KR101594799B1 - Ash Separation Apparatus and Solid Fuel Chemical Looping Combustor Using This - Google Patents

Abstract

The present invention relates to an ash separation apparatus spraying solid particles and ashes upward in a fluidized bed at the same time to separate the ashes and the solid particles having different specific gravities and particle sizes, thereby selecting only fallen solid particles and discharging dispersed ashes; and to a solid fuel medium circulating combustor enabling circulation without loss of oxygen donating particles by using the same. The ash separation apparatus comprises a vertically long casing having a space inside; an inlet port where ashes and solid particles are mixed and supplied; a gas dispersion plate formed on the lower part of the casing; a fluidized gas supply pipe supplying a fluidized gas to a lower space of the gas dispersion plate; a solid spray pipe penetrating the gas dispersion plate, and absorbing the ashes and the solid particles stacked on the upper side of the gas dispersion plate through a solid absorption hole formed on the outer circumference, and spraying the ashes and the solid particles toward the inside of the casing by an injection gas; a solid particle receiver installed around the solid spray pipe, and storing fallen solid particles; a solid particle outlet port connected to the solid particle receiver, and discharging only the solid particles to the outside; and an ash discharge pipe installed on the upper part of the casing, and protruding toward the inside of the casing to discharge dispersing ashes with a gas.

Description

[0001] The present invention relates to an ash separator and a solid fuel medium circulating combustor using the same,

The present invention relates to a material separator and a solid fuel medium circulating combustor using the same. More particularly, the present invention relates to a solid fuel separator for separating solid materials (oxygen donor particles, unreacted solid fuel) The present invention also relates to a solid material fuel circulating combustor capable of circulating operation without loss of oxygen donating particles by using the material separator for injecting particles and a fly ash simultaneously and sorting only solid particles falling and discharging scattered fly ash.

The CLC (Chemical-Looping Combustion) technology can separate CO ₂ from its original source without the need for a separate separation facility. It is a next-generation, low-emission, high-efficiency power generation system with low generation of thermal NOx and high power generation efficiency. Technology. Recently expensive gaseous fuel instead of being able to directly combust the solid fuel, the process within a separate grading equipment solid that can be fundamentally divided into the CO ₂ without fuel looping combustion (SF-CLC, Solid Fuel Chemical Looping Combustion) technology Are being studied.

The basic concept of the solid fuel medium circulation combustion technique is shown in FIG. In the oxidation reactor, oxygen-donating particles (M) in the form of metal react with oxygen in the air to form metal oxides (MO) (hereinafter referred to as oxygen-binding particles) as shown in the following reaction formula 1, . In the reduction reactor, steam or CO ₂ is supplied to the gas for fluidization of the solid fuel, and the gasification of the solid fuel is caused by the fluidized gas.

[Reaction Scheme 1]

M + 0.5 O _{2 -} > MO

In this case, as the solid fuel, coal, coke, char, biomass, etc. can be used. In the case of coal, for example, in a reduction reactor, carbon reacts with steam to produce CO and H ₂ Or carbon reacts with CO ₂ to form CO as shown in Scheme 3. Then, the generated CO and H ₂ react with the metal oxide transferred from the oxidation reactor to form CO ₂ or H ₂ O, as shown in equations (4) and (5), and the oxygen donor particles reduced to the metal form are recycled to the oxidation reactor .

[Reaction Scheme 2]

C + H ₂ O - > CO + H ₂

[Reaction Scheme 3]

C + CO _{2 -} > 2CO

[Reaction Scheme 4]

CO + MO - CO ₂ + M

[Reaction Scheme 5]

H ₂ + MO - H ₂ O + M

As a result, CO ₂ and H ₂ O are the only gases discharged from the reduction reactor of the medium circulation combustor. Therefore, when H ₂ O is condensed and removed, CO ₂ can be originally separated at a high concentration without a separate separation facility.

In the reduction reactor of the solid fuel medium circulation combustion, the gasification reaction by the steam and the combustion reaction by the oxygen donor particles occur simultaneously. The oxidation reaction and the reduction reaction are carried out at a high temperature of 600 to 1000 ° C. At this time, when the coal, biomass, waste and so on continuously supplied to the solid fuel in the reduction reactor and reduced by reaction with oxygen carrier particles, the volatile, combustible components, such as fixed carbon will react with oxygen contained in the oxygen carrier particles CO _2, CO, and H ₂ O, and is discharged to the outside of the reactor. However, the ash contained in the solid fuel is accumulated in the reduction reactor.

Therefore, it is difficult to separate the oxygen donor particles and the ash when the solid fuel is used as the fuel, so that the oxygen donor particles and the ash that stay in the reduction reactor must be removed periodically or continuously.

Therefore, in the case of the solid fuel medium circulation combustor, the oxygen donor particles containing the expensive metal components such as Ni, Co, Fe, Cu, Mn, and Ce and their complexes are used instead of the oxygen donor particles (iron ore, ilmenite, oxide scale, bauxite and combinations thereof).

However, when disposing of low-cost oxygen donor particles together with a material, cost of disposal of the waste is required, and even low-cost oxygen donor particles must be constantly made up. Therefore, there is a problem.

Korean Patent Publication No. 10-2014-0087853

It is an object of the present invention, which has been devised to solve the problems described above, to provide a slurry separator for separating a solid material from a material having a specific gravity or particle size, and a solid fuel medium circulating combustor capable of circulating operation without loss of oxygen donor particles .

According to an aspect of the present invention, there is provided a portable terminal comprising: a casing having a space in a longitudinal direction and having a space therein; An inlet port through which the mixture of the material and the solid particles is supplied; A gas distribution plate formed at a lower portion of the casing; A fluidized gas supply pipe for supplying fluidized gas to a lower space of the gas distribution plate; A solid distributor pipe installed through the gas distributor plate and sucking the solid material and the material loaded on the gas distributor plate through a solid suction hole formed on the outer periphery and injecting the solid material into the casing by the injection gas; A solid particle receiver installed around the solid spray tube to receive falling solid particles; A solid particle outlet port connected to the solid particle receiver to discharge only solid particles to the outside; And a material discharge pipe installed on the upper portion of the casing and projecting to the inside of the casing to discharge the scattered material together with the base.

And the height of the solid spraying tube projecting from the gas distribution plate can be changed.

Further, the solid spraying tube is attached to and detached from the solid spraying tube fixing part formed at the lower part of the casing.

The length of the solid spray tube is adjusted by screwing the solid spray tube to the solid spray tube, and the solid tube is connected to the solid spray tube by extrapolating the solid spray tube. do.

In addition, the above-mentioned material discharge pipe can change the height from the gas distribution plate.

Further, the above-mentioned material discharge pipe is attached to and detached from the material discharge pipe fixing portion formed on the upper portion of the casing.

In addition, the length of the ash discharge pipe is adjusted by screwing to the discharge pipe fixing part formed on the upper part of the casing, and the pipe extension pipe is detached from the discharge pipe fixing part while extruding the pipe discharge pipe.

Still another invention is a solid fuel medium circulation combustor having the above-described material separator, comprising: an oxidation reactor in which oxygen donor particles are fluidized to capture oxygen; An oxidized cyclone separating a mixture of gas and oxygen-bonded particles discharged from the oxidation reactor; A reducing reactor in which a gasification reaction of the solid fuel by the reducing fluidizing gas and a combustion reaction by the oxygen binding particles separated and supplied from the oxidized cyclone occur and discharges the material and the reduced oxygen donor particles; A reducing cyclone for separating a mixture of gas and oxygen donor particles discharged from the reduction reactor and returning the mixture to the reduction reactor; And a sorbent separator for separating the sorbent donor particles supplied from the reduction reactor and the material to transfer only oxygen donor particles to the oxidation reactor.

And a material cyclone for separating a mixture of the slurry discharged from the slurry separator and the gas is connected to the slurry separator.

According to the present invention, it is possible to separate the required solid particles from the materials, and thus, in the case of the solid fuel medium circulation combustor using the same, continuous circulation combustion is possible without loss of oxygen donor particles. Therefore, expensive oxygen donor particles (Ni, Co, Fe, Cu, Mn, Ce, etc.) as well as low-cost oxygen donor particles (iron ore, ilmenite, oxide scale, bauxite and composite thereof) can be used.

As a result, in the prior art, the cost of disposing of the oxygen donor particles together with the material is reduced, and the maintenance cost due to continuous replenishment of the oxygen donor particles can be drastically reduced. The difficulty can be reduced.

1 is a conceptual diagram illustrating a solid fuel medium circulation combustion technique.
2 is a schematic configuration of a solid fuel medium circulation combustor according to the prior art.
3 is a schematic configuration of a solid fuel medium circulation combustor to which a slurry separator according to the present invention is applied.
Figure 4 is a schematic cross-sectional view of the slurry separator of Figure 3;
5 is an enlarged sectional view of the upper part of the casing of the ash separator in Fig.
Fig. 6 and Fig. 7 are graphs of the results of the test examples.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described with reference to the accompanying drawings. In the drawings, the same reference numerals are used to designate the same or similar components, and the same reference numerals will be used to designate the same or similar components. Detailed descriptions of known functions and configurations are omitted.

The basic process configuration of the solid fuel medium circulation combustor 100 according to the prior art is as shown in FIG. The solid fuel medium circulation combustor 100 includes an oxidation reactor 102 for capturing oxygen while oxygen donor particles are fluidized and an oxidation cyclone 102 for separating a mixture of gas and oxygen binding particles discharged from the oxidation reactor 102 The oxidation reaction of the solid fuel with the reducing fluidizing gas and the combustion reaction with the oxygen binding particles separated and supplied from the oxidizing cyclone 108 are performed and the reduced oxygen donating particles are introduced into the oxidation reactor 102, And a reducing cyclone 124 separating a mixture of gas and oxygen donor particles discharged from the reduction reactor 102 and returning the mixture to the reduction reactor I 120.

Since the oxidation reactor 102 plays a role of causing oxygen to react with oxygen donor particles and oxygen, it also has a role of ejecting particles to the upper part and transferring the particles to the reduction reactor 120. Therefore, a fast fluidized bed type is generally used. The oxygen supplied to the oxidation reactor 102 is supplied by an oxidizing fluidized gas supplied through the oxidized fluidized gas supply pipe 104 provided in the lower portion of the oxidation reactor 102, .

The oxidized cyclone 108 connected to the oxidizing reactor discharge pipe 106 of the oxidation reactor 102 includes an oxidized cyclone solid discharge pipe 110 for discharging the oxygen binding particles and an oxidized cyclone gas And has a discharge pipe 112.

A loop chamber 114 may be interposed between the oxidation cyclone 108 and the reduction reactor 120. The loop chamber 114 prevents the oxidizing fluidized gas and the reducing fluidized gas injected into the oxidation reactor 102 and the reduction reactor 120 from being mixed with each other and the oxidation reactor 102 and the reduction reactor 120 (Oxygen-donating particles or oxygen-binding particles) which may be caused by the differential pressure between the anode and the cathode.

In the loop chamber 114, a loop chamber fluidizing gas supply pipe 116 to which a loop chamber fluidizing gas is supplied is installed for moving the oxygen binding particles. As the loop chamber fluidizing gas, carbon dioxide or steam may be used. The loop chamber 114 supplies the oxygen binding particles inside the reduction reactor 120 through the loop chamber discharge pipe 118.

The reduction reactor 120 is a fluidized bed reactor and is provided with a reducing fluidized gas supply pipe 132 through which a reducing fluidizing gas is supplied at a lower portion and a reduction cryocatalyst separating gas (CO ₂ or H ₂ O) Clone 124 is connected via reduction gas discharge pipe 122. As the reducing fluidizing gas, carbon dioxide or steam may be used. Solid fuel is supplied to the inside of the reduction reactor 120 through a solid fuel supply line 119, and coal, coke, char, biomass, etc. may be used as the solid fuel.

