JP3010207B2 - Gas and particle contact separation device - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas-solid multi-phase heat exchanger, a gas fuel combustion apparatus, or a gas-solid chemical reaction apparatus. The present invention relates to an apparatus for contacting and separating solid particles with a gas that mixes and contacts solid particles and separates the solid particles after contact.

[0002]

2. Description of the Related Art Conventionally, for example, cement production facilities,
There are many facilities and devices that emit high-temperature solid particles, such as steelmaking facilities, garbage incineration facilities, and fluidized bed boilers. Therefore,
Energy can be saved by exchanging hot particles discharged from these facilities with gas and recovering the waste heat.

However, conventional gas-particle heat exchangers are not efficient because of their low efficiency, complicated structure, large size, and high cost for installation. The recovery of waste heat from particles has not been put to practical use.

[0004] In addition to the above-mentioned existing facilities,
There is a demand for the development of an efficient heat exchanger between gas and particles in various heat engines and the like. For example, in a fusion reactor expected to be put into practical use in the future, the use of a so-called solid-gas multiphase flow in which gas and solid fine particles are mixed as a coolant is being studied.

[0005] That is, in the existing light water reactor or fast breeder reactor, a cooling method using light water or liquid sodium can sufficiently cope with the problem, but in a fusion reactor, particularly in a plasma facing device in the reactor, the heat load is several times larger than that of the light water reactor. For this reason, if this is performed by water cooling, it will be handled by high-pressure subcooled boiling, and energy recovery must be abandoned, and excessive pressurization under high temperature and strong neutron irradiation environment will be a structural material Greatly reduces the choices available. For this reason, it is desirable to use a solid-gas mixed-phase flow from which high energy recovery efficiency can be obtained without pressurization as the coolant.

In the future nuclear fusion power reactor, it is expected that a combined power generation system composed of a primary-side single-phase gas turbine cycle and a Rankine cycle with a secondary-side steam turbine will be used. When a solid-gas multiphase flow is used as a coolant in this system, the power density of the furnace is so high that the solid phase concentