WO2014110884A1

WO2014110884A1 - Powdered solid fuel boiler and dry purification process system

Info

Publication number: WO2014110884A1
Application number: PCT/CN2013/075699
Authority: WO
Inventors: 吴道洪; 吴玉林; 王胜美; 陈琳; 鲁光明; 沈大平
Original assignee: 北京神雾环境能源科技集团股份有限公司
Priority date: 2013-01-18
Filing date: 2013-05-16
Publication date: 2014-07-24

Abstract

A powdered solid fuel boiler and a dry purification process system (100). The powdered solid fuel boiler (1) comprises: a hearth (11); a regenerative rotating commutating heater (2); a first fume passage (3), wherein an inlet end of the first fume passage (3) is communicated with a top portion of the hearth (11), and an outlet end of the first fume passage (3) is communicated with the regenerative rotating commutating heater (2), so that fume is delivered into one of at least paired accommodating portions (25) of a heat exchanger main body (21) and exchanges heat with a heat carrier (23) accommodated in the accommodating portion (25); an air passage (4), used for delivering air at least into the other one of the paired accommodating portions (25) of the heat exchanger main body (21), so that a heat carrier (23) accommodated in the accommodating portion (25) exchanges heat with air, and the air after heat exchange is supplied into the hearth (11); and a WCFB fume desulfurization device (5), wherein a part of the fume after desulfurization is re-circulated into a second fume passage (101). By means of the powdered solid fuel boiler and the dry purification process system, the fume exhaust temperature is reduced; the efficiency of the boiler, the desulfurization efficiency, and the fume purification rate are improved; and the influence of corrosion is lowered.

Description

Powdered solid fuel boiler and dry purification process system

Technical field

The invention relates to the field of heat exchange technology, and in particular to a powdery solid fuel boiler and a dry purification process system. Background technique

Rotary air preheater is a flue gas end heat exchange device commonly used in boilers of major power plants. Its performance directly affects boiler thermal efficiency. The traditional rotary air preheater generally uses metal as the heat transfer medium, and can only recover the heat of the flue gas below 500 °C. By preheating the combustion air, the flue gas heat is brought back to the furnace, and the combustion condition is improved, thereby improving the boiler. s efficiency.

However, the conventional rotary air preheaters are mostly metal corrugated plates, but the metal corrugated plate rotary air preheaters have low temperature corrosion during operation, and due to the narrow circulation of gas, it is easy to cause ash and ash. The rotary air preheater can reduce the temperature of the flue gas to about 13CTC. Therefore, after entering the flue gas purification system of any process, the flue gas needs to be sprayed and cooled, and then treated, which will also have corrosion effects on the equipment, and the process is complicated and the equipment is complicated. Large investment, high operating costs, and large requirements for land occupation and water supply. Summary of the invention

The present invention aims to solve at least one of the technical problems existing in the prior art. To this end, an object of the present invention is to provide a powdery solid fuel boiler and a dry purification process system which have a low exhaust gas temperature and eliminate corrosion effects.

A powdery solid fuel boiler and a dry purification process system according to an embodiment of the present invention, comprising: a powdery solid fuel boiler, the powdery solid fuel boiler defining a furnace; a regenerative rotary reversing heater, the heat storage The rotary reversing heater comprises: a heat exchanger body; a driving device, the driving device is configured to drive the heat exchanger body to rotate about a central axis thereof; a partitioning member, the partitioning member is oriented along the central axis Provided in the heat exchanger body, and partitioning the heat exchanger body into at least one pair of receiving portions, the pair of receiving portions being disposed diametrically opposite to the central axis; a heat carrier, the heat carrier Separably housed in the accommodating portion, the heat carrier is formed of a non-metallic solid material; a first flue gas passage, an inlet end of the first flue gas passage is in communication with a top of the furnace, and an outlet end is The regenerative rotary reversing heater is in communication to pass fumes generated in the furnace into at least one of the pair of the receiving portions and to accommodate the heat contained therein a heat exchange passage for introducing at least air into the other of the pair of the receiving portions to allow heat exchange between the heat carrier contained therein and the air; And the WCFB flue gas desulfurization device, the flue gas after the heat exchange of the regenerative rotary reversing heater flows into the WCFB flue gas desulfurization device through the second flue gas passage.

