holder similar to the holder 124 on the downstream side of 2b and 123b.

Returning to FIG. 1, the operation of the hydrogen production system according to the present invention will be described. The waste or fuel a supplied to the gasification chamber 1 of the integrated gasification furnace 101 is decomposed into combustible gas b, char h, and ash by thermal decomposition. here,
As the waste or fuel a, waste plastic,
It is desirable to use organic wastes or fuels having a high calorific value to some extent, such as waste tires, car shredder dust, wood waste, general waste RDF, coal, heavy oil, tar, and the like.

Among the chars h produced by thermal decomposition in the gasification chamber 1, those having a large particle size and not entrained in the combustible gas are transferred to the char combustion chamber 2 together with the fluidized medium. In the char combustion chamber 2, air, oxygen-enriched air, or an aerobic gas such as oxygen is used as the fluidizing gas g2,
Completely burn char h. Part of the amount of heat generated by the combustion of the char h is supplied to the gasification chamber 1 as sensible heat of the fluidized medium c2 that is circulated back to the gasification chamber 1 and is used as the amount of heat required for thermal decomposition in the gasification chamber 1. Used.

According to this method, the combustible gas generated by the thermal decomposition of the waste or solid fuel a in the gasification chamber 1, that is, the synthesis gas b, and the combustion gas e generated by the combustion of the char h in the char combustion chamber 2 Is not mixed, high-calorie synthesis gas b can be obtained. In particular, the fluidized gas g1 in the gasification chamber 1 contains no air or oxygen gas,
For example, steam or the like is used. In this way, by supplying the total amount of heat required for thermal decomposition by supplying the amount of heat generated by the combustion of the char h in the char combustion chamber 2 through the sensible heat of the fluidized medium, in the gasification chamber 1. It is possible to obtain a high-calorie synthesis gas b having a low combustion gas concentration such as CO ₂ and H ₂ O without performing partial combustion at all.

When steam is used as the fluidizing gas g1 in the gasification chamber 1, it is possible to completely exclude an inert gas such as nitrogen gas or argon gas. The inert gas concentration can be kept low. As a result, the flow rate of the synthesis gas b can be reduced, so that the devices such as the gas compression device 107, the CO conversion device 104, and the hydrogen separation device 120 in the subsequent stage can be downsized, and the gas compression power can be reduced. .

In the case of a general partial combustion gasification furnace, it was necessary to supply pure oxygen as an oxidant in order to prevent nitrogen from being mixed into the synthesis gas. When used, even if air is used as the oxidant in the char combustion chamber 2, nitrogen in the air is not mixed with the synthesis gas b side. Therefore, reduction of oxygen production power and reduction of nitrogen gas concentration in synthesis gas can both be achieved,
Especially effective.

Integrated gasification furnace 10 in the present embodiment
In No. 1, the amount of heat obtained by burning heavy components such as char h generated when the object to be treated a is pyrolyzed and gasified is
It is characterized in that it is used as the amount of heat necessary for the pyrolysis gasification of the object a.

Here, since the heavy components such as char h contain a large amount of carbon and they completely burn in the char combustion chamber 2, carbon dioxide generated by the combustion of carbon contained in the heavy components such as char h. Does not mix with the synthesis gas b generated in the gasification chamber 1. This corresponds to the fact that the hydrogen content and the carbon content in the material to be treated a selectively change the ratio of separation and recovery into the synthesis gas b and the combustion gas e. That is,
A relatively large amount of hydrogen content in the object a to be processed is recovered on the side of the synthesis gas b, and a large amount of carbon content in the object a to be processed is recovered on the side of the combustion gas e.

As a result, as compared with the case where the conventional general partial combustion type gasifier is used, the synthesis gas b
The hydrogen content in the inside increases. Typically, a hydrogen-rich syngas with a molar ratio of hydrogen to carbon monoxide of 2 or more is easily obtained.

This means that the amount of gas components other than hydrogen in the synthesis gas b is small, and compared with the case where a conventional general partial combustion system gasifier is used, the size of the latter stage equipment is smaller. And the power required for gas compression can be reduced. In other words, reduction of plant construction cost,
The operating cost can be reduced.

The synthesis gas b obtained as described above is guided to the gas purification device 102. Note that, depending on the temperature of the synthesis gas b, heat may be recovered by a waste heat boiler (not shown) to reduce the temperature of the synthesis gas b, and then the synthesis gas b may be introduced to the gas purification device 102.

