JP2003322309A - Fluidized-bed furnace - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a fluidized-bed furnace as a combined furnace consisting of a gasifying furnace and an oxidizing furnace formed in one unit. <P>SOLUTION: The fluidized-bed furnace is partitioned into the gasifying furnace and the oxidizing furnace with a partition wall 8. The circulation flow of a fluid medium is formed in at least one of the gasifying furnace and the oxidizing furnace. The partition wall 8 has a communication port via which the fluid medium is distributed from the gasifying furnace to the oxidizing furnace or from the oxidizing furnace to the gasifying furnace. <P>COPYRIGHT: (C)2004,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a compound furnace having two functions of a gasification furnace and an oxidation furnace even though it is a single furnace, and more particularly to a compound furnace in which the gasification furnace and the oxidation furnace are integrated. Fluidized bed furnace.

[0002]

2. Description of the Related Art At present, from the standpoint of global environmental protection, CO ₂
Reduction measures are important. Also, given the current situation where nuclear power and oil are largely unreliable for energy issues, it is presumed that the time will come when we will have to rely on coal. From such a viewpoint, a highly efficient, compact, and clean coal-fired power generation system is expected as a CO ₂ reduction measure and an alternative energy for the time being. on the other hand,
Since conventional pulverized coal boilers have problems such as limited coal types and limited efficiency, atmospheric pressure type fluidized bed boilers have been developed for multi-kind coal. However, the atmospheric pressure fluidized bed boiler (AFBC) itself does not perform as expected, and since only the steam turbine can be installed in the atmospheric pressure type fluidized bed boiler, there is a limit to high efficiency and large output. For this reason, it is moving to a pressurized fluidized bed boiler (PFBC) capable of a combined power generation system using a gas turbine.

Among the conventional pressurized type fluidized bed boilers, the bubbling type pressurized fluidized bed boiler has the most advanced development and the 80 MWe class demonstrator is operated, but it has the following problems. (A) Issues in load control method At present, a method of controlling the load by changing the fluidized bed height is adopted. That is, the fluid medium is extracted from the inside of the combustor and sent to another storage container, and the heat transfer coefficient is reduced by exposing the heat transfer surface in the fluidized bed to reduce the amount of heat recovery and the steam turbine output. Lower. In addition, the combustion gas discharged from the fluidized bed with reduced fuel supply is cooled by the exposed heat transfer surface, so the combustor outlet temperature, that is, the gas turbine inlet temperature, decreases, and as a result, the gas turbine output decreases. Is. On the other hand, when increasing the load, the reverse method is used.

However, the layer height changing method has the following problems. A storage container for putting the hot fluid medium into and out of the combustor is required, and operation under high temperature and high pressure is not easy, and when a fluid medium with a high heat generation density is taken in and out of the storage container, agglomeration ( Cohesive ash) is generated. Since the boiler is under pressure, the problem of wear in the splash zone when the heat transfer surface in the fluidized bed is exposed is a greater problem than in the atmospheric bubbling fluidized bed boiler (AFBC). The amount of carbon monoxide (CO) generated is reduced by cooling the combustion exhaust gas that has exited the fluidized bed at low load into the inner layer pipe and by reducing the bed height and decreasing the residence time of the combustion gas in the layer. It also increases NOx (nitrogen oxide) emissions.

(B) Increasing the size of the pressure vessel Since the bubbling type pressurized fluidized bed boilers up to the present time are designed to accommodate a square combustor in a cylindrical pressure vessel in plan view, it is inevitable. There is wasted space,
Inevitably, the pressure vessel becomes larger and the cost increases.
In response to this, at the 12th ASME Fluidized Bed International Conference in San Diego in May 1993, "PRINCIPLES
AND DESIGN PHILOSOPHY FOR A 350 MWe PFBC MODULE ''
According to Jim Anderson et al. Of ABB Carbon, AB, a conventional circular pressure vessel 145 as shown in FIG.
A bubbling type pressurized fluidized bed boiler having a planar configuration in which two rectangular combustors 146 are housed in one is deformed into one rhombus as shown in FIG.
It is said that by combining the bases into one furnace, the overall planar shape is made into a hexagonal shape and placed as close to a circular shape as possible to be housed in a circular pressure vessel 145 to reduce the size of the pressure vessel. This is because, in the case of a layer, the cylindrical configuration makes it extremely difficult to arrange the heat transfer tubes in the layer. A storage container and pipes for taking in and out the fluidized medium are required for load control, and if these storage containers and the like are housed inside the pressure container, the pressure container becomes large.

(C) Abrasion of heat transfer tube in the bed In the conventional bubbling type pressurized fluidized bed boiler, the heat transfer tube is disposed in the bed having a high fluidization speed, so that the heat transfer tube is abraded and the surface is hardened by thermal spraying. Measures such as treatment are necessary.

(D) Complicated coal feeding mechanism In the conventional bubbling type pressurized fluidized bed boiler, since fuel such as coal is not sufficiently diffused horizontally in the bed, many bubbling type pressurized fluidized bed boilers are used to avoid uneven combustion. In addition to complicating the coal feeding mechanism, it is difficult to evenly distribute coal to each coal feeding pipe, and in the event of unevenness, in-layer combustion The non-uniformity causes agglomeration, resulting in operation failure.

(E) Consumption of limestone In a conventional pressurized fluidized bed power generation system, limestone was mixed with a fluid medium for desulfurization. However, this limestone is highly worn and contributes sufficiently to the desulfurization reaction. Without it, it was scattered as fly ash from the dust collector. Therefore, the high desulfurization rate required by thermal power plants cannot be expected, and if the desulfurization rate is increased, a huge amount of waste (fly ash) will be produced.

Further, coal gasification combined cycle power generation has also been studied, and the system is a combined power generation system in which the entire amount of coal is gasified, gas is purified, and then supplied to a gas turbine.
The target efficiency when using a 1300 ° C class air-cooled gas turbine is 47.1% at the power generation end. On the other hand, with regard to the pressurized fluidized bed boiler, although an 80MWe class power plant is already operating overseas and there are advantages such as the need for desulfurization equipment, the integrated coal gasification combined cycle system is superior in terms of efficiency. , A topping cycle combined cycle power generation system that has both characteristics and is superior in performance is being studied. This topping cycle combined cycle power generation system basically decomposes coal into coal gas and char in a gasification furnace, combusts the char in a fluidized bed boiler (oxidizing furnace), and discharges the combustion exhaust gas and coal gas at the gas turbine inlet. The mixed combustion is performed to generate a high temperature gas, thereby operating the gas turbine with high efficiency.

Further, regarding the fluidized bed boiler used in the oxidation furnace also in the topping cycle combined cycle power generation system,
There are the same problems as described above, the fixed bed gasifier also has a tar remaining problem, and the spouted bed gasifier also has an ash stick problem. On the other hand, since the fluidized bed gasification furnace operates at an intermediate temperature, it has various advantages such as tar problems, ash sticks can be avoided, and desulfurization in the furnace is possible. When a fluidized bed boiler is adopted, the above (A)-
The problems listed in (D) remain.

Focusing on the gasification furnace and the oxidation furnace used in the above-described topping cycle combined cycle power generation system, the gasification furnace and the oxidation furnace are configured as separate furnaces and are generated in the gasification furnace. The char is sent to the oxidation furnace for combustion in the oxidation furnace.

[0012]

SUMMARY OF THE INVENTION An object of the present invention is to provide a fluidized bed furnace as a compound furnace in which a gasification furnace and an oxidation furnace are integrated.

[0013]

In order to solve the above-mentioned problems, a first aspect of the present invention is a fluidized bed furnace partitioned by a partition wall into a gasification furnace and an oxidation furnace. A circulating flow of a fluidized medium is formed inside at least one of the oxidation furnaces, and the partition wall communicates the fluidized medium from the gasification furnace to the oxidation furnace or from the oxidation furnace to the gasification furnace. It is characterized by having a mouth.

A second aspect of the present invention is a fluidized bed furnace partitioned by a partition wall into a gasification furnace and an oxidation furnace, and a fluidized medium is provided inside each of the gasification furnace and the oxidation furnace. Of the fluidization medium and a portion of the fluidization medium of strong fluidization state are formed, and the portion of the gasification furnace of gentle fluidization state is a strong fluidization state of the oxidation furnace through the partition wall. And the partition wall has a communication port for flowing a fluidized medium from the gasification furnace to the oxidation furnace or from the oxidation furnace to the gasification furnace. Is.

According to a preferred aspect of the present invention, the hearth of the gasification furnace or the oxidation furnace is inclined toward the partition wall. According to a preferred aspect of the present invention, the gasification furnace has a gas outlet for taking out the produced gas to the outside, and the oxidation furnace has a combustion gas outlet for taking out the combustion gas by complete combustion of char to the outside. To do. According to a preferred aspect of the present invention, an in-layer heat transfer tube is arranged in the fluidized bed of the oxidation furnace.

[0016]

According to the present invention, coal is partially gasified while the coal and the desulfurizing agent are supplied to the gasification furnace and circulated in the fluidized bed, and the produced gas is discharged from the gas outlet at the upper part of the gasification furnace to the outside. Derived. Due to the effect of the circulating flow of the fluidized medium, the input coal, desulfurizing agent, etc. are uniformly dispersed in all directions in the fluidized bed of the gasifier, and even with a simple coal feeding facility, uneven distribution of fuel can be avoided and clinker may occur. There is no. On the other hand, the char that has not been gasified enters the oxidation furnace and is completely burned while circulating in the fluidized bed. Then, the combustion gas is taken out from the combustion gas outlet at the upper part of the oxidation furnace. The unburned char and the like entering the oxidation furnace are gently settled while burning in the fluidized bed of the oxidation furnace, and then pass through the connecting flow path under the partition wall to be refluxed to the fluidized bed of the gasification furnace. The circulating flow of the fluidized medium makes it possible to ensure that the unburned char and the like have a sufficient residence time and complete combustion in the oxidation furnace. It is also possible to provide a secondary air nozzle on the oxidation furnace free board and perform two-stage combustion.

According to one embodiment of the present invention, a combustor is arranged in a pressure vessel, and a pressurized fluidized bed having a heat transfer tube in a fluidized bed in the combustor burns fuel such as coal and oil coke. In a pressurized fluidized bed boiler in a combined cycle power generation system in which combustion gas is introduced into a gas turbine, fluidizing air is jetted upward at the bottom of the combustor at a mass velocity of at least one side higher than the other side. Equipped with an air dispersion device for blocking the upward flow of the fluidizing air jetted from the portion above the air jet portion having a large mass velocity,
In addition, a fluidized bed main combustion chamber is formed by providing an inclined partition wall for reflecting and diverting the fluidizing air toward the upper side of the air jetting portion having a small mass velocity, and the fluidized air is partitioned from the main combustion chamber by the inclined partition wall. A heat recovery chamber is formed, and a heat transfer surface through the heat receiving fluid is provided in the heat recovery chamber,
A heat recovery chamber diffuser is provided at the bottom of the heat recovery chamber, and in the main combustion chamber, the amount of air ejected from the air dispersion device is controlled so that a fluid medium is formed above the air ejection part having a small mass velocity. A moving bed that sediments and diffuses is formed, and a fluidized medium is actively fluidized above the air ejection portion with a large mass velocity to swirl toward the upper portion of the moving bed to form a swirling fluidized bed, and the heat recovery chamber is The upper and lower parts of the partition wall are connected to the main combustion chamber so that a part of the fluidized medium crosses the upper part of the inclined partition wall and enters the heat recovery chamber, and is jetted from the heat recovery chamber diffuser. After controlling the amount of diffused air to settle the fluidized medium in the heat recovery chamber in the state of a moving bed, the fluidized medium is circulated from the lower communication port of the inclined partition wall to the main combustion chamber, and the heat recovery is performed. Above the room Become upper integral of the serial main combustion chamber to form a freeboard, combustion gases from the combustion gases from the heat recovery chamber the main combustion chamber may be mixed.

According to one embodiment of the present invention, in the freeboard, one or more air nozzles are provided on the side surface to blow in secondary air to mix and stir the combustion gas from the main combustion chamber and the heat recovery chamber. However, the unburned substance contained in the combustion gas may be burned sufficiently.
According to one embodiment of the present invention, in the freeboard, a screen is provided between the heat recovery chamber and the main combustion chamber to prevent combustion products having a large particle diameter from jumping into the heat recovery chamber. The combustion gas from the recovery chamber may be allowed to pass while being rectified and sufficiently mixed with the combustion gas in the main combustion chamber.

According to one embodiment of the present invention, a combustor is arranged in a pressure vessel, and a pressurized fluidized bed having a heat transfer tube in a fluidized bed in the combustor burns fuel such as coal and oil coke. In the pressurized fluidized bed boiler in the combined cycle power generation system in which the combustion gas is introduced into the gas turbine, the combustor is formed into a cylindrical shape, and the combustion gas outlet of the combustor is connected to the pressure vessel, and the combustion is performed. A cylindrical partition wall concentric with the cylindrical outer wall of the reactor, the cylindrical partition wall forms a main combustion chamber on the inside and an annular heat recovery chamber on the outside, and the hearth of the main combustion chamber is the central part. Has a conical shape whose height becomes higher and lower toward the periphery, and an air dispersion device configured to eject fluidizing air at a mass velocity at the outer peripheral portion is larger than that at the central portion in the hearth of the main combustion chamber. Providing a mass speed on the cylindrical partition wall Of a large conical slope so as to block the upward flow of the fluidizing air ejected from the portion above the large air ejecting portion and redirect the fluidizing air upward toward the air ejecting portion having a small mass velocity. A partition is provided, a heat transfer surface through which a heat receiving fluid is passed is provided in the heat recovery chamber, and a heat recovery chamber diffuser is provided at the bottom of the heat recovery chamber. In the main combustion chamber, a heat transfer chamber from the air dispersion device is provided. By controlling the amount of ejected air, a moving layer in which the fluidized medium sediments and diffuses is formed above the air jetting portion with a small mass velocity, and the fluidized medium is actively fluidized above the air jetting portion with a large mass velocity, and the moving layer is formed. While swirling toward the upper part to form a swirling fluidized bed, the heat recovery chamber communicates with the main combustion chamber at the upper and lower parts of the partition wall, and a part of the fluidized medium from the upper part of the partition wall. The heat After allowing the fluidized medium in the heat recovery chamber to settle in a moving bed by controlling the amount of air diffused from the heat recovery chamber diffuser so that the fluidized medium is allowed to enter the storage chamber, and then the fluidized medium in the heat recovery chamber is allowed to settle in the state of a moving bed. It may be circulated to the main combustion chamber.

According to one embodiment of the present invention, the upper part of the heat recovery chamber is integrated with the upper part of the main combustion chamber to form a freeboard, and the combustion gas from the heat recovery chamber and the main combustion chamber are integrated. The combustion gas from the above may be mixed. According to one embodiment of the present invention, in the freeboard, a single or a plurality of air nozzles are provided on a side surface of the freeboard to blow in secondary air, and the combustion gas from the main combustion chamber and the heat recovery chamber is mixed and stirred. You may comprise so that the unburned substance contained in combustion gas may be burned sufficiently. According to one embodiment of the present invention, in the freeboard, a screen is provided between the heat recovery chamber and the main combustion chamber to prevent combustion products having a large particle diameter from jumping into the heat recovery chamber. The combustion gas from the recovery chamber may be allowed to pass while being rectified and sufficiently mixed with the combustion gas in the main combustion chamber. According to one embodiment of the present invention, an air diffuser is provided in a hearth portion below a communication port between the main combustion chamber and the heat recovery chamber provided in a lower portion of the partition wall, and the communication port is fluidized. You may do it. According to one embodiment of the present invention, the heat transfer surface of the heat recovery chamber is formed by radially arranged in-layer heat transfer tubes, and the in-layer heat transfer tubes are classified according to use by an evaporation tube block, a steam superheated tube block, and steam. Since it is used as a reheat tube block, it may be divided into several tube groups in plan view. According to one embodiment of the present invention, a dust collector is installed in the passage of the combustion exhaust gas discharged from the combustor, and fly ash collected by the dust collector is collected.
It may be configured to return to the heat recovery chamber through an opening on the side surface of the pressure vessel. According to one embodiment of the invention,
A dust collector is installed in the passage of the combustion exhaust gas discharged from the combustor, and fly ash collected by the dust collector is returned to the main combustion chamber and / or the freeboard through the opening on the side surface of the pressure vessel. It may be configured as follows. According to one embodiment of the present invention, the char generated in the gasification furnace is combusted in the oxidation furnace, and the combustion exhaust gas and the gas generated from the gasification furnace are mixed and combusted at the gas turbine inlet to generate high temperature gas. In a topping cycle combined cycle power generation system that drives a gas turbine and uses it for power generation and compression of combustion air,
A pressurized internal circulation type fluidized bed boiler may be used as the gasification furnace and / or the oxidation furnace.

According to one embodiment of the present invention, in a fluidized bed furnace in a pressurized fluidized bed combined cycle power generation system, the fluidized bed furnace has a cylindrical shape, and a cylindrical partition wall is concentric with the cylindrical outer wall of the fluidized bed furnace. And a cylindrical partition wall to form a gasification furnace on the inside and an annular oxidation furnace on the outside, and the hearth of the gasification furnace has a conical shape in which the central portion is high and decreases toward the periphery. In the hearth of the gasification furnace, an air disperser configured to eject fluidizing air at an outer peripheral portion at a mass velocity larger than that at the central portion is provided, and the cylindrical partition wall has a mass velocity of A conical slanting partition that blocks upward flow of fluidizing air jetted from the large air jetting portion and redirects the fluidizing air upward toward the air jetting portion having a small mass velocity. Part,
An oxidation furnace diffuser is provided at the bottom of the oxidation furnace and is connected to the gasification furnace at an intermediate portion and a lower portion of the partition wall, and in the gasification furnace, the amount of air ejected from the air dispersion device is controlled. A moving layer in which the fluid medium sinks and diffuses is formed above the air jet part with a low mass velocity, and the fluid medium is actively fluidized above the air jet part with a high mass velocity and swirls toward the upper part of the moving layer. By swirling, a swirling fluidized bed is formed, and a part of the fluidizing medium is allowed to enter the oxidation furnace from an intermediate portion of the partition wall, and the amount of air diffused from the oxidation furnace air diffuser is controlled to effect the oxidation. After the fluidized medium in the furnace is settled in a moving bed state, the fluidized medium is circulated from the lower communication port of the partition wall to the gasification furnace, and the upper part of the oxidation furnace and the upper part of the gasification furnace are separated by the partition. By the wall Separated from each other to form freeboards so that the combustion gas from the oxidation furnace and the gas generated from the gasification furnace do not mix and are discharged to the outside from different gas outlets, respectively. The furnace and the gasification furnace may be integrated.

The above-described embodiments have the following effects. (1) Since the combustion chamber and the heat recovery chamber are functionally separated in the same furnace, load control does not depend on the fluidized bed height change method, but the overall heat of the in-layer heat transfer tubes is adjusted by adjusting the air volume in the heat recovery chamber. Since it can be easily carried out by changing the transfer coefficient, complicated operations and equipment required for taking in and out the fluid medium are unnecessary, and agglomeration that occurs when the fluid medium is taken in and out can be prevented. Further, since the fluidized bed temperature can be kept substantially constant even when the load changes, it is possible to always operate under optimal temperature conditions for suppressing NOx, SOx, and the like. Moreover, since the in-layer heat transfer tube is present only in the heat recovery chamber in the gentle fluidized state, it is less worn as compared with the case where it is arranged in the fluidized bed in the violently fluidized state. Further, since the swirl flow is formed inside the fluidized bed, the flow does not stay in the fluidized bed, and the fuel such as coal is uniformly dispersed and burned, so that the occurrence of agglomeration can be prevented. Since the gas that has left the fluidized bed is not cooled by the inner tube, the amount of carbon monoxide (CO) generated can be suppressed to a low level, and the gas turbine efficiency can be prevented from lowering. Furthermore, the upper part of the heat recovery chamber is integrated with the upper part of the main combustion chamber to form a freeboard of a large space, and the combustion gas from the heat recovery chamber and the combustion gas from the main combustion chamber are mixed in this freeboard. It
Therefore, the combustion gas retention time in the freeboard can be lengthened and combustible components can be sufficiently burned in the freeboard. Further, in the freeboard, by blowing the secondary air, the combustion gas from the main combustion chamber and the heat recovery chamber can be mixed and stirred, and the combustion substance contained in the combustion gas can be sufficiently burned.

(2) A partition wall is provided inside the fluidized bed of a cylindrical combustor housed in a pressure vessel configured to maintain an internal pressure equal to or higher than atmospheric pressure, and the main combustion chamber and the heat recovery chamber are separated. The partition wall is composed of a cylindrical partition wall and a conical partition wall, and the conical partition wall blocks the upward passage of the fluidizing air, and redirects the fluidizing air toward the center of the furnace. In addition to functioning as a reflection wall, a conical hearth is provided in the main combustion chamber, and an air dispersion nozzle arranged in the hearth fluidizes the main combustion chamber.
Within the range of concentric circles with a diameter of about 1/2, the minimum fluidization rate is 1 to
Adjust the amount of air blown out from the air dispersion nozzle so that the fluidization state is about 2.5 times and the annular portion outside the concentric circle has a strong fluidization state about 4 to 12 times the minimum fluidization speed. As a result, inside the fluidized bed of the main combustion chamber, the fluidized medium gradually disperses and moves in all directions from the center along the conical hearth surface, and then blows up along the inside of the partition wall, but gradually toward the center. When the cohesive force to the surface of the fluidized bed rises to the highest level, the reaction force turns around and explosively expels the fluidized medium in the circumferential and upward directions, resulting in a large amount of fluidized medium crossing the partition wall and recovering the heat. Enter the room.

On the other hand, the fluidized medium remaining on the surface of the fluidized bed becomes a cylindrical flow in the vicinity of the center and settles while entraining the surrounding fluidized medium, and when it reaches the vicinity of the center of the conical hearth, this time again in the horizontal circumferential direction. A circulatory flow is generated which turns into the movement to.
Due to this circulating flow, a diffusive flow in which the fluidized medium gradually disperses and moves in all directions from the center along the conical hearth surface is generated, so that the fuel and desulfurizing agent are uniformly diffused. Is uniform, there is no agglomeration, the number of coal feeding ports is small, and the coal feeding facility is extremely simplified. The fluid medium remaining on the surface of the fluidized bed becomes a cylindrical flow near the center and settles while entraining the surrounding fluid medium, so that the residence time in the bed of fuel, desulfurizing agent, etc. can be long, improving combustion efficiency and desulfurization. It is extremely effective in improving efficiency.

On the other hand, a large amount of fluid medium crosses the partition wall,
Although it enters the heat recovery chamber, at this time, the free board above the main combustion chamber and the heat recovery chamber is provided with a comb-shaped screen so as to surround the heat recovery chamber so that solids such as coal with coarse particles can be solidified. Since the mixture of fuel can be prevented, formation of agglomeration can be avoided even though the heat recovery chamber fluidized bed is in a gentle fluidized state within twice the minimum fluidization rate. This screen acts as a baffle for the combustion gas generated from the heat recovery chamber, and has the effect of being sufficiently mixed and stirred with the combustion gas generated from the main combustion chamber.

Particularly, in a pressurized fluidized bed boiler, a large amount of unburned matter in the combustion exhaust gas naturally lowers the combustion efficiency, but in a dust collecting device provided further downstream, for example, in a cyclone. Combustion of unburned material causes agglomeration formation, and in the case of a ceramic filter, problems such as combustion on the filter surface and damage to the filter occur, leading to serious problems such as operation failure. linked. Therefore, it is desirable to completely burn combustible components in the combustion furnace, and the stirring and mixing effect due to the baffle action of the screen has a secondary air introduction method, a freeboard height, a combustion gas retention time in the freeboard, etc. They also act synergistically, and have a great effect on burning the combustible components in the fuel sufficiently in the freeboard.

(3) Since the internal circulating fluidized bed boiler of the present invention has no heat transfer surface in the main combustion chamber, it is possible to burn the main combustion chamber in a reducing atmosphere. Therefore, by setting the distribution ratio of combustion air, the main combustion chamber is supplied with less than the theoretical amount of air required for combustion, and the heat recovery chamber is supplied with the amount of air required for control to ensure complete combustion. The remaining amount of air required for the second-stage combustion is performed by using a plurality of secondary air nozzles provided on the freeboard as secondary air.
As a result, the main combustion chamber is burned in a reducing atmosphere, and the volatile components of coal are actively released by reducing combustion, and hydrocarbons such as CH ₄ and CO or gas-phase N species (NHi, HCN, etc.) in the gas-phase reaction. And the like reduce the nitrogen oxides generated by combustion, and at the same time bring about the effect of reducing the selectivity of conversion of N chemical species into oxides, and thus low NOx combustion becomes possible.

(4) By providing an air chamber and an air diffuser in the lower part of the partition wall and in the hearth of the connecting flow passage, the entire connecting flow passage is fluidized and flows through the heat recovery chamber to the main combustion chamber. The amount of media can be increased. The air chamber may be in communication with the heat recovery control air chamber, or may be controlled independently of the air chamber, and in the case of independent control, the fluidized medium is independent of the aeration amount of the heat recovery chamber. The amount of circulation can be controlled,
It is also possible to act as a kind of control valve. As a result, it is possible to lubricate a larger amount of fluidized medium than in the case of the rectangular combustion furnace, and it is possible to take advantage of the characteristics of the cylindrical combustion furnace in which the heat recovery chamber can be made larger than in the case of the rectangular combustion furnace.

(5) In-layer heat transfer tubes are radially arranged inside the heat recovery chamber flow tank, and are used as an evaporation tube block, a steam superheater tube block, and a steam reheat tube block according to the purpose, so that they can be seen in a plan view. It is possible to adjust the amount of air diffused from the hearth of the heat recovery chamber for each block by arranging the pipes separately for each function, and to independently control the heat collection amount of each block. . Also, between each block,
There is a maintenance space, which is effective for checking the heat transfer tubes in the layers. Further, the maintenance space is not always necessary, and if the maintenance space is not provided, it becomes more compact.

(6) The fly ash collected by the cyclone provided in the combustion exhaust gas system is returned to the heat recovery chamber, whereby the average particle size and specific weight in the heat recovery chamber are reduced. This is because the average particle size in the main combustion chamber is about 0.6 mm, whereas the particle size that is entrained in the combustion exhaust gas and collected by the cyclone and recycled is much smaller, and since char is also included, the specific weight is also small. In the heat recovery room,
Since the fluidizing gas velocity is as small as about twice the minimum fluidizing velocity, recycled particles are not re-scattered, and therefore the average particle size and specific weight in the heat recovery chamber are smaller than those in the main combustion chamber.

Since the minimum fluidization rate (Umf) is proportional to the square of the particle diameter of the fluidized medium and also to the specific weight, the fluidization rate of the heat recovery chamber is considerably smaller than that of the main combustion chamber. Therefore, the amount of air for heat recovery control can be considerably reduced as compared with the case where the heat recovery chamber is not recycled, and as a result, the fluidized gas velocity (U0) in the heat recovery chamber becomes small. Since the wear rate of the in-layer heat transfer tubes arranged in the heat recovery chamber is proportional to the cube of the fluidizing gas velocity (U0), the wear is greatly reduced by decreasing U0. Also, the heat recovery control air constantly fluctuates in order to control the temperature of the fluidized bed in the main combustion chamber, but the small amount of this air reduces the influence of fluctuations in the heat recovery air amount on combustion. It is very effective for stable combustion.

(7) To install a dust collector in the passage of the combustion exhaust gas derived from the cylindrical internal circulation fluidized bed boiler, and to recover the unreacted desulfurizing agent and the unburned carbon content from the collected fly ash. By classifying the fly ash according to the particle size into three stages of large, medium and small, and by returning only the fly ash of the intermediate particle size to the main combustion chamber and / or the freeboard and / or the fuel supply system, The highest char concentration is usually 10-6
Since only particles in the range of about 0 μm can be returned to the cylindrical combustor, NOx can be reduced, combustion gas system wear can be reduced, and combustion efficiency can be increased with the minimum amount of circulating ash.

(8) In the topping cycle combined cycle power generation system, a pressurized internal circulation type fluidized bed boiler is used in the gasification furnace and / or the oxidation furnace, and all the unburned char discharged from the gasification furnace is caused to accompany the generated gas. After being cooled to 600 ° C or below and collected by the dust collector installed in the subsequent stage,
After being introduced into the oxidation furnace and completely burned, the combustion exhaust gas is cooled down to 600 ° C or less after leaving the oxidation furnace, and the particles containing Na and K are collected and discharged by the dust collector installed in the latter stage to make it clean. Combustion gas that has become clean and the produced gas that has been collected and discharged after leaving the gasification furnace and that contains Na and K and is clean is mixed and combusted in a topping cycle combustor, and the high temperature combustion that is generated Since the gas is introduced into the gas turbine, the combustion gas does not contain alkali metals such as Na and K that cause high temperature corrosion of the gas turbine blade. It is possible to deal with.

[0034]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of a pressurized internal circulation type fluidized bed boiler according to the present invention will be described below with reference to the drawings. (Embodiment 1) FIG. 1 is a vertical sectional view of a pressurized cylindrical internal circulation type fluidized bed boiler of the present invention, and FIG.
It is a sectional view taken along the line (a) -II (a). The embodiment shown in FIG. 1 is an embodiment in which a cylindrical internal circulation type fluidized bed boiler is built in a cylindrical pressure vessel, and the schematic configuration of the present invention will be described using this.

The pressure vessel 1 has a cylindrical shape, the upper surface is a mirror plate having a combustion gas outlet 4, and the lower surface is a mirror plate having a flow air inlet 3, a heat recovery chamber control air inlet 5 and the like. It is configured so as to be able to maintain an internal pressure equal to or higher than atmospheric pressure. Although the pressure vessel 1 shown in FIG. 1 has a cylindrical shape, it may have a spherical shape.

A cylindrical combustor 2 is arranged inside the pressure vessel 1, and the cylindrical combustor 2 is one closed vessel having a cylindrical outer wall 11 formed by connecting water pipes, A combustion chamber fluidized bed is formed therein. A combustion gas outlet 2a is provided at the upper end of the cylindrical combustor 2,
The combustion gas outlet 2a is joined to the combustion gas outlet 4 of the pressure vessel 1. The bottom of the cylindrical combustor 2 is supported by a cylindrical support 7 mounted on the lower end plate of the pressure vessel 1.

A partition wall 8 is provided inside the fluidized bed of the cylindrical combustor 2.
The partition wall 8 separates the main combustion chamber 9 and the heat recovery chamber 10. The partition wall 8 is composed of a water pipe taken out from the cylindrical outer wall 11, and this water pipe is further covered with a fire resistant material. The partition wall 8 is composed of a cylindrical partition wall 8a and a conical partition wall 8b formed on the upper portion of the cylindrical partition wall 8, and the conical partition wall 8b blocks the upward flow passage of the fluidizing air to flow. It functions as a reflection wall that redirects chemical air toward the center of the furnace.
As a result, a swirling flow is generated inside the main combustion chamber 9 as shown by the arrow. The freeboard 31 is integrally formed above the main combustion chamber 9 and the heat recovery chamber 10. Heat recovery room 1
There is no partition wall between the freeboard on the upper part of 0 and the freeboard on the upper part of the main combustion chamber 9, and the freeboard 31 is an integrated space, so that the combustion gases of both sides freely pass each other. It is configured.

Further, in the heat recovery chamber 10, an intra-layer heat transfer tube 15 branched from an upper header 13 for inner layer tube and a lower header 14 for inner layer tube provided outside the outer wall 11 of the cylinder is arranged. The inner heat transfer tubes 15 are radially arranged when seen in a plane as shown in FIG. Pressure vessel 1
The water inlet 16 is installed in the lower part of the
Boiler water introduced from No. 6 is introduced into the inner layer lower header 14 via the connecting pipe 16a after passing through the cylindrical outer wall 11 and distributed from the inner layer lower header pipe 14 to the inner heat transfer pipe 15. To be done. And the in-layer heat transfer tube 15
The steam generated in 1 is collected in the upper header 13 for the inner layer pipe, and is discharged to the outside from the steam outlet 17.

On the other hand, the pressure vessel 1 is provided with a pressure equalizing nozzle 18, and a pressure equalizing air system 19a is branched from a high pressure flow air system 19 connected to the flow air inlet 3 to divide the pressure equalizing nozzle. The pressure vessel 1 and the cylindrical combustor 2 are connected to each other 18 so that the pressure inside the pressure vessel 1 and the inside of the cylindrical combustor 2 are substantially uniform except for the pressure loss of the fluidized bed, and the combustor 2 has a non-pressure resistant structure. However, in this case, the freeboard 3 of the cylindrical combustor 2
In No. 1, the external pressure corresponding to the fluidized bed pressure loss is received. Further, when a pressure reducing valve or the like is provided in front of the pressure equalizing nozzle 18 so that the space 36 between the pressure vessel 1 and the cylindrical combustor 2 and the freeboard 31 become equal in pressure, the cylindrical combustor 2 Of these, the portion below the fluidized bed receives the internal pressure corresponding to the fluidized bed pressure loss. Further, the pressure vessel 1 is provided with a coal feeding inlet 6, and the coal feeding inlet 6 is connected to the coal feeding nozzle 22.

In the main combustion chamber 9, there is installed a conical hearth 20 whose center is high and which is lowered toward the outer peripheral side.
An air dispersion nozzle 21 is installed in the hearth 20. The air dispersion nozzle 2 communicating with the fluidizing air inlet 3
Fluidizing air is jetted from 1 to fluidize the fluidizing medium in the main combustion chamber 9. Also, the coal feeding nozzle 2
2 is open in the vicinity of the hearth 20 of the main combustion chamber 9 and in the vicinity of the partition wall 8. Although the mass velocity of the fluidizing air ejected from the outer peripheral annular portion of the air dispersion nozzle 21 is a velocity sufficient to form a fluidized bed of the fluidized medium in the furnace, it is ejected from the central portion of the air dispersion nozzle 21. The mass velocity of the fluidizing air is selected to be smaller than that of the outer peripheral annular portion. by this,
Within the range of a concentric circle having a diameter of about ½ of the main combustion chamber 9, a gradual fluidization state of about 1 to 2.5 times the minimum fluidization speed is set, and the annular portion outside the concentric circle has the minimum fluidization speed. 4-1
The fluidized medium is made to be about twice as strong as the fluidized state. Inside the fluidized bed of the main combustion chamber, the fluidized medium gradually disperses and moves in all directions along the conical hearth surface, and then the outer peripheral annular portion. At that point, the moving direction turns upward due to the high fluidization speed and blows up along the inside of the partition wall 8, but the cohesive force in the central direction gradually increases and reaches the maximum on the surface of the fluidized bed. Then, due to the reaction force, the fluid medium is explosively scattered in the circumferential direction and the upward direction.

As a result, a large amount of fluid medium passes through the partition wall 8 and enters the heat recovery chamber 10. At this time, since the fluidized bed in the heat recovery chamber is in a gentle fluidized state within twice the minimum fluidization rate, it is in a state where agglomeration is likely to occur,
It is necessary to avoid mixing of solid fuel such as coarse-grained coal. Therefore, the freeboard 31 is provided with a screen 12 composed of a water pipe and a protector having a comb-teeth shape so as to surround the heat recovery chamber 10, and the screen 12 prevents the inflow of coarse solid fuel. A baffle effect is exerted on the combustion gas generated from the heat recovery chamber 10, so that the combustion gas generated from the main combustion chamber 9 is sufficiently mixed and stirred.

Especially in a pressurized fluidized bed boiler, the large amount of unburned matter in the combustion exhaust gas naturally lowers the combustion efficiency, but it does not occur in a dust collector provided further downstream, for example, in a cyclone. Combustion of fuel occurs and agglomeration is formed.In the case of a ceramic filter, troubles such as combustion on the filter surface and damage to the filter occur, leading to serious problems such as operation failure. Come on. Therefore, it is desirable to completely combust combustible components in the combustion furnace, and the effect of stirring and mixing by the baffle action of the screen 12 is the secondary air charging method described later, the freeboard height, and the combustion gas retention in the freeboard. It also acts synergistically with time, etc., and has a great effect on burning the combustibles in the freeboard sufficiently.

On the other hand, the fluidized medium remaining on the surface of the fluidized bed becomes a cylindrical flow in the vicinity of the center and sinks while entraining the surrounding fluidized medium, and when it reaches the vicinity of the center of the conical hearth, this time again in the horizontal omnidirectional direction. A circulatory flow is generated which turns into the movement to.
Due to the effect of this circulating flow, a coal feeding nozzle 2 provided near the hearth
CWP (Coal Water Paste) etc. introduced from 2 is evenly distributed in all directions of the main combustion chamber, and even with a simple coal feeding facility, uneven distribution of fuel is avoided and there is no fear of clinker generation.

Further, the heat recovery chamber 10 is provided with a hearth 23 having an inverted conical shape, the height of which is higher from the inner peripheral side toward the outer peripheral side, and the air dispersion nozzle 24 is installed in the hearth 23. Air is jetted from the air dispersion nozzle 24 communicating with the heat recovery chamber control air inlet 5 to gently flow in the heat recovery chamber 10 so that the heat recovery chamber 10 is crossed over the partition wall 8.
The fluidized medium entering is slowly settled in the heat recovery chamber fluidized bed while being cooled by the in-layer heat transfer tube 15, and then passes through the connecting flow passage 27 below the partition wall 8 along the inclined hearth. Return to the main combustion chamber fluidized bed. As a result, the amount of heat generated in the main combustion chamber 9 is effectively recovered through the in-layer heat transfer tube 15 in the heat recovery chamber 10. Further, an air introduction pipe 25 and a rear air diffuser nozzle 26 are also provided on the rear surface of the conical partition wall 8b to fluidize the fluidized medium that has entered the heat recovery chamber 10,
Although it can be partially burned, it may not be provided when the angle of the conical partition wall 8b is increased.

A fluid combustion air chamber 28 is formed below the main combustion chamber hearth 20. The fluid combustion air chamber 28 is surrounded by a water pipe 29 supporting the partition wall 8 and connected to the fluid air inlet 3. There is. A heat recovery control air chamber 30 is formed below the heat recovery chamber hearth 23, and the heat recovery control air chamber 30 is connected to the outside by a heat recovery control air inlet 5.

The upper part of the heat recovery chamber 10 is integrated with the upper part of the main combustion chamber 9 to form a wide space freeboard 31, and the combustion gas from the heat recovery chamber 10 and the main combustion chamber 9 are formed in the freeboard 31. With the combustion gases from. Therefore, the combustion gas retention time in the freeboard 31 can be lengthened, and combustible components can be sufficiently burned in the freeboard 31. Further, a plurality of secondary air nozzles 33 are installed on the freeboard 31, so that the two-stage combustion system can be adopted. Reference numeral 34 is a secondary air inlet. Since the internal circulation fluidized bed boiler of the present application has no heat transfer surface in the main combustion chamber 9, it is possible to burn the main combustion chamber in a reducing atmosphere. Volatile emission of coal is actively carried out by reducing combustion, and hydrocarbons such as CH ₄ and CO or gas-phase N species (NHi,
Low NOx combustion is possible because HCN and the like) reduce nitrogen oxides produced by combustion and reduce the selectivity of conversion of N chemical species into oxides. Therefore, the main combustion chamber 9 is supplied with not more than the theoretical air amount required for combustion, the heat recovery chamber 10 is supplied with an amount of air required for control, and the remaining amount of air required for complete combustion is 2 A two-stage combustion system in which secondary air is supplied from the secondary air nozzle 33 to the freeboard 31 is used as secondary air.

Further, in the freeboard 31, the combustion gas is prevented from short-circuiting and flowing to the combustion gas outlet 4, and the baffle 32 is provided so as to perform sufficient stirring and mixing combustion inside the freeboard.
Providing is also an option. However, the baffle is not necessary when the mixing and stirring with the secondary air is sufficient, the superficial velocity is slow, the freeboard height is sufficient, and there is no possibility of a short circuit flow of the combustion gas.