According to the powdered solid fuel boiler and the dry purification process system of the embodiment of the invention, the regenerative rotary reversing heater and the WCFB flue gas desulfurization device are provided, and the regenerative rotary reversing heater can set the temperature of the high temperature flue gas Greatly reduced, thereby improving the efficiency of the boiler system, and in the subsequent flue gas purification treatment WCFB flue gas desulfurization equipment The water spray device can be omitted, which not only optimizes the process, saves cost and reduces the corrosion effect, but also effectively solves the problem of ash adherence after water spray.

Further, the powdery solid fuel boiler and the dry purification process system according to the present invention may have the following additional technical features:

According to an embodiment of the present invention, the pulverized coal is formed of at least one of anthracite coal and lean coal.

Optionally, a screen superheater, a wall superheater and a superheater are arranged from the inlet end of the first flue gas passage toward the outlet end of the first flue gas passage. Thus, by providing a superheater, the cycle thermal efficiency of the entire steam power unit can be effectively improved.

Further, a economizer is disposed in the first flue gas passage adjacent to the outlet end of the first flue gas passage. Thus, by providing the economizer, the heat of the flue gas can be effectively absorbed, the exhaust gas temperature can be lowered, and the smoke loss can be reduced, thereby saving fuel.

According to an embodiment of the invention, the velocity of the flue gas entering the regenerative rotary reversing heater from the first flue gas passage is adjustable. Thereby, the temperature of the air to be preheated is effectively increased.

Optionally, the heat carrier is SiC or ceramic and has a small spherical, sheet or porous structure. As a result, the regenerative rotary reversing heater is resistant to high temperatures, corrosion and wear.

Optionally, the temperature of the flue gas after heat exchange by the regenerative rotary commutation heater is 65-75 °C. While the boiler exhaust gas temperature has dropped to 65-75 °C, there is a major change in the tail desulfurization process. That is to use the WCFB dry desulfurization process, so that the tail does not need to spray water to cool down, to avoid corrosion problems, the flue gas is reduced to 65~75 °C, which is the inlet smoke temperature of the WCFB dry desulfurization process, and the original exhaust gas above 12CTC The temperature must be sprayed to cool down to 65~75 °C, which saves a water spray process and saves energy, avoiding the unfavorable problem of ash adherence after water spray. Thereby, part of the latent heat of vaporization in the flue gas can be recovered, thereby improving the thermal efficiency of the boiler, and at the same time, the flue gas entering the subsequent WCFB flue gas desulfurization equipment does not need to be sprayed and cooled.

According to an embodiment of the invention, the air is oxygen-enriched air, and the air is heated to 300-650 ° C after heat exchange by the regenerative rotary commutation heater. As a result, the air lift temperature is higher.

According to an embodiment of the present invention, the regenerative rotary reversing heater further includes: a condensed liquid removing device disposed under the heat exchanger body to remove heat exchange Condensed liquid produced during the process.

According to an embodiment of the present invention, the WCFB flue gas desulfurization apparatus includes: an absorption tower, the second flue gas passage is in communication with a bottom of the absorption tower; a lime removal silo, the decalcification silo is disposed in the absorption tower The upper part is used for spraying slaked lime into the absorption tower; the dust remover is connected to the absorption tower for dedusting the flue gas after the slaked lime absorption reaction; and the chimney, after the dust removal The flue gas after the dust removal is connected to the bacon through a third flue gas passage, and the third flue gas passage is provided with an induced draft fan to introduce the flue gas to the chimney. Thus, by providing an absorption tower and a slaked lime tank, the flue gas can be absorbed and reacted with the slaked lime sprayed from the slaked lime tank in the absorption tower. By providing a dust remover, the flue gas after desulfurization can enter the dust collector for purification, and finally through the chimney. Discharge into the atmosphere.

Further, the WCFB flue gas desulfurization apparatus further includes: a recirculation pipe, and the recirculation pipe is inclined And used to recycle slaked lime at the bottom of the precipitator into the absorption tower. Thereby, the utilization efficiency of slaked lime is effectively improved by a plurality of cycles, thereby improving the desulfurization efficiency.