The gas purification apparatus 102 according to the present embodiment
As described above, the gas cleaning device 103 that removes the chlorine content and the dust content in the synthesis gas b, the desulfurization device 105 that removes the sulfur content in the synthesis gas b, and the pressure of the synthesis gas b are increased. Synthetic gas compression device 107, CO conversion device 104 for converting carbon monoxide in the synthetic gas b into hydrogen, hydrogen for obtaining pure hydrogen by separating the hydrogen content and other components (excess components) in the synthetic gas b The separating device 120 is included.

The synthesis gas b is first subjected to removal of chlorine-containing gas components such as hydrogen chloride, dust, carbon particles and the like in the gas cleaning device 102. A scrubber is typically used as the gas cleaning device 102, and gas cleaning is performed by absorbing chlorine, dust and carbon particles in the cleaning water.

Next, hydrogen sulfide,
Sulfur-containing gas components such as carbonyl sulfide are removed. The sulfur-containing gas component and the chlorine-containing gas component not only have the effect of deteriorating the catalyst and adsorbent in the subsequent apparatus, but also cause corrosion of the plant equipment, and therefore, they are typically 10 ppm or less, preferably 1 ppm or less, It is preferably removed to 0.1 ppm or less. In addition, dust and solids such as carbon particles are not included in the hydrogen separator 1 in the subsequent stage.
It adheres to the adsorbent at 20 and deteriorates the performance of the adsorbent, so that it is removed to a sufficiently low concentration.

The synthesis gas from which impurities have been removed as described above is boosted in the synthesis gas compression apparatus to a pressure necessary for the operation of the hydrogen separation apparatus. Here, the compression of the synthesis gas may be performed immediately before the hydrogen separation device 120, that is, after the CO conversion device 104, but the CO conversion device reduces the volume of the reactor and the reaction by increasing the operating pressure. Since the efficiency can be increased, as shown in the figure, it is preferable to perform the compression of the synthesis gas before the CO conversion device 104, that is, after removing the impurities.

Similarly, the compression of the syngas is performed by the desulfurization unit 105.
It is possible to reduce the volume of the desulfurization device 105 by configuring the gas compression device 107 based on the sulfur content because the gas containing the sulfur content is passed through the compressor 107. It is necessary to take measures against corrosion.
Therefore, when the sulfur content in the synthesis gas is very high and there is a risk of corrosion when it is passed through the synthesis gas compression device 107 as it is, the desulfurization device 105 is placed in front of the synthesis gas compression device 107 as shown in the figure. If the sulfur content in the synthesis gas is not so high that there is no risk of corrosion even if it is passed through the synthesis gas compression device 107 as it is, the desulfurization device 105 is placed after the synthesis gas compression device 107. Preferably.

Further, the first desulfurization device for desulfurizing the synthesis gas compression device 107 to the extent that there is no risk of corrosion is provided in front of the synthesis gas compression device 107, and affects the CO conversion device 104 and the hydrogen separation device 120. The second desulfurization device (not shown) that performs desulfurization to the extent that there is no
You may comprise so that it may be installed in the latter stage.

The pressure of the syngas after exiting the syngas compressor 107 is such that the operating pressure of the hydrogen separator 120 plus the pressure loss of each pipe and the pressure loss of the CO converter. Necessary, generally 1 MPa or more,
Preferably 1.5 MPa or more, more preferably 2 MP
It is better to be a or more.

When the operating pressure of the integrated gasification furnace 101 is a negative pressure or a positive pressure of less than about 1 MPa, it is necessary to compress the synthetic gas as described above. If the operating pressure is about 1 MPa or more, the syngas compression device 107 is not always necessary.

The synthesis gas compressed in the synthesis gas compression device 107 advances a CO shift reaction represented by the following in the presence of a catalyst in the CO conversion device to convert a part of carbon monoxide in the synthesis gas into hydrogen. Convert. CO + H ₂ O ← → H ₂ + CO ₂

If the steam required for the reaction is not sufficiently contained in the synthesis gas, it is necessary to separately mix the steam 1 with the synthesis gas as shown in the figure. The steam to be mixed may be steam generated in other boilers,
Preferably, steam generated by waste heat recovery in this system is used, such as steam obtained by heat recovery from combustion gas generated in the char combustion chamber 2 of the integrated gasification furnace 101 and steam obtained in the heat recovery chamber 3. As a result, the energy efficiency of the entire system can be improved and the fuel cost can be reduced.