CO ₂ or H ₂ O is discharged through the reduced cyclone gas discharge pipe 126 of the reduction cyclone 124 and the oxygen donor particles separated through the reduced cyclone solid discharge pipe 128 are introduced into the reduction reactor 120, .

The oxygen donor particles reduced in the reduction reactor 120 are introduced into the oxidation reactor 102 through the reduction reactor discharge pipe 130.

Generally, the solid fuel as a fuel in the medium circulation combustor 100 using solid fuel is supplied as fine particles in the form of fine particles in order to maximize the combustibility (reactivity). In addition, as the volatile and combustible components (carbon, hydrogen, etc.) contained in the fuel are consumed by the devolatilization, gasification and combustion process of the solid fuel, the ash remains, and in this process, The size of the oxygen-donating particles may be reduced and the size and weight of the oxygen-donating particles may be further reduced

The particulate mixture of oxygen donor particles and ash mixture contains oxygen donor particles with high particle density (heavy) and large particle size, and a low particle density (lightweight) and small particle size. Therefore, if the materials can be separated and removed continuously by using the difference in characteristics (density and size) of these particles, it is possible to minimize the problems caused by the accumulation of the ash and the economic loss caused by the disposal of the mixture of the ash and the oxygen- have.

In the present invention, a material separator 134 for removing such a material is proposed, which is applied to the solid fuel medium circulation combustor 101 as shown in FIG. In the solid fuel medium circulation combustor 101 of FIG. 3, the same reference numerals are applied to the same components as those of the solid fuel medium circulation combustor 100 of FIG. 2, and detailed description thereof is omitted. However, there is a difference that the reduction reactor discharge pipe 130 is connected to the material separator 134.

The material separator 134 separates the oxygen donor particles (solid particles) and the ash supplied from the reducing reactor discharge pipe 130 by the specific gravity difference and supplies the material to the material cyclone 144. The material cyclone gas discharge pipe 146 of the material cyclone 144 discharges the residual gas to the outside and the material cyclone solid discharge pipe 148 discharges the ash.

The oxygen donor particles are supplied to the oxidation reactor 102 through the solid particle discharge pipe 140 of the material separator 134.

Next, the material separator 134 will be described with reference to Figs. 4 to 6. Fig. The material separator 134 includes a casing 150 having a space therein and having a length in the longitudinal direction, an inlet port 130 through which the material and the solid particles are mixed and supplied, A gas distribution plate 152, a fluidized gas supply pipe 136 for supplying a fluidized gas to a lower space of the gas distribution plate 152, and a solid intake hole 136 formed through the gas dispersion plate 152, A solid spray tube 154 for sucking the material and the solid particles placed on the upper side of the gas dispersion plate 152 through the discharge port 162 and spraying the same to the inside of the casing 150, A solid particle outlet port 158 connected to the solid particle receiver 156 for discharging only solid particles to the outside and a solid particle outlet port 158 for discharging only solid particles to the outside, Fly ash that is installed and discharges fly ash with gas It comprises a pipe (166).

The casing 150 is in the form of a fluidized bed reactor, and a space through which the fluidizing gas is introduced by the fluidizing gas supply pipe 136 is formed below the gas distributing plate 152. Steam or carbon dioxide may be used as the fluidizing gas.

A solid spray tube 154 is installed through the lower portion of the casing 150 and the gas dispersion plate 152. The solid spraying tube 154 sucks the surrounding solid particles and the ash into the space of the casing 150 so that the light ash is raised by the surrounding flowing gas and the relatively heavy solid particles are dropped do. At this time, a solid suction hole 162 for sucking solids around the solid spray tube 154 is formed on the surface of the solid spray tube 154.

At this time, the position of the solid suction hole 162 is considerably important for effectively sucking the solid particles loaded on the gas dispersion plate 152 of the casing 150. Therefore, in the present invention, it is important to adjust the height H4 of the solid layer existing above the solid suction holes 162 to be suitable for solid suction, ) Can be controlled by controlling the amount of solid that is injected.