FIG. 2B is a view showing a modification of FIG. 2A. As shown in FIG. 2B, the in-layer heat transfer tube group is the evaporation tube block 40, No. 1 steam superheater tube block 41,
No. 2 steam superheater tube block 42, No. No. 3 steam superheater tube block 43, and further steam reheater tube block 44 are divided by function, and in the case of the through-flow type, although not shown, they pass through the connecting tubes, respectively, and evaporate tube block 40, No. 1 steam superheater tube block 41, No. 1 2 steam superheater tube block 42, No. 3 Steam heating tube block 43
Steam flows in this order. The generated superheated steam is guided to the high-pressure steam turbine, then returns to the steam reheat pipe block 44 to be heated again, and then is introduced into the intermediate-pressure steam turbine.

As a result of the division by function, the heat collection amount of each block can be controlled independently by controlling the amount of air diffused from the hearth of the heat recovery chamber for each block. It is possible. A maintenance space 45 is provided between the blocks, which is effective for inspecting the intra-layer heat transfer tube. Further, the maintenance space is not always necessary, and if the maintenance space is not provided, it will be a little more compact than this figure.

FIG. 3 is an explanatory view for explaining the control system of the air system according to the load change. When the load changes, the steam flow rate of the steam outlet (turbine inlet steam system) 17 changes, and the flow meter accordingly. The steam flow rate signal of F31 changes. The calculator Y0 calculates the output signal of the steam pressure regulator P31 in addition to the flow signal from the flow meter F31, and outputs the output signal. This output signal is sent to the fuel system to supply fuel according to the load and is also input to the calculator Y0 'of the air system.

In the computing unit Y0 ', in addition to the input signal from Y0, the output signal of the oxygen concentration controller A25 provided in the combustion exhaust gas system 50 and the heat recovery control air flow controller F21.
The air flow rate signals from are calculated and combined, and the amount of combustion air is adjusted so that the oxygen concentration in the oxygen concentration controller A25 becomes constant. As a result, a signal indicating the remaining air amount obtained by subtracting the heat recovery chamber air amount from the combustion air amount is output. Based on the output signals, the computing units Y1 and Y2 perform computations so that the flowing air amount and the secondary air amount are supplied at a constant ratio, and the flowing air flow rate controller is controlled by the output signals from Y1 and Y2, respectively. F22, the secondary air flow controller F24 is controlled.

By setting the ratio, the main combustion chamber 9 is supplied with air in an amount equal to or less than the theoretical air amount required for combustion, and the heat recovery chamber 10 is supplied with an amount of air required for control, and further required for complete combustion. The remaining amount of remaining air can be supplied to the freeboard 31 as secondary air for two-stage combustion. Therefore, the main combustion chamber 9 can be burned in a reducing atmosphere, the volatile matter of the coal is actively released by the reducing combustion, and hydrocarbons such as CH ₄ and CO or gas phase N species (NHi) in the gas phase reaction. , HCN, etc.) reduces nitrogen oxides produced, and also reduces the selectivity of conversion of N chemical species into oxides, resulting in low NOx combustion.

On the other hand, the output signal of the steam pressure regulator P31 controls the fluidized bed temperature regulator T58 via the calculator Y31. That is, when the steam pressure drops a little, Y
The output signal from 31 slightly lowers the layer temperature set value of T58. Along with that, the operation signal from the fluidized bed temperature controller T58 changes and acts on the heat recovery air flow rate controller F21 via the calculator Y21, resulting in an increase in the heat recovery air amount. Since the overall heat transfer coefficient of the in-layer heat transfer tube in the heat recovery chamber is almost proportional to the fluidizing gas velocity in the fluidized bed in the heat recovery chamber as shown in FIG. The amount of heat collection increases and the steam pressure recovers. This reverse operation occurs when the steam pressure exceeds the set value, and the steam pressure is reduced by decreasing the heat recovery air amount. In this way, the main operation is to adjust the fuel supply amount, and the secondary operation is to adjust the heat recovery air amount to minimize the effect of load changes and enable quick and stable control. Is.

Further, by connecting the outlet gas of the gas turbine 38 and the air intake port of the compressor 39 and adjusting the amount of combustion exhaust gas mixed in the supply air with the valve 49, NOx can be reduced and fluidization at low load can be achieved. Since the flow can be stabilized by increasing the speed, it is described in FIG. 3 for the time being, but basically the system can be configured without it.

FIG. 5 is an explanatory view showing the detailed structure of the cylindrical combustor 2 shown in FIG. In the case of the cylindrical combustion furnace as shown in FIG. 1, the heat recovery chamber 10 expands in an annular shape outside the partition wall 8, and the heat recovery chamber can be made larger than in the case of the rectangular combustion furnace, so that a large number of heat transfer chambers can be provided. It is possible to arrange heat tubes. Therefore, in order to make the best use of the characteristics, it is necessary to circulate a larger amount of fluid medium than in the case of the rectangular combustion furnace. However, conventionally, since there is no air diffuser in the lower part of the partition wall 8 and the communication passage 27, it is secondarily fluidized by the flowing air from the heat recovery chamber air dispersion nozzle 24 and the main combustion chamber air dispersion nozzle 21. However, there was a portion where the flow was not active like the reference numeral 27a in the figure. In order to eliminate this, an air chamber 30 'and an air dispersion nozzle 24' are provided in the lower part of the partition wall 8 and in the hearth of the connecting flow passage 27. As a result, the entire communication passage 27 is fluidized, and the amount of the flowing medium that circulates through the heat recovery chamber 10 to the main combustion chamber 9 can be increased. The air chamber 30 ′ may be in communication with the heat recovery control air chamber 30 or may be controlled independently of the air chamber 30. In the case of independent control, it is possible to control the circulating amount of the fluidized medium regardless of the aeration amount of the heat recovery chamber, and it is also possible to perform an operation like one kind of control valve.

(Embodiment 2) FIG. 6 is an explanatory view showing a second embodiment of the present invention including a combustion exhaust gas treatment system. As shown in FIG. 6, the combustion exhaust gas discharged from the pressure vessel 1 is guided to the exhaust gas system 50 and introduced into the cyclone 51. The fly ash collected by the cyclone 51 falls by gravity and is stored in the seal mechanism 52 while being recycled by the ash recycled air 5
3, the heat recovery chamber 1 via the recycled ash introduction pipe 54 penetrating the side surface of the pressure vessel 1 and the cylindrical combustor 2.
It is set back to 0.

By recycling fly ash to the heat recovery chamber 10, the average particle size and specific weight in the heat recovery chamber are reduced. While the average particle diameter in the main combustion chamber 9 is about 0.6 mm, the particle diameter entrained in the combustion exhaust gas and collected by the cyclone and recycled is much smaller, and since char is also included, the specific weight is also small. Since the fluidizing gas velocity in the heat recovery chamber 10 is as low as about twice the minimum fluidizing velocity,
The recycled particles do not scatter again, and therefore the average particle size and specific weight in the heat recovery chamber 10 are
Will be smaller than.

Since the minimum fluidization rate (Umf) is proportional to the square of the particle size of the fluidized medium and also to the specific weight, the minimum fluidization rate of the heat recovery chamber is considerably smaller than that of the main combustion chamber. . Therefore, the amount of air for heat recovery control can be considerably smaller than that in the case where it is not recycled to the heat recovery chamber, and as a result, the fluidized gas velocity (UO) in the heat recovery chamber
Becomes smaller. Since the wear rate of the in-layer heat transfer tube arranged in the heat recovery chamber is proportional to the cube of the fluidized gas velocity (UO), the wear is greatly reduced by the decrease of UO. Further, the heat recovery control air amount is constantly fluctuating in order to control the fluidized bed temperature of the main combustion chamber 9 as shown in FIG. 3. However, the small air amount means that the heat recovery air amount The effect of fluctuations on combustion is reduced, which is extremely effective for stable combustion.

Further, as shown in FIG. 6, the exhaust gas is further introduced into the dust collector 55 via the cyclone 51. The dust collector 55 is composed of, for example, a ceramic filter or a high temperature bag filter. The fly ash collected there is cooled by the ash cooler 56 and then discharged through the lock hopper 57 under atmospheric pressure. On the other hand, the high temperature exhaust gas collected and cleaned is introduced into the gas turbine 58. As for fuel, the coal stored in the raw coal bunker 59 was crusher 6
0 is crushed and sent to the agitation tank 61, and the desulfurizing agent charged from the desulfurizing agent bunker 62 and water 64 are agitated and mixed to produce a slurry-like fuel, which is sent to the combustor 2 by the slurry pump 65 and fed with coal. It is supplied from the nozzle 22 into the fluidized bed of the main combustion chamber.

It is also possible to recycle fly ash to the freeboard 31 by the recycle ash introduction pipe 54a. At this time, the concentration of particles in the freeboard is increased, the stirring effect of the combustion gas is increased, and the contact effect between the unburned char and the unreacted desulfurizing agent and the combustion gas is increased. As a result, the combustion efficiency is increased and the desulfurization and denitration performance is improved. In addition, the recycled ash introduction officer 54a is extended to near the center of the main combustion chamber 9,
Fly fly ash is recycled C on the surface of or in the moving bed, and by entraining it in the descending fluidized medium, sufficient retention time is taken in the fluidized bed of the main combustion chamber to improve combustion of unburned components and desulfurization and denitration reaction. It is also possible to contribute to.

The pressurized internal circulation type fluidized bed boiler shown in FIG. 1 is a once-through type, but is shown as a forced circulation type boiler in FIGS. 6 to 8. In the forced circulation type boiler, a brackish water cylinder 71 is provided, and water is supplied thereto by the boiler water supply system 70, while the forced circulation pump 72 passes the forced circulation pipe 73 to the water pipe wall or the evaporation pipe in the heat recovery chamber layer. Circulate can water to. On the other hand, the steam 74 generated in the brackish water cylinder 71 is sent to a superheat pipe provided in the heat recovery chamber layer by a connecting pipe (not shown), and the superheated steam 74 'generated there is supplied to the high pressure steam turbine.

(Embodiment 3) FIG. 7 is an explanatory view showing a third embodiment of the present invention including a combustion exhaust gas treatment system.
As shown in FIG. 7, the fly ash collected by the cyclone 51 provided in the middle of the exhaust gas system 50 is cooled by the ash cooler 77. Although not shown in the drawing, it is possible to effectively collect heat by using water supply to the boiler or flowing air as the cooling medium. The cooled fly ash is introduced into the classification tank 79 via the lock hopper 78, and is mixed with the fly ash obtained from the dust collector 55 via the ash cooler 56 and the lock hopper 57 to be classified. In this figure, an example of fluidized bed classification is shown in which the classification air 80 is introduced through the diffuser pipe 81, but the invention is not necessarily limited to this.

Usually 60 separated selectively in the classification tank 79
Unreacted desulfurizing agent and unburned carbon having a particle diameter of μm or less are carried to the cyclone 83 by air. The particles further classified here, about 10 μm or less, are introduced into the dust collector 84, separated from the transfer air, and then discharged to the outside. On the other hand, fly ash with a particle size of 10 to 60 μm discharged from the cyclone 83 is introduced into the cylindrical combustor 2 by the recycled ash pressure feed air 88 through the seal valve 85, the lock hopper 86, and the rotary valve 87. When returning to the combustor 2,
When the method of returning to the heat recovery chamber by using the recycled ash introduction pipe 54, the characteristics as described in the detailed description of FIG. 6 can be exhibited, and the fly ash can be recycled to the freeboard 31 by the recycled ash introduction pipe 54a. Is possible. At this time, the particle concentration in the freeboard increases, the effect of stirring the combustion gas is increased, and the contact efficiency between the unburned char and the unreacted desulfurizing agent and the combustion gas is increased. As a result, the combustion efficiency is increased and the desulfurization and denitration performance is improved.

Further, by extending the recycle ash introduction pipe 54a, the fly ash is recycled near the center of the main combustion chamber 9 and on the surface of or in the bed of the moving bed, and the fly ash is entrained in the descending fluidized medium to flow in the main combustion chamber. It is also possible to contribute to the combustion of unburned components and the improvement of desulfurization and denitration reaction by taking sufficient residence time in the layer. In this way, the particles are classified into three stages according to the particle size, and only the particles having the highest char concentration in the range of about 10 to 60 μm are returned to the cylindrical combustor 2 to reduce NOx with a minimum amount of circulating ash and to reduce the combustion gas system. It is possible to improve effects such as wear reduction and combustion efficiency increase.

Further, although the cyclone 51 and the dust collecting device 55 are two-stage dust collecting in this figure, the cyclone 51, the ash cooler 77 and the lock hopper 78 can be eliminated and the dust collecting device 55 can be used alone. is there. Also, at that time, the ash cooler 56,
The classification may be performed under pressure without using the lock hopper 57. A ceramic filter is usually used for the dust collector 55.

FIG. 8 shows another example of treating classified fly ash. 60 normally separated by the classification tank 79
Unreacted desulfurizing agent and unburned carbon having a particle diameter of μm or less are carried to the cyclone 83 by air. The particles further classified here, about 10 μm or less, are introduced into the dust collector 84, separated from the transfer air, and then discharged to the outside. On the other hand, fly ash with a particle size of 10 to 60 μm discharged from the cyclone 83 is stored in a hopper 89 after passing through a seal valve 85, a lock hopper 86, and a rotary valve 87, and then mixed with coal and a desulfurizing agent in a mixing device 90. Is mixed with the particulate fuel and is supplied to the cylindrical combustor 2 by the fuel pressure-fed air. On the other hand, 10 to 10 discharged from the rotary valve 87
The fly ash of 60 μm is pneumatically transported not by the combustion system but by the secondary air 34, and the free air 31 is fed from the secondary air nozzle 33.
It is also possible to input to.

(Embodiment 4) FIG. 9 is one of the embodiments of the present invention and shows an example of an overall system diagram as a pressurized fluidized bed boiler. The system shown in FIG. 9 will be briefly described. The boiler shown in the figure is configured as a once-through type boiler, and during operation, slurry fuel is supplied to the combustor 2 by the slurry pump 65.
And is supplied to and burned in the fluidized bed of the main combustion chamber 9. The combustion exhaust gas passes through the exhaust gas system 50, is dust-removed by the dust collector 55, drives the high-pressure gas turbine 100 and the low-pressure gas turbine 101, and then further exhausts the gas cooler 10.
The boiler feed water is heated by 2 and is emitted into the atmosphere from the chimney 103.

On the other hand, the flow combustion air is boosted by the low pressure compressor 104 and the high pressure compressor 106 driven by the gas turbine, and a part of it is branched as heat recovery control air and introduced into the heat recovery control air chamber 30. The rest is introduced into the fluid combustion air chamber 28, and combustion is performed while the fluid medium in the main combustion chamber 9 is swirlingly fluidized. Regarding the steam system, the feed water is sent to the boiler by the boiler feed water pump 107 while being heated by the exhaust gas cooler 102 on the way.
After passing through the water pipe forming the cylindrical wall, it becomes superheated steam through the evaporation pipe 108 and the steam superheat pipe 109 in the heat recovery chamber layer. The generated superheated steam drives the high-pressure steam turbine 110, then returns to the combustor 2 again, and the in-layer heat transfer tube 111 for reheating is used.
After being heated in the medium pressure turbine 112, low pressure turbine 1
After driving 13 and generating electricity with the generator 114, the condenser 11
It becomes condensate at 5 and is used again as boiler feed water.

(Embodiment 5) FIG. 10 shows Embodiment 1 of the present invention.
As one example, an example in which an internal circulation type fluidized bed boiler is incorporated as an oxidation furnace of a topping cycle combined cycle power generation system will be shown. Further, although not particularly shown, it is also possible to use the pressurized cylindrical fluidized bed boiler according to the present invention as a gasification furnace of the topping cycle combined cycle power generation system shown in FIG. The application to the gasification furnace can be explained as follows. That is, as described in detail with reference to FIGS. 1 and 3, the heat transfer surface is not arranged in the main combustion chamber 9 of the pressurized internal circulation type fluidized bed boiler of the present application. Therefore, for the purpose of reducing NOx, 2
Stage combustion is performed, and as a result, the main combustion chamber 9 is burned in a reducing atmosphere with an air ratio of about 0.8. Moreover, the main combustion chamber 9
Since the inside of the furnace is configured to have a difference in fluidized gas velocity, the actual air ratio in the moving layer of the main combustion chamber is about 0.5.
And the operation is close to that of a gasifier. Therefore, it is extremely easy to switch to a gasification furnace for a topping cycle.In terms of heat balance, if heat recovery in the bed is unnecessary, it is sufficient to stop the heat recovery control air, and remove the heat transfer tube in the bed. May be.

Here, a schematic system will be described with reference to FIG. First, coal 121 and desulfurizing agent 12 are placed in the gasification furnace 120.
2 is supplied and decomposed into coal gas, char, CaS and the like by the air 124 inside the gasification furnace 120. Char and CaS and the like are discharged from the gasification furnace 120 and from the dust collector 123 provided in the coal gas passage, introduced through the passage 125 into the oxidation furnace 126 including an internal circulation type fluidized bed boiler, It is supplied near the hearth of the cylindrical combustor 2. The supply destination is not necessarily near the hearth and may be on the fluidized bed.

In the oxidation furnace 126, coal 121 and desulfurizing agent 1
It is also possible to supply 22 and it is thrown into the main combustion chamber 9 through the coal feeding nozzle 22 and burns together with the char. On the other hand, the combustion gas generated in the oxidation furnace 126 is the dust collector 1
After the dust is removed by 27, it is introduced into the combustor 129 at the inlet of the gas turbine 128, is discharged from the gasification furnace 120 there, and is mixed and burned with the coal gas removed by the dust collector 123 and the dust collector 130 to produce a high temperature gas. Therefore, the gas turbine 128 is driven with high efficiency.

Further, the gas turbine 128 drives the compressor 131 and the generator 132. Gas turbine 12
The exhaust gas exiting from No. 8 is cooled by the heat recovery device 133 and then released into the atmosphere. On the other hand, the superheated steam 74 'generated in the boiler
After driving the steam turbine 134 and the generator 135 connected to the turbine 134, the steam returns to the condensate by the condenser 136 and is supplied to the boiler again by the boiler water supply pump 137. The operation of the pressurized cylindrical fluidized bed boiler inside the oxidation furnace 126 is the same as in the first to fourth embodiments.

(Sixth Embodiment) FIG. 11 shows a first embodiment of the present invention.
The gasification furnace 120 and the oxidation furnace 126 of the topping cycle combined cycle power generation system are equipped with a pressurized cylindrical fluidized bed boiler.
An example incorporated as is shown. In FIG. 11, coal 121 and desulfurizing agent 122 are supplied to a gasification furnace 120, and air 19 is supplied for partial combustion gasification.
In addition to air, 150 oxygen or 1 steam as oxidant
It is also possible to add 51.

All the unburned chars and the like generated in the gasification furnace 120 are entrained with the generated gas and cooled to 600 ° C. or lower by the gas cooling device 140 installed in the subsequent stage, and Na which causes high temperature corrosion of the gas turbine blades. , K or the like is solidified or fixed on the surface of the particles, the particles are collected by the dust collector 141, and then introduced into the oxidation furnace 126 to be completely burned. The combustion exhaust gas of the oxidation furnace 126, after exiting the oxidation furnace 126, is cooled by a gas cooling device 142 installed in the subsequent stage to 600
Na, K cooled to below ℃ and solidified by this cooling
Alkali metal particles such as are collected and discharged by the particle dust collector 143. Ceramic filters are usually used for the dust collectors 141 and 143.

Combustion gas cleansed by removing Na and K, which cause high temperature corrosion, and product gas cleansed after leaving the gasification furnace 120, are mixed and burned in a combustor 129. , Combustor 1 by cooling each gas
Since the combustion temperature at 29 is slightly lowered, the combustion exhaust gas amount is reduced by operating the oxidation furnace 126 with the excess air ratio as low as possible in order to prevent the combustion temperature from decreasing. Therefore, the amount of oxygen required in the combustor 129 is separately supplied to the combustor as oxygen 150.

The high temperature combustion gas generated in the combustor 129 drives the gas turbine 128 with high efficiency. Then, the gas turbine 128 drives the compressor 131 and the generator 132. The exhaust gas from the gas turbine 128 is cooled by the heat recovery device 133 and then released into the atmosphere. In this embodiment, if the material of the turbine blade is improved,
The gas cooling devices 140 and 142 may be omitted.

(Embodiment 7) FIG. 12 shows one embodiment of the present invention, in which a pressurized cylindrical fluidized bed boiler is constructed as a furnace in which a gasification furnace and an oxidation furnace of a topping cycle combined cycle power generation system are integrated. Here is an example. In a cylindrical fluidized bed furnace 201 in a pressurized fluidized bed combined cycle power generation system, a partition wall 203 concentric with a cylindrical outer wall 202 is provided in the fluidized bed, and the partition wall 203 is a cylindrical partition wall 203a and a conical partition wall 2
03b, the voids 204 and 205 are provided in the middle and lower portions of the partition wall 203 to serve as communication ports, and the upper end portion is connected to the ceiling surface of the cylindrical outer wall 202 to form a gas outlet 206.

A gasification furnace 207 is provided inside the partition wall 203.
The outer annular space is used as the oxidation furnace 208.
The hearth of the fluidized bed furnace has a conical shape whose center is higher in the hearth 209 of the gasification furnace 207 and lowers toward the partition wall 203. The hearth 212 of the oxidation furnace 208 is inclined inward, so that the hearth cross section of the entire fluidized bed furnace is W-shaped in any direction. Further, the hearth 209 of the gasification furnace 207 and the hearth 21 of the oxidation furnace 208.
In the lower part of 2, the independent air chambers 214 to 217 are provided.
(Described later) is installed.

The gasification furnace fluidized bed is fluidized by the air dispersion nozzle 210 arranged in the hearth 209 of the gasification furnace 207. At that time, within a concentric circle having a diameter of about 1/2 of that of the gasification furnace 207. From the air dispersion nozzle 210, a gentle fluidization state of about 1 to 2.5 times the minimum fluidization rate and a strong fluidization state of about 4 to 12 times the minimum fluidization rate in the annular portion outside the concentric circle are set. Adjust the amount of air blown out of. As a result, inside the fluidized bed of the gasification furnace, the fluidized medium gently disperses and moves in all directions from the center along the conical hearth surface, and when it reaches the outer peripheral annular portion, the fluidization velocity is high there. Therefore, the movement direction turns upward.
That is, the fluidized medium is blown up along the inside of the partition wall 203, but the cohesive force toward the center gradually increases as the cone-shaped partition wall 203b is inclined, and when it reaches the maximum on the surface of the fluidized bed, the reaction medium is rotated by the reaction force. Explosively explodes in the upward and upward directions.

As a result, a large amount of fluid medium such as unburned char passes through the communication passage 204 provided in the partition wall 203 and enters the oxidation furnace 208. On the other hand, the fluidized medium remaining on the surface of the fluidized bed becomes a cylindrical flow in the vicinity of the center and settles while entraining the surrounding fluidized medium, and when it reaches the vicinity of the center of the conical hearth, it moves again in the horizontal direction all around. A circulating flow is generated that turns into. Due to the effect of this circulation flow, coal and desulfurizing agent, etc., which are injected from the coal feeding nozzle 211 provided near the hearth, are uniformly dispersed in all directions in the fluidized bed of the gasification furnace, and the fuel supply is simple despite the simple coal feeding facility. Uneven distribution is avoided and there is no fear of clinker.

Further, by providing an air dispersion nozzle 213 on the hearth 212 of the oxidation furnace 208 and gently flowing in the oxidation furnace 208, unburned chars and the like passing through the voids 204 and entering the oxidation furnace 208 flow in the oxidation furnace 208. After slowly settling while burning in the bed, the partition wall 20 is formed along the inclined hearth.
3 Passes through the lower connecting flow path 205 and is returned to the gasification furnace fluidized bed. Although it is possible to provide an air introduction pipe for fluidization and a rear air diffuser nozzle also on the back surface of the conical partition wall 203b, it is not necessary to provide them when the angle of the conical partition wall 203b is increased. .

The amount of air blown out from the air dispersion nozzle provided in the hearth 212 of the oxidation furnace 208 is controlled by the outer wall 202 of the cylinder.
The annular portion along the partition wall 203 is adjusted to have a large fluidization rate and the annular portion along the partition wall 203 has a small fluidization rate.
It is also possible to create a circulating flow that settles along and rises along the cylindrical outer wall 202. By this circulation flow,
It is further ensured that the unburned char and the like in the oxidation furnace 208 are burned completely with a sufficient residence time.

Therefore, regarding the air chambers for supplying air to the air dispersion nozzles provided in the respective hearths, the moving bed air chambers for supplying a small amount of air to the center below the hearth 209 of the gasification furnace 207. There are 214, and the surroundings are surrounded by a fluidized bed air chamber 215 for giving a large fluidization rate, and each is connected to an air inlet. Further, an air chamber 216 is provided on the conical inner wall side and an air chamber 217 is provided on the cylindrical outer wall side in the lower part of the hearth 212 of the oxidation furnace 208, so that the amount of fluidized air can be controlled respectively. . A combustion gas outlet 218 is provided on the outer cylinder wall 202 above the oxidation furnace 208.

In this manner, coal is partially gasified while the coal and the desulfurizing agent are supplied to the central gasification furnace 207 and circulated in the fluidized bed, and the produced gas is the gas outlet 206 at the upper part of the gasification furnace. From the outside. On the other hand, the char that has not been gasified enters the oxidation furnace 208 through the void 204 and is completely combusted while circulating in the fluidized bed. Then, the combustion gas is taken out from the combustion gas outlet 218 in the upper portion of the oxidation furnace 208. It is also possible to provide a secondary air nozzle 219 on the oxidation furnace freeboard and perform two-stage combustion.

(Embodiment 8) FIG. 13 is a system diagram showing an embodiment of the present invention including a gas processing system.
The coal 251 and the desulfurizing agent 252 are supplied to the gasification furnace 207,
Partial combustion gasification is performed by the air 253. In addition to air, oxygen 150 or steam 151 may be added as an oxidant.

All the unburned chars and the like generated in the gasification furnace 207 are entrained with the generated gas and cooled to 600 ° C. or less by the gas cooling device 254 installed in the subsequent stage, which causes high temperature corrosion of the gas turbine blades. An alkali metal such as Na or K is solidified or fixed on the surface of the particles, and the particles are collected by the dust collector 255. On the other hand, the unburned char that has passed through the gap 204 and is introduced into the oxidation furnace 208 from the gasification furnace 207 is completely combusted in the oxidation furnace 208, and the combustion exhaust gas thereof exits the combustion gas outlet 218 and is installed in the latter stage. Alkali metal particles such as Na and K which have been cooled to 600 ° C. or less by the gas cooling device 256 and solidified by this cooling are collected by the dust collector 257 and discharged to the outside of the system.

The collected particles from the dust collector 255 are pneumatically supplied to the oxidation furnace 208. A ceramic filter is usually used for the dust collectors 255 and 257, and the produced gas and combustion exhaust gas cleaned by removing Na and K that cause high temperature corrosion are mixed and combusted in the combustor 258 to generate high temperature combustion. The gas drives the gas turbine 261 with high efficiency. Then, the gas turbine 261 is the compressor 26
2. Drive the generator 263. The exhaust gas leaving the gas turbine 261 is cooled by the heat recovery device 264 and then released into the atmosphere. In this embodiment, the gas cooling devices 254 and 256 may be omitted if the material of the turbine blade is improved. It is also possible to arrange the in-layer heat transfer tube 265 in the fluidized bed of the oxidation furnace 208. Further, it is possible to provide the pressure vessel 266 outside the fluidized bed furnace so that the fluidized bed furnace has a non-pressure resistant structure.

According to each of the above-described embodiments, the effects listed below can be obtained. (1) Since the combustion chamber and the heat recovery chamber are functionally separated inside the same combustion container, load control does not depend on the fluidized bed height change method, but overall heat transfer of the in-layer heat transfer tubes by adjusting the air volume in the heat recovery chamber. Since it can be easily done by changing the coefficient,
No complicated operation or equipment (such as a bed material storage container) is required for taking in and out the fluid medium, and it is possible to prevent the occurrence of agglomeration when the fluid medium is taken in and out. Further, since the fluidized bed temperature changes little when the load changes, it is possible to always operate under the optimum temperature condition for suppressing NOx, SOx and the like. Moreover, since the in-bed heat transfer tube is present only in the heat recovery chamber in a gently flowing state, the wear is less than that in the case of being arranged in the fluidized bed in a violently flowing state. (2) Since the fluidized medium causes a diffusive flow that gradually disperses and moves in all directions along the conical hearth surface from the center, the fuel and the desulfurizing agent are uniformly diffused, resulting in uniform combustion and agglomeration. It does not occur, and the coal feeding port only needs to be provided near the center, which has the effect of greatly simplifying the coal feeding facility. (3) Since the fluidized medium on the surface of the fluidized bed becomes a cylindrical flow near the center and sinks while entraining the surrounding fluidized medium, the residence time in the bed of the fuel, the desulfurizing agent and the like is long, and the combustion efficiency is improved. It is extremely effective in improving the desulfurization efficiency. (4) In the case of the conventional rectangular internal circulation fluidized bed boiler, in which the in-layer heat transfer tubes are arranged on two opposite sides of the rectangle, in the case of the present invention, the entire circumference can be utilized, so that more heat is transferred. Since the heat pipe can be arranged, the structure becomes more compact. (5) In the conventional pressurized fluidized bed boiler, a rectangular combustion vessel with a water tube structure is housed in the pressure vessel, but the combustor is protected in case of pressure fluctuation inside the combustor and inside the pressure vessel. Therefore, in the present invention, since the combustor has a cylindrical shape, the combustor has sufficient strength and the reinforcement is simple. Also, since the pressure vessel and combustor are a combination of circles, there is no wasted space,
It has a compact arrangement. (6) By providing a screen having a comb-like shape so as to cover the heat recovery chamber on the freeboard, mixing of solid fuel such as coarse-grained coal into the heat recovery chamber is avoided, and the heat recovery chamber is prevented. In addition to preventing the formation of agglomeration in the heat recovery chamber, it has the effect of baffling the combustion gas generated from the heat recovery chamber and sufficiently mixing and stirring it with the combustion gas in the main combustion chamber. (7) Since the pressurized internal circulation fluidized bed boiler has no heat transfer surface in the main combustion chamber, it can be burned in a reducing atmosphere. As a result, the volatile components of coal are actively released, and hydrocarbons such as CH ₄ and CO or gas phase N in the gas phase reaction.
Chemical species (NHi, HCN, etc.) reduce the generated nitrogen compound, and at the same time bring about the effect of lowering the selectivity of conversion of N chemical species into oxides, which enables low NOx combustion. (8) Several heat transfer chambers are arranged radially inside the fluidized bed, and are used as an evaporation tube block, a steam superheater tube block, and a steam reheat tube block according to the purpose. By dividing and arranging according to function,
By adjusting the heat recovery air amount for each block, it is possible to independently control the heat collection amount of each of the evaporation tube block, the steam superheating tube block, and the steam reheating tube block. (9) The fly ash collected by the cyclone provided in the combustion exhaust gas system is returned to the heat recovery chamber, so that the average particle size and specific weight in the heat recovery chamber are reduced. As a result, the minimum fluidization rate becomes small, and the heat recovery air amount can be small. Therefore, the wear of the in-layer heat transfer tube is significantly reduced, and the influence of the fluctuation of the heat recovery air amount on the combustion is small, which is extremely effective for stable combustion. (10) Classify fly ash, unburned carbon, unreacted desulfurizing agent, etc. recovered from the combustion gas discharged from the combustor, and only fly ash with a particle size in the range of 10 to 60 μm is recovered in the main combustion chamber or heat. By returning to the chamber, NOx reduction with the minimum amount of circulating ash,
It is possible to reduce the wear of the combustion gas system and increase the combustion efficiency. Therefore, it is possible to omit the denitration device, and it is possible to expect an improvement in the desulfurizing agent utilization rate in desulfurization in the furnace, and it is possible to increase the desulfurization rate. (11) The fly ash collected by the dust collector is cooled and then classified at atmospheric pressure to selectively return the unburned carbon content and the unreacted desulfurizing agent to the combustor. In addition to avoiding problems such as slugging associated with the handling of a high-pressure substance under high pressure, only the useful substance is returned by the classification, which reduces the amount of handling. In addition, by recycling to the fuel system, kneading the slurry fuel and supplying it to the combustor, the recycling system to the combustor can be omitted, and the contact between the unreacted desulfurizing agent and the fuel will be good and the desulfurization rate will be improved. Is also effective. (12) In the topping cycle combined cycle power generation system, the pressurized cylindrical internal circulation type fluidized bed boiler of the present application is used for the gasification furnace and / or the oxidation furnace, and all unburned char discharged from the gasification furnace is caused to accompany with the generated gas. , Cooled to 600 ° C or lower, collected by a dust collector installed in the subsequent stage and then introduced into an oxidation furnace for complete combustion, and the combustion exhaust gas is cooled to 600 ° C or lower after exiting the oxidation furnace, The particles containing Na and K are collected and discharged by the dust collector installed in
High temperature generated when the clean combustion gas and the particles containing Na and K that have been collected after leaving the gasification furnace are collected and discharged, and the clean product gas is mixed and burned by the topping combustor. Since the combustion gas is introduced into the gas turbine, alkali metals such as Na and K, which cause high temperature corrosion of the gas turbine blades, are not contained in the combustion gas. It can be handled by the conventional technology. (13) In the cylindrical fluidized bed furnace of the pressurized fluidized bed combined cycle power generation system, a partition wall concentric with the cylindrical outer wall is provided in the fluidized bed, and voids are provided in the middle and lower portions of the partition wall to serve as communication ports. , The upper end is in contact with the ceiling surface of the outer wall of the cylinder to form a gas outlet, and the inside of the partition wall is a gasification furnace,
The annular space outside the partition wall is used as an oxidation furnace so that the gasification furnace and the oxidation furnace can be used as two furnaces.
It can be operated with high efficiency as a compound reactor having two functions.

[0089]

According to the present invention, coal is partially gasified while the coal and the desulfurizing agent are supplied to the gasification furnace and circulated in the fluidized bed, and the produced gas is discharged from the gas outlet at the upper part of the gasification furnace. Outsourced. Due to the effect of the circulating flow of the fluidized medium, the input coal, desulfurizing agent, etc. are uniformly dispersed in all directions in the fluidized bed of the gasifier, and even with a simple coal feeding facility, uneven distribution of fuel can be avoided and clinker may occur. There is no. On the other hand, the char that has not been gasified enters the oxidation furnace and is completely burned while circulating in the fluidized bed. Then, the combustion gas is taken out from the combustion gas outlet at the upper part of the oxidation furnace. The unburned char and the like entering the oxidation furnace are gently settled while burning in the fluidized bed of the oxidation furnace, and then pass through the connecting flow path under the partition wall to be refluxed to the fluidized bed of the gasification furnace. The circulating flow of the fluidized medium makes it possible to ensure that the unburned char and the like have a sufficient residence time and complete combustion in the oxidation furnace. It is also possible to provide a secondary air nozzle on the oxidation furnace free board and perform two-stage combustion.

[Brief description of drawings]

FIG. 1 is a sectional view showing an embodiment of a pressurized internal circulation type fluidized bed boiler of the present invention.

2 (a) is a sectional view taken along line II (a) -II (a) of FIG. 1, and FIG. 2 (b) is a modification of FIG. 2 (a).

FIG. 3 is an explanatory diagram illustrating a control system of an air system according to a load change.

FIG. 4 is a diagram showing the relationship between the overall heat transfer coefficient of the inner layer tube and the superficial velocity.

5 is an explanatory diagram showing a detailed structure of the cylindrical combustor of FIG. 1. FIG.

FIG. 6 is a system diagram showing an example including a combustion exhaust gas treatment system of the present invention.

FIG. 7 is a system diagram showing another example including the combustion exhaust gas treatment system of the present invention.

FIG. 8 is a system diagram showing still another example including the combustion exhaust gas treatment system of the present invention.

FIG. 9 is an overall system diagram of a pressurized internal circulation type fluidized bed boiler of the present invention.

FIG. 10 is a system diagram showing an example in which the internal circulation type fluidized bed boiler of the present invention is incorporated as an oxidizing furnace of a topping cycle combined cycle power generation system.

FIG. 11 is a system diagram showing an example in which the internal circulation type fluidized bed boiler of the present invention is incorporated as a gasification furnace and an oxidation furnace of a topping cycle combined cycle power generation system.

FIG. 12 is a sectional view showing a furnace in which the gasification furnace and the oxidation furnace of the topping cycle combined cycle power generation system are integrated in the internal circulation type fluidized bed boiler of the present invention.

FIG. 13 is a system diagram showing an example including a combustion exhaust gas treatment system of the present invention.

FIG. 14 is a plan view showing a conventional bubbling type pressurized fluidized bed boiler.

FIG. 15 is a plan view showing a conventional bubbling type pressurized fluidized bed boiler.

[Explanation of symbols]

1 pressure vessel 2 Cylindrical combustor 3 Flowing air inlet 4 Combustion gas outlet 5 Heat recovery control air inlet 6 coal feeding entrance 7 Cylindrical support 8 partition walls 9 Main combustion chamber 10 heat recovery room 11 cylindrical outer wall 12 screens Upper header for 13-layer inner pipe Lower header for 14-layer inner pipe 15 Layer heat transfer tube 16 Water inlet 18 Pressure equalizing nozzle 19 Flow air system 20 Main combustion chamber hearth 21 Main combustion chamber air dispersion nozzle 22 Coal supply nozzle 23 Heat recovery room hearth 24 Heat recovery chamber Air dispersion nozzle 27 communication channel 28 Air chamber for fluid combustion 30 Heat recovery control air chamber 31 Free Board 33 Secondary air nozzle 51 cyclone 55 Dust collector 58 gas turbine 100 high pressure gas turbine 101 low pressure gas turbine 120,207 Gasification furnace 126,208 Oxidation furnace 201 fluidized bed furnace

Continued front page    (72) Inventor Takahisa Miyoshi             Chiba Prefecture Sodegaura City Daishuku 94 Ebarasha House 2-201 (72) Inventor Seiichiro Toyoda             1-10-12 Mita, Minato-ku, Tokyo (72) Inventor Akira Shimokura             204-40 Hitorizawa-cho, Isogo-ku, Yokohama-shi, Kanagawa (72) Inventor Tomoyuki Shinano             2-5-3 Kandaiji, Kanagawa-ku, Yokohama-shi, Kanagawa             −512 (72) Inventor Shugo Hosoda             3-2, 3204 Shiomidai, Isogo-ku, Yokohama-shi, Kanagawa             −421 F-term (reference) 3K064 AA02 AA04 AA06 AB03 AD05                       AE11 AE20 AF03 AF08 BA03                       BA05 BA13 BA14 BA24                 4K046 HA05 JA05 JD06 KA03 KA05

Claims (5)

[Claims] 1. A fluidized bed furnace partitioned by a partition wall into a gasification furnace and an oxidation furnace, wherein a circulating flow of a fluidized medium is formed inside at least one of the gasification furnace and the oxidation furnace, The fluidized bed furnace, wherein the partition wall has a communication port for flowing a fluidized medium from the gasification furnace to the oxidation furnace or from the oxidation furnace to the gasification furnace. 2. A fluidized bed furnace partitioned by a partition wall into a gasification furnace and an oxidation furnace, wherein the inside of each of the gasification furnace and the oxidation furnace contains a fluidized state of a fluidized medium. A portion of the fluidizing medium that is in a strong fluidized state is formed, and a portion of the gasification furnace that is in a gentle fluidized state faces the portion of the oxidizing furnace that is in a strongly fluidized state through the partition wall. The fluidized bed furnace is characterized in that the partition wall has a communication port for flowing a fluidized medium from the gasification furnace to the oxidation furnace or from the oxidation furnace to the gasification furnace. 3. The fluidized bed furnace according to claim 1, wherein a hearth of the gasification furnace or the oxidation furnace is inclined toward the partition wall. 4. The gasification furnace has a gas outlet for taking out the generated gas to the outside, and the oxidation furnace has a combustion gas outlet for taking out the combustion gas by the complete combustion of char to the outside. The fluidized bed furnace according to any one of 1 to 3. 5. The fluidized bed furnace according to claim 1, wherein an in-layer heat transfer tube is arranged in a fluidized bed of the oxidation furnace.