Further, the method further includes: a fourth flue gas passage that recirculates a portion of the flue gas in the third flue gas passage into the second flue gas passage. Thereby, the purification rate of the flue gas is further improved.

The additional aspects and advantages of the invention will be set forth in part in the description which follows. DRAWINGS

The above and/or additional aspects and advantages of the present invention will become apparent and readily understood from

1 is a schematic view of a powdery solid fuel boiler and a dry purification process system according to an embodiment of the present invention; FIG. 2 is a regenerative rotary reversing heater in a powdery solid fuel boiler according to an embodiment of the present invention. Top view. detailed description

The embodiments of the present invention are described in detail below, and the examples of the embodiments are illustrated in the drawings, wherein the same or similar reference numerals are used to refer to the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the drawings are intended to be illustrative only and not to limit the invention.

In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "back", "left", "right", "vertical", "horizontal", The orientation or positional relationship of the "top", "bottom", "inside", "outside" and the like is based on the orientation or positional relationship shown in the drawings, and is merely for the convenience of describing the present invention and simplifying the description, rather than indicating or implying The device or component referred to must have a particular orientation, configuration and operation in a particular orientation, and thus is not to be construed as limiting the invention. Moreover, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, "multiple" means two or more unless otherwise stated.

In the description of the present invention, it should be noted that the terms "installation", "connected", and "connected" should be understood broadly, and may be fixed or detachable, for example, unless otherwise explicitly defined and defined. Connected, or connected integrally; can be mechanical or electrical; can be directly connected, or indirectly connected through an intermediate medium, can be the internal communication of the two components. The specific meaning of the above terms in the present invention can be understood in a specific case by those skilled in the art.

A powdered solid fuel boiler and dry purification process system 100 in accordance with an embodiment of the present invention will now be described with reference to FIG.

As shown in FIG. 1 , a powdery solid fuel boiler and a dry purification process system 100 according to an embodiment of the present invention include: a powdery solid fuel boiler 1, a regenerative rotary reversing heater 2, a first flue gas passage 3, Air passage 4 and WCFB flue gas desulfurization equipment 5. The regenerative rotary reversing heater 2 is used for exchanging heat between the high temperature flue gas and the air to be preheated, thereby raising the temperature of the air to be preheated to a certain value. The regenerative rotary reversing heater 2 comprises: a heat exchanger body 21, a driving device, a partition 22 and a heat carrier 23, as shown in Figs. Therein, the drive means is used to drive the heat exchanger body 21 to rotate about its central axis 24. The partition 22 is disposed in the heat exchanger body 21 in the direction of the central axis 24, and divides the heat exchanger body 21 into at least one pair of accommodating portions 25, each pair of accommodating portions 25 being disposed diametrically opposite to the central axis. The heat carriers 23 are respectively accommodated in the accommodating portion 25, and the heat carrier 23 is formed of a non-metallic solid material.

In one of the examples of the present invention, the heat exchanger body 21 may be formed as a hollow cylinder, and the partition 22 may be substantially plate-shaped, and the partition extends in the direction of the center line axis of the heat exchanger body 21, thereby The heat exchanger body 21 is partitioned into a pair of receiving portions, the heat carriers are respectively disposed in the two receiving portions, and the heat carrier can be made of a non-metallic solid material, and the flue gas and the air to be preheated are respectively introduced into the two receiving portions, and then passed through The driving device drives the heat exchanger main body 21 to rotate, the flue gas exchanges heat with the heat carrier in the accommodating portion in which it is located, heats the air to be preheated, and the heat carrier in the accommodating portion therewith, thereby causing the air to be preheated The temperature rises.

Of course, the invention is not limited thereto, and in other examples of the invention, the partition 22 may also divide the heat exchanger body 21 into two pairs, three pairs or even pairs of receiving portions.