A solid particle receiver 156 in the form of a bowl for containing falling solid particles is disposed around the solid spray tube 154. Since the fluid passes around the solid particle receiver 156, the material shot upward by the solid ejecting tube 154 rises together with the fluid, and only heavy or large solid particles are allowed to flow into the solid particle receiver 156. [ (156). And a solid particle outlet port 158 connected to the solid particle receiver 156 for discharging only solid particles to the outside and the solid particle outlet port 158 is connected to the oxidation reactor 102 Lt; / RTI >

A casing discharge pipe 166, which is installed on the upper portion of the casing 150 and discharges the fly ash together with the gas, is formed protruding into the casing 150. The material discharge pipe (166) can change the height from the gas distribution plate. As a result, it is possible to set the exact position at which the solid particles are discharged but only the material is discharged.

A washer discharge pipe fixing portion 163 is formed on the casing 150. The ash discharge pipe fixing portion 163 may be formed as a pipe having an outer diameter larger than that of the ash discharge pipe 166. An adjustment screw 168 is formed on an outer peripheral portion of the ash discharge pipe 166 and the adjustment screw 168 is screwed to the ash discharge pipe fixing portion 163 to connect the ash discharge pipe 166 and the gas dispersion It is possible to finely adjust the distance H1 between the plates 152. [

The flange 164 formed in the holding pipe 163 and the flange 170 formed around the holding pipe extension pipe 138 into which the holding pipe 166 is inserted can be screwed The material pipe extension pipe 142 is connected to the material cyclone 144 described above.

Alternatively, a flange may be simply formed around the ash discharge pipe, and the front end of the discharge pipe may be inserted into the discharge pipe fixing part 163 to be exposed to the inside of the casing 150, And the flange 164 formed on the washer discharge pipe fixing portion 163 may be used.

[Test Example]

The performance test of the ash separator shown in Fig. 4 was performed in a cold model simulating the flow.

The model was carried out under the condition that the particles were transported by air under ambient conditions. A cylindrical acrylic tube with a certain cross section (inner diameter of 15 cm) was used as the material separator, and a 25 mm perforated plate with a square pitch of 1 mm was used as the gas dispersion plate. Respectively.

An acrylic tube with an inner diameter of 24 mm was used as the ash discharge pipe, and the height of the ash discharge pipe was set at 0.75, 0.80, and 0.85 m from the top of the gas dispersion plate.

The solid spraying tube used was a 7.45 mm inner diameter stainless steel tube, the total length was 0.6 m from the gas distribution plate, and the solid inlet was 0.15, 0.25, and 0.35 m from the gas distribution plate.

As the oxygen donor particles, OCN 706-1100 particles (NiO weight content 70%) were used. The average particle size was 139 μm, the particle size distribution was 106-212 μm, and the bulk density was 1655 kg / m 3.

P-110 particles (a mixture of K ₂ CO ₃ and MgO and a support) used as a CO ₂ absorbent were used as the particles for simulating the material. The average particle size was 58 μm, the particle size distribution was 0 to 75 μm, The density is 640 kg / m3.

In the sorbent separator, oxygen donor particles and CO ₂ sorbent were mixed at a ratio of 5: 5 by weight. In the sorbent separator, the height of the solid particles was 0.5 m above the gas dispersion plate.

In the experimental results, the solid discharge rate (G) represents the discharge rate (kg / hr) of the mixed particles through the ash discharge pipe 160 per unit time, and the separation efficiency E represents the P- 110 particle weight percentage (%).

6, when the height H2 of the solid intake hole 162 is 0.15 m from the gas distribution plate and the flow rate Q1 of the fluidizing gas is 18.2 Nl / min (U1 = 0.018 m / s) The flow rate Q2 was changed to 2, 4, 6, 8 and 10 Nl / min (U2 = 0.81, 1.61, 2.42, 3.23 and 4.04 m / s) and the height H1 of the discharge pipe was 0.75, 0.80 and 0.85 m, the change in the discharge rate (G) and the separation efficiency (E) of the solid mixture through the ash discharge pipe are shown.