Integrated gasification furnace 10 in the present embodiment
From the gasification chamber 1 of No. 1, as described above, the synthesis gas b containing a large amount of hydrogen, in which the molar ratio of hydrogen to carbon monoxide is typically 2 or more, is obtained. The amount of carbon monoxide required to be converted into hydrogen by the CO shift reaction is smaller than that in the case where hydrogen is produced using a synthesis gas obtained from a combustion type gasifier. Therefore, the CO converter can be downsized and the amount of steam to be mixed can be reduced, which is effective in reducing the construction cost of the plant and the operating cost.

The synthesis gas i after the CO shift reaction is guided to the hydrogen separation device 120 and separated into pure hydrogen and other gases. It is preferable to use a pressure swing adsorption type hydrogen separator as the hydrogen separator 120 (FIG. 3). In this method, pure hydrogen is obtained by selectively adsorbing components other than hydrogen by passing pressurized synthetic gas through a column filled with an adsorbent such as synthetic zeolite. The adsorbent repeats adsorption and desorption by changing the pressure of the tower,
Can be recycled.

Since the pressure swing adsorption type hydrogen separation device has a simple structure, the efficiency is hardly reduced even if the equipment scale is small, and the equipment cost is not expensive. Furthermore, the adsorbent can be used without replacement for a long time, and the operating cost is low. From this, compared to the conventional method using a carbon dioxide removal device for physical absorption, chemical absorption, etc., the equipment cost especially for small-scale equipment
This has the effect of reducing operating costs.

Since the obtained hydrogen has a positive pressure of about the operating pressure of the hydrogen separation device 120, when it is used at a nearby plant or the like, it can be delivered as it is through a pipe. Further, when the obtained hydrogen is transported and used in other places of use, it may be compressed by a hydrogen compression device (not shown) and shipped as compressed hydrogen, or it may be cooled in a hydrogen liquefaction device (not shown). It may be shipped as liquefied hydrogen.

On the other hand, from the hydrogen separation device 120, a surplus gas k containing carbon monoxide, carbon dioxide, and some hydrogen not recovered as pure hydrogen is obtained. The surplus gas k is combustible and has a calorific value, and thus can be used as a heat source in the system. In particular, in the case of the present embodiment, the surplus gas k
Is preferably combusted in the char combustion chamber 2 of the integrated gasification furnace 101, and the fluidized medium c2 is heated by the combustion heat. In this case, the integrated gasification furnace 10
1 is particularly effective because the rate of partial combustion of the object a to be processed can be reduced and high gasification efficiency can be obtained.

In utilizing the heat quantity of the surplus gas k, for example, the surplus gas k is not burned in the char combustion chamber 2 of the integrated gasification furnace 101, but the surplus gas k is separately burned by a combustion device (not shown). The high temperature combustion gas obtained by the above may be used as the fluidizing gas g2 of the char combustion chamber 2. However, in that case, the oxygen concentration in the fluidized gas g2 may be reduced, and the combustion efficiency of the char h in the fluidized bed portion of the char combustion chamber 2 may be reduced. It is preferably burnt.

That is, as shown in FIG. 1 or 2, when the surplus gas k is burned in the char combustion chamber 2, there is no fear of reducing the oxygen concentration in the fluidized bed portion of the char combustion chamber 2, and the surplus gas k The fluidized medium c2 can be effectively heated by the radiant heat of the flame generated by burning k.

The surplus gas k may be directly reused as the fluidizing gas in the gasification chamber 1 or may be burned in the gasification chamber 1. However, the surplus gas k contains almost no hydrogen, but contains a large amount of carbon such as carbon monoxide, carbon dioxide, hydrocarbon gas, etc. Therefore, when this is returned to the gasification chamber 1, it is generated. The hydrogen concentration in the gas b is reduced. That is, since the excess gas k contains a large amount of unnecessary components in the product pure hydrogen, it is desirable to burn the char gas in the char combustion chamber 2 so as not to mix with the generated gas b.

In the case of such a configuration, when viewed as the whole system, the carbon content in the raw material is selectively combusted in the char combustion chamber 2 as the pyrolysis residue h or the surplus gas k. The amount of heat obtained at this time is used to perform the thermal decomposition reaction of the raw material to extract the hydrogen content. That is, it can be said that this is a particularly preferable form when considering the purpose of the present system of efficient hydrogen production.