In the existing gas heat exchange system, the outlet temperature of the flue gas after passing through the gas heat exchanger cannot be lowered below 130 ° C, because this causes the sulfuric acid to precipitate, resulting in the metal in the gas heat exchanger. Severe corrosion of the manufactured parts. However, in the above-described regenerative rotary commutation heater 2 of the present invention (for, for example, high-temperature flue gas containing sulfur), since the heat carrier is formed of a non-metallic solid material such as SiC or ceramic, there is no need to worry about sulfur. At 130 ° C, there is a problem of corrosion caused by the dew point, and the outlet temperature of the high-temperature flue gas can be lowered to a temperature below the dew point of sulfur to maximize heat exchange. According to an embodiment of the present invention, the high temperature The outlet temperature of the flue gas leaving the gas heat exchanger is less than 130 ° C. Further, the outlet temperature of the high temperature flue gas leaving the gas heat exchanger is less than 70 ° C. This temperature is almost impossible to achieve in a conventional gas heat exchange system. In addition, under the temperature at which the outlet temperature is lowered to the dew point, the water vapor condenses out as liquid water, releasing a large amount of latent heat (the amount of heat absorbed by the water vapor from 100 ° C to 10 CTC is equivalent to the water rising from 0 ° C. Up to 3 times the amount of heat absorbed at 100 ° C). Since the heat carrier is formed of a non-metallic solid material, after the sulfur deposition is performed to some extent, the heat carrier accommodated in the accommodating portion can be continuously used, thereby reducing the components existing in the conventional gas heat exchange system. The problem of increased costs caused by replacement. In addition, according to the inventors' calculation using the accepted calculation method in the field, according to the calculation by the inventor, by carrying the regenerative rotary reversing heater, the cold air is heated to the hot air to facilitate the combustion, and the exhaust gas temperature is lowered to 65~75°C, effectively utilizing the waste heat of the fuel and improving the efficiency of the boiler

More than 3 percentage points. . In addition, the scope of application of coal is expanded, that is, the grade of coal used can be lowered, and the production cost is further reduced.

Among them, the powdery solid fuel boiler 1 is defined with a furnace 11. The inlet end of the first flue gas passage 3 communicates with the top of the furnace 11 and the outlet end communicates with the regenerative rotary reversing heater 2 to pass the flue gas generated in the furnace 11 into at least a pair of heat storage. Rotating one of the accommodating portions of the reversing heater 2 and exchanging heat with the heat carrier accommodated in the accommodating portion. The air passage 4 is for introducing at least air into the other of the pair of receiving portions, such that The heat carrier accommodated in the accommodating portion exchanges heat with the air, and the air after the heat exchange is supplied to the inside of the furnace 11. The flue gas after heat exchange by the regenerative rotary reversing heater 2 flows into the WCFB flue gas desulfurization device 5 through the second flue gas passage 101.

In the following description, the heat exchanger body 21 is rotated counterclockwise, and the flue gas is introduced into the heat exchanger body 21 along the right side of the central axis, and the preheated air is introduced into the heat exchanger along the left side of the central axis. The main body 21 will be described as an example.

As shown in FIG. 1, the powdery solid fuel boiler 1 defines a furnace 11 for accommodating pulverized coal, and one end of the flue gas passage 3 communicates with the furnace 11 and the other end thereof communicates with the regenerative rotary reversing heater 2. The flue gas generated in the furnace 11 is introduced into the first accommodating portion 211 of the regenerative rotary reversing heater 2 (for example, the right side of the regenerative rotary reversing heater 2 shown in FIG. 1), The second accommodating portion 212 of the regenerative rotary reversing heater 2 (for example, the left side of the regenerative rotary reversing heater 2 shown in FIG. 1) is used to pass the air to be preheated, in the heat exchange When the main body 21 is in an unrotated state, the flue gas exchanges heat with the heat carrier in the first accommodating portion 211 to raise the temperature of the heat carrier, and after the heat carrier absorbs heat, the heat exchanger main body 21 rotates counterclockwise, the first accommodating The portion 211 is rotated to the left side of the central axis, the second receiving portion 212 is rotated to the right side of the central axis, and the heat carrier rotated into the first receiving portion 211 on the left side exchanges heat with the air to be heated to bring the heated air temperature Lit, at the same time, the smoke is rotating The heat carrier in the second accommodating portion 212 on the right side is heated.

The heat exchanger body 21 continues to rotate counterclockwise, at which time the first receiving portion 211 is rotated back to the right side of the central axis, the second receiving portion 212 is rotated back to the left side of the central axis, and rotated back to the second accommodation on the left side. The heat carrier in the portion 212 exchanges heat with the air to be heated, and the flue gas heats the heat carrier in the first accommodating portion 211 which is rotated back to the right side, and the cycle is repeated to complete the heating of the preheated air.

In one of the examples of the present invention, the preheated air is heated to a certain temperature and can be obtained from a powdery solid fuel boiler.

The bottom of 1 is supplied into the furnace 11 to perform high-temperature oxidation combustion with the pulverized coal in the furnace π.

Alternatively, the pulverized coal is formed of at least one of anthracite and lean coal.

The flue gas after heat exchange with the preheated air enters the WCFB flue gas desulfurization apparatus 5 through the second flue gas passage 101 for purification.

According to the powdered solid fuel boiler and the dry purification process system 100 of the embodiment of the present invention, the regenerative rotary reversing heater 2 and the WCFB flue gas desulfurization device 5 are provided, and the regenerative rotary reversing heater 2 can set the high temperature. The temperature of the flue gas is greatly reduced, thereby improving the efficiency of the boiler system, and at the same time, the sprinkler device can be omitted in the subsequent flue gas purification treatment WCFB flue gas desulfurization device 5, which not only optimizes the process, saves cost and reduces corrosion effects. At the same time, it also effectively solves the problem of ash adherence after water spray.

Optionally, a screen superheater 6, a wall superheater 7 and a superheater are disposed in order from the inlet end of the first flue gas passage 3 toward the outlet end of the first flue gas passage 3. For example, in the example of FIG. 1, the screen superheater 6 and the wall superheater 7 are disposed adjacent to the inlet end of the first flue gas passage 3, and are spaced apart from each other in the left-right direction, and the superheater is adjacent to the first flue gas passage 3. The exit side is set. Thus, by providing a superheater, the cycle thermal efficiency of the entire steam power unit can be effectively improved.

Further, an economizer 9 is disposed in the first flue gas passage 3 near the outlet end of the first flue gas passage 3. For example, in the example of FIG. 1, the economizer 9 is disposed below the superheater and is spaced apart from the superheater in the up and down direction. Set the distance. Thus, by providing the economizer 9, the heat of the flue gas can be effectively absorbed, the exhaust gas temperature can be lowered, and the exhaust gas loss can be reduced, thereby saving fuel.

In one embodiment of the invention, the flue gas velocity entering the regenerative rotary commutation heater 2 from the first flue gas passage 3 is adjustable. Thereby, the temperature of the air to be preheated is effectively increased.

Alternatively, the heat carrier is SiC or ceramic and has a small spherical, sheet-like or porous structure. Thus, the regenerative rotary reversing heater 2 is resistant to high temperatures, corrosion, and wear.

Alternatively, the temperature of the flue gas after heat exchange by the regenerative rotary commutation heater 2 is 65-75 °C. In the boiler exhaust temperature, it is necessary to spray water to cool down to 65~75 °C, which saves a water spray process and saves energy, avoiding the unfavorable problem of ash adherence after water spray. Thereby, part of the latent heat of vaporization in the flue gas can be recovered, thereby improving the thermal efficiency of the boiler, and at the same time, the flue gas entering the subsequent WCFB flue gas desulfurization device 5 does not need to be sprayed and cooled.

Alternatively, the air is oxygen-enriched air, and the air is heated to 300-650 ° C after heat exchange through the regenerative rotary commutation heater 2 . As a result, the air lift temperature is higher.

In an embodiment of the present invention, the regenerative rotary reversing heater 2 further includes: a condensed liquid removing device disposed under the heat exchanger body to remove the heat generating process Condensing liquid.