As shown in FIG. 6, as the height H2 of the solid suction hole 162 is equal to the height H1, the amount of the solid to be injected increases as the flow rate of the solid injection tube increases. The discharge rate increased and the separation efficiency of the materials tended to decrease. Also, when the flow rate of the solid injection nozzle is the same, as the height (H1) of the material discharge pipe increases, the distance (H3) between the material discharge pipe and the solid discharge pipe increases, so that the discharge rate of the mixed particles through the material discharge pipe decreases. Separation efficiency of the ash was increased.

As a result, FIG. 6 shows that the discharge rate and separation efficiency of the mixed particles can be controlled by changing the flow rate of the solid injection nozzle and the height H1 of the discharge pipe. On the other hand, the separation efficiency was 91.6 ~ 100% in this experimental range.

7, when the height H1 of the ash discharge pipe is 0.85 m from the gas distribution plate and the flow rate of the fluidizing gas is 18.2 Nl / min (U1 = 0.018 m / s), the flow rate Q2 of the solid- (U2 = 0.81, 1.61, 2.42, 3.23, 4.04 m / s) and changing the height H2 of the solid intake hole 162 to 0.15, 0.25, and 0.35 m (G) and the separation efficiency (E) of the solid mixture through the ash discharge pipe when the height (H4) of the solid layer existing above the solid suction hole was changed.

As shown in FIG. 7, as the flow rate of the solid injection nozzle increases under the condition that the height H2 of the solid intake hole 162 is equal to the height H1 of the material discharge pipe, the amount of the solid to be injected increases, The discharge rate of the particles increased and the separation efficiency of the ashes tended to decrease. Also, when the flow rate of the solid spraying tube is the same, the height H4 of the solid layer existing above the solid suction hole decreases as the height H2 of the solid suction hole 162 increases, In contrast, the separation efficiency of the materials tended to increase.

As a result, the discharge speed and the separation efficiency of the mixed particles can be controlled by changing the height H2 of the solid suction hole 162, that is, the height H4 of the solid layer present above the solid suction hole I can prove that. On the other hand, the separation efficiency was 92.7 ~ 100% in this experimental range.

Oxygen donor particles, which are large and heavy by the fluidized bed, are mainly present in the lower portion of the solid layer inside the material separator 134, and small and lightweight materials may cause segregation in the upper portion of the solid layer in the material separator. When the particle separation phenomenon occurs, the material is present in the upper part of the solid layer. Therefore, when the height H2 of the solid intake hole 162 is increased in the solid injection pipe 154, the solid mixture is injected into the solid mixture hole 162 It is possible to separate the material from the lower flow rates (lower U2 and Q2) since the fraction occupied by the material can be increased, and the fraction of the material in the solid injected through the solid ejection tube 154 increases, Can be increased.

On the other hand, when the height H2 of the solid intake hole 162 increases, the height H4 of the solid layer existing on the solid intake hole 162 decreases, so that the pressure applied by the solid decreases and flows into the solid inlet The total solid amount decreases. Therefore, it is possible to select the height H2 of the solid intake hole 162 that is suitable for the experiment.

In addition, at the upper end of the solid spray tube 154, there exist particles mixed with oxygen donor particles. However, as the height increases, the fraction of oxygen donor particles decreases and the fraction of the ash particles increases. Therefore, if the installation height H1 of the material discharge pipe 166 is increased, the separation efficiency of the material can be increased. However, increasing the installation height H1 of the ash discharge pipe 166 decreases the total solid discharge amount (oxygen donor particle + ash) through the ash discharge pipe 166. [

Further, as the diameter of the material discharge pipe 166 changes, the flow rate U4 at the discharge pipe changes. Increasing the diameter of the discharge tube decreases U4, reducing the total solid emissions (oxygen donor particles + ash) and the ash separation efficiency.

The height and diameter of the ash discharge pipe 166 may be changed using a coupling structure having a plurality of flanges as shown in FIG.

As a result, according to the present invention, the material is separated from the system by using a sorbent separator that receives a mixture of the oxygen donor particles and the sorbent material from the reduction reactor of the medium circulation combustor and separates the material into oxygen donor particles, . ≪ / RTI > To do this, basically, we use the difference in the speed of the end of two particles, and by changing the height (H2) of the solid suction hole, segregation of two particles can be used together. Also, by changing the height H1 of the material discharge pipe, the concentration distribution of the solid particles in the axial direction of the upper portion of the solid spray tube 154 can be varied, thereby maximizing the separation efficiency of the material.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it will be understood by those of ordinary skill in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. It can be understood that

100, 101: solid fuel medium circulation combustor 102: oxidation reactor
104: oxidized fluidized gas supply pipe 106: oxidation reactor discharge pipe
108: Oxidation cyclone 110: Oxidized cyclone solid discharge pipe
112: oxidized cyclone gas exhaust pipe 114: loop chamber
116: loop chamber fluidized gas supply pipe 118: loop chamber discharge pipe
119: Solid fuel supply line 120: Reduction reactor
122: Reduction gas discharge pipe 124: Reduction cyclone
126: Reduction cyclone gas discharge pipe 128: Reduction cyclone solid discharge pipe
130: Reduction reactor exhaust pipe 132: Reduced fluidized gas supply pipe
134: material separator 138: material discharge pipe extension pipe
140: Solid particle discharge pipe 142: Solid spray pipe extension pipe
144: Material Cyclone 146: Material Cyclo gas discharge pipe
148: Material cyclone solid discharge pipe 150: The material separator
152: gas distributor plate 154: solid distributor pipe
156: Solid particle receiver 158: Solid particle outlet port
162: solid intake hole 163:
164, 170: flange 166:
168: Adjusting screw

Claims (6)

A casing having a space therein and having a long length in the longitudinal direction;
An inlet port through which the mixture of the material and the solid particles is supplied;
A gas distribution plate formed at a lower portion of the casing;
A fluidized gas supply pipe for supplying fluidized gas to a lower space of the gas distribution plate;
A solid distributor pipe installed through the gas distributor plate and sucking the solid material and the material loaded on the gas distributor plate through a solid suction hole formed on the outer periphery and injecting the solid material into the casing by the injection gas;
A solid particle receiver installed around the solid spray tube to receive falling solid particles;
A solid particle outlet port connected to the solid particle receiver to discharge only solid particles to the outside; And
And a material discharge pipe installed on the upper portion of the casing and protruding into the casing so as to discharge the material scattered with the gas.
The separator according to claim 1, wherein the ash discharge pipe is capable of changing the height from the gas distribution plate.
3. The separator according to claim 2, wherein the ash discharge pipe is attached to and detached from the discharge pipe fixing part formed on the upper part of the casing.
[3] The apparatus according to claim 2, wherein the ash discharge pipe is length-adjustable by screwing the ash discharge pipe fixing part formed at the upper part of the casing and is detachable from the ash discharge pipe fixing part while extruding the ash discharge pipe extrusion pipe As shown in Fig.
A solid fuel medium circulation combustor having a material separator according to any one of claims 1 to 4,
An oxidation reactor in which oxygen donor particles are fluidized to capture oxygen;
An oxidized cyclone separating a mixture of gas and oxygen-bonded particles discharged from the oxidation reactor;
A reducing reactor in which a gasification reaction of the solid fuel by the reducing fluidizing gas and a combustion reaction by the oxygen binding particles separated and supplied from the oxidized cyclone occur and discharges the material and the reduced oxygen donor particles;
A reducing cyclone for separating a mixture of gas and oxygen donor particles discharged from the reduction reactor and returning the mixture to the reduction reactor; And
And a material separator for separating the oxygen donor particles supplied from the reduction reactor and the material to transfer only oxygen donor particles to the oxidation reactor.
6. The method of claim 5,
And a material cyclone for separating a mixture of the ash and the gas discharged from the material separator is connected to the material separator.

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