From the high temperature exhaust gas e from the char combustion chamber 2, heat can be recovered as steam by the waste heat boiler 201. In addition to this, by installing a waste heat boiler (not shown) in the preceding stage of the gas cleaning device 103, heat can be recovered from the synthesis gas b, and the CO conversion reaction is an exothermic reaction. The heat can be recovered from the device or the gas after CO conversion. The steam obtained by recovering these heats is fluidized gas g in the gasification chamber 1.
Electric power required by the system can be generated by using steam supplied as No. 1, steam for CO conversion reaction, or the like as steam required by the system, or by generating power by a steam turbine (not shown).

In this system, the compression power of the gas in the synthesis gas compression device 107 occupies most of the required power. Therefore, the electric power generated by the steam turbine is preferably used as the required electric power for the gas compression device 107. More preferably, the gas compressor 107 can be directly driven by using the steam obtained by the heat recovery by using a steam turbine instead of an electric motor as a driving machine of the gas compressor 107.

When the product pure hydrogen j is shipped as compressed hydrogen or liquefied hydrogen, it is preferable to use the above-mentioned electric power as a power source of a compression device or a refrigeration device (not shown) necessary for compression or cooling. . More preferably, by using a steam turbine instead of an electric motor as the driving device of these compression device and refrigeration device, it is possible to directly drive the gas compression device using the steam obtained by the heat recovery.

The surplus gas k from the hydrogen separation device 120 may be burned in a heat recovery boiler (not shown) separately without burning in the char combustion chamber 2 to recover heat as steam. A part of the gas k may be burned in the char combustion chamber 2 and the rest may be burned in the heat recovery boiler. In this case, the ratio of burning the surplus gas k in the heat recovery boiler is such that the required power of the system including the compression power of the obtained synthesis gas b becomes equal to the generated power obtained from the heat recovered steam. It is desirable to adjust to.

That is, when the required power of the system is larger than the generated power, the ratio of burning the surplus gas k in the char combustion chamber 2 is reduced, and the ratio of burning it in the heat recovery boiler is increased to increase the gasification efficiency. By lowering the generation amount of the synthesis gas b to reduce the compression power of the synthesis gas b, that is, the power required for the system, and increasing the power generated by heat recovery to balance the power required and the power generated. Can be taken.

When the required power of the system is smaller than the generated power, the ratio of burning the surplus gas k in the char combustion chamber 2 is increased, and the ratio of burning the excess gas k in the heat recovery boiler is decreased to reduce the gasification efficiency. To increase the amount of syngas generated. By doing so, the compression power of the syngas b, that is, the power required for the system is increased, and the power generated by heat recovery is reduced, so that the power required and the power generated can be balanced.

With such a configuration, even if the heat generation amount of the object to be processed fluctuates, it becomes possible to carry out the operation while balancing the required power and the generated power in the system, and Since the amount of electric power and heat supplied can be minimized, the operating cost of the system can be reduced.

When the hydrocarbon gas concentration in the synthesis gas b is high, the gas purification device 102 may include a reforming device (not shown). The reforming device is a device in which a reforming catalyst is housed in a container, and decomposes and reforms hydrocarbons in the synthesis gas to reform to a gas rich in hydrogen gas. The reformer has a cylindrical appearance, for example. A burner is installed at the center of the cylindrical structure. The outer side of the cylindrical combustion chamber is formed into an annular space, and the reforming catalyst is filled therein. The reforming catalyst is heated by the burner. Water is supplied to the reforming catalyst portion from the outside.
In this way, the hydrocarbon is reformed into a gas containing hydrogen gas as a main component and CO gas by the action of the reforming catalyst.

The reformer is preferably installed upstream of the CO converter 104. This is because the CO gas generated in the reformer can be converted into hydrogen gas by the CO converter 104. Further, the reformer may be integrated with the CO converter 104.

On the downstream side of the CO conversion device 104,
A CO selective oxidation device (not shown) may be provided. The apparatus is filled with a CO selective oxidation catalyst, and the CO conversion apparatus 10
The CO gas remaining without becoming CO ₂ in 4 is selectively oxidized by oxygen in the air for CO selective oxidation (2CO + O ₂ → 2
CO ₂ ). Therefore, the gas leaving the CO selective oxidation catalyst contains almost no CO gas, becomes a gas containing hydrogen gas and carbon dioxide gas as main components, and is supplied to the hydrogen separation device 120.

The integrated gasification furnace 101 is provided with a classifying device 108 for classifying the fluidized medium c3 and the incombustible substance d extracted from the gasification chamber 1. After the classification, the fluidized medium c3 is returned to the gasification chamber 1, and the incombustible material d is taken out to the outside.

[0109]

As described above, according to the present invention, since the gasification chamber and the char combustion chamber are partitioned by the first partition wall, the gasification chamber and the char combustion chamber are separated from the interface of the fluidized bed. Since there is no gas flow in the vertically upper part and a communication port that connects the gasification chamber and the char combustion chamber is formed in the lower part of the first partition wall, char combustion is performed from the char combustion chamber side to the gasification chamber side. The fluidized medium heated in the chamber can be moved. In addition, since a gasification chamber that forms a fluidized bed of a gasification chamber having a first interface is provided by internally flowing a high-temperature fluidized medium, the object to be treated is gasified to generate a combustible synthesis gas containing hydrogen. In the char combustion chamber fluidized bed, the char generated in the char combustion chamber fluidized bed can be generated by causing a high temperature fluid medium to flow inside to form a char combustion chamber fluidized bed having a second interface and being generated by gasification in the gasification chamber. To provide a hydrogen production system capable of heating a fluidized medium because it has a char combustion chamber for combustion, and having a hydrogen separation device 120 that removes an excess component from synthesis gas, so that highly pure hydrogen can be obtained. Is possible.

[Brief description of drawings]

FIG. 1 is a flowchart illustrating a hydrogen production system that is an embodiment of the present invention.

FIG. 2 is a conceptual front sectional view showing an example of an integrated gasification furnace that constitutes the hydrogen production system according to the embodiment of the present invention.

FIG. 3 is a flowchart showing an example of a hydrogen separation device that constitutes the hydrogen production system according to the embodiment of the present invention.

[Explanation of symbols]

1 gasification chamber 2 Char combustion chamber 3 heat recovery room 101 Integrated gasifier 102 gas purification equipment 103 gas cleaning device 104 CO converter 105 Desulfurization equipment 120 hydrogen separator 121, 122, 123 adsorption tower 124 Excess gas holder 129 Gas return piping 201 Waste heat boiler 202 dust remover 203 Chimney a Processing object b Syngas c1, c2 fluid medium d Incombustible e Combustion gas g1, g2 fluidized gas h char i Syngas (in front of hydrogen separator) j High-purity hydrogen k Surplus gas component l water vapor m air

─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. ⁷ Identification code FI theme code (reference) C10J 3/46 C10J 3/46 LM C10K 1/32 C10K 1/32 3/04 3/04 F term ( Reference) 4D012 CA20 CB16 CD07 CG01 CH01 CH04 CH05 CH10 CK01 CK03 CK10 4G040 BA02 BB03 4H060 AA01 AA02 BB02 BB12 BB22 BB33 CC15 DD01 EE03 FF03 GG02

Claims (4)

[Claims] 1. A high-temperature fluidizing medium is fluidized internally to
And a gasification chamber for forming a combustible synthesis gas containing a hydrogen content by gasifying the object to be treated in the gasification chamber fluidized bed; It is fluidized inside to form a char combustion chamber fluidized bed having a second interface, and char generated by gasification in the gasification chamber is combusted in the char combustion chamber fluidized bed to heat the fluidized medium. A char combustion chamber; and a hydrogen separator for removing excess components from the synthesis gas to obtain high-purity hydrogen; the gasification chamber and the char combustion chamber are vertically above the interface of the respective fluidized beds. Is partitioned by a first partition wall so that there is no gas flow, and a communication port that connects the gasification chamber and the char combustion chamber is formed in the lower part of the first partition wall. The height of the upper end is the first
And a communication port that is less than or equal to the interface of
A hydrogen production system configured to move the fluidized medium heated in the char combustion chamber from the char combustion chamber side to the gasification chamber side through the communication port. 2. The CO conversion device according to claim 1, wherein the synthesis gas generated in the gasification chamber further contains carbon monoxide, and the CO conversion device reacts the carbon monoxide with steam to convert the carbon monoxide into hydrogen gas. Hydrogen production system. 3. The hydrogen separation device has an adsorbent for adsorbing the surplus component, and a container for accommodating the adsorbent,
The synthesis gas is introduced into the container, and the pressure in the container is changed between a relatively high pressure and a low pressure so that adsorption and desorption of the excess component are repeated.
The hydrogen production system according to claim 1 or 2. 4. The hydrogen production system according to claim 1, further comprising a return path that returns the removed excess component to the char combustion chamber.