In one embodiment of the invention, the WCFB flue gas desulfurization apparatus 5 comprises: an absorption tower 51, a lime removal compartment 52, a dust collector 53 and a chimney 55. The second flue gas passage 101 communicates with the bottom of the absorption tower 51. A slaked lime tank 52 is disposed at an upper portion of the absorption tower 51 for injecting slaked lime into the absorption tower 51. The dust remover 53 is connected to the absorption tower 51 for dust removal of the flue gas after the slaked lime absorption reaction. The flue gas after the dust removal by the dust remover 53 is communicated to the bacon 55 through the third flue gas passage 102, and the third flue gas passage 102 is provided with an induced draft fan 1021 to guide the flue gas to the chimney 55. Thus, by providing the absorption tower 51 and the slaked lime tank 52, the flue gas can be absorbed and reacted with the slaked lime sprayed from the slaked lime silo 52 in the absorption tower 51. By providing the dust remover 53, the flue gas after desulfurization can enter the dust remover 53. Purification is carried out and finally discharged into the atmosphere via bacon 55.

In the example of FIG. 1, one end of the second flue gas passage 101 communicates with the regenerative rotary reversing heater 2, and the other end thereof communicates with the bottom of the absorption tower 51, thereby regeneratively rotating the reversing heater 2 The temperature-reduced flue gas is introduced into the absorption tower 51, and the flue gas rises to the upper portion of the absorption tower 51 to absorb the slaked lime sprayed from the slaked lime silo 52, and then enters the dust remover 53 for dust removal, and the desulfurized purified flue gas leaves the dust remover 53. The third flue gas passage 102 is entered, and the third flue gas passage 102 is provided with an induced draft fan. Finally, the flue gas is discharged into the atmosphere by the bacon 55 under the action of the induced draft fan 1021.

Further, the WCFB flue gas desulfurization apparatus 5 further includes: a recirculation pipe 54, a recirculation pipe 54 disposed obliquely and for recycling the slaked lime at the bottom of the precipitator 53 into the absorption tower 51. As shown in Fig. 1, one end of the recirculation pipe 54 communicates with the bottom of the precipitator 53, and the other end thereof communicates with the absorption tower 51, and the slaked granules returned from the recirculation pipe 54 to the absorption tower 51 are again entered into the absorption tower 51. Low temperature flue gas reaction. Thereby, the utilization efficiency of slaked lime is effectively improved by a plurality of cycles, thereby improving the desulfurization efficiency.

In one of the examples of the present invention, at least one fluidizing fan 541 may be provided at the bottom of the recirculation pipe 54 to function as a smooth return. Two fluidizing fans 541 are shown in the example of Fig. 1, and two fluidizing fans 541 are spaced apart in the left-right direction. It can be understood that the number of fluidizing fans 541 can be set according to actual requirements to better meet actual requirements. Further, the method further includes: a fourth flue gas passage 103, and the fourth flue gas passage 103 recirculates a part of the flue gas in the third flue gas passage 102 into the second flue gas passage 101. For example, in the example of FIG. 1, one end of the fourth flue gas passage 103 communicates with the third flue gas passage 102 and one end of the fourth flue gas passage 103 communicates with the third flue gas passage 102 after the induced draft fan, and the other end thereof The second flue gas passage 101 communicates. Thereby, the purification rate of the flue gas is further improved.

In summary, the powdery solid fuel boiler and the dry purification process system 100 according to the present invention are equipped with a regenerative rotary reversing heater. According to the calculation by the inventor, by carrying a regenerative rotary reversing heater, the cold air is heated to the hot air to facilitate combustion, and the exhaust gas temperature is lowered to 65 to 75 ° C, and the waste heat of the fuel is effectively utilized, and the boiler is used. The efficiency is increased by more than 3 percentage points. In addition, due to the fact that the boiler exhaust gas temperature is lowered to 65-75 °C, the tail desulfurization process needs to undergo major changes. That is to use the WCFB dry desulfurization process, so that the tail does not need to spray water to cool down, avoid corrosion problems, and save a water spray process, which can save energy and avoid the unfavorable problem of gray plastering after water spray.

In the description of the present specification, the description of the terms "one embodiment", "some embodiments", "illustrative embodiment", "example", "specific example", or "some examples", etc. Particular features, structures, materials or features described in the examples or examples are included in at least one embodiment or example of the invention. In the present specification, the schematic representation of the above terms does not necessarily mean the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in a suitable manner in any one or more embodiments or examples.

While the embodiments of the present invention have been shown and described, the embodiments of the invention may The scope of the invention is defined by the claims and their equivalents.

Claims

Claim

A powdery solid fuel boiler and a dry purification process system, characterized in that it comprises:

a powdery solid fuel boiler, the powdered solid fuel boiler is defined with a furnace;

a regenerative rotary reversing heater, the regenerative rotary reversing heater comprising:

Heat exchanger body;

a driving device, the driving device is configured to drive the heat exchanger body to rotate about a central axis thereof; a partitioning member, the partitioning member is disposed in the heat exchanger body along a direction of the central axis, and The heat exchanger body is partitioned into at least one pair of receiving portions, the pair of receiving portions being disposed diametrically opposite to the central axis;

a heat carrier, the heat carrier being respectively accommodated in the accommodating portion, the heat carrier being formed of a non-metallic solid material;

a first flue gas passage, an inlet end of the first flue gas passage is in communication with a top of the furnace, and an outlet end is connected to the regenerative rotary reversing heater to generate flue gas generated in the furnace Passing into at least one of the pair of the receiving portions and exchanging heat with the heat carrier housed therein;

An air passage for introducing at least air into the other of the pair of the receiving portions to allow the heat carrier accommodated therein to exchange heat with the air;

The WCFB flue gas desulfurization device, the flue gas after heat exchange by the regenerative rotary reversing heater flows into the WCFB flue gas desulfurization device through the second flue gas passage.

2. The powdery solid fuel boiler and dry purification process system according to claim 1, wherein the pulverized coal is formed of at least one of anthracite and lean coal.

3. The powdered solid fuel boiler and dry purification process system according to claim 1, wherein the outlet from the first flue gas passage faces the outlet of the first flue gas passage The screen is provided with a screen superheater, a wall superheater and a superheater in sequence.

A powdery solid fuel boiler apparatus according to claim 3, wherein an economizer is disposed in said first flue gas passage adjacent said outlet end of said first flue gas passage.

The powdery solid fuel boiler and the dry purification process system according to claim 1, wherein the flue gas velocity entering the regenerative rotary reversing heater from the first flue gas passage is Adjustment.

The powdery solid fuel boiler and dry purification process system according to claim 1, wherein the heat carrier is SiC or ceramic.

7. The powdery solid fuel boiler and dry purification process system according to claim 1, wherein the temperature of the flue gas after heat exchange by the regenerative rotary commutation heater is 65-75 ° C .

8. The powdery solid fuel boiler and dry purification process system according to claim 1, wherein the air is oxygen-enriched air, and the air passes through the regenerative rotary commutation heater for heat exchange. It is then heated to 300-650 °C. The pulverized solid fuel boiler and the dry cleaning process system according to claim 1, wherein the regenerative rotary reversing heater further comprises:

A condensed liquid removal device is disposed below the heat exchanger body to remove condensed liquid generated during heat exchange.

The powdery solid fuel boiler and the dry purification process system according to claim 1, wherein the WCFB flue gas desulfurization device comprises:

An absorption tower, wherein the second flue gas passage is in communication with a bottom of the absorption tower;

a slaked lime silo, wherein the slaked lime silo is disposed at an upper portion of the absorption tower for injecting slaked lime into the absorption tower; and the dust remover is connected to the absorption tower for use in absorbing the slaked lime Flue gas for dust removal;

The chimney, the flue gas after being dusted by the dust collector is connected to the bacon through a third flue gas passage, and the third flue gas passage is provided with an induced draft fan to introduce the flue gas to the chimney.

The powdery solid fuel boiler and the dry purification process system according to claim 10, wherein the WCFB flue gas desulfurization apparatus further comprises:

A recirculation pipe, the recirculation pipe being disposed obliquely and for recycling slaked lime at the bottom of the precipitator into the absorption tower.

The powdery solid fuel boiler and the dry purification process system according to claim 11, further comprising:

a fourth flue gas passage, the fourth flue gas passage recirculating a portion of the flue gas in the third flue gas passage into the second flue gas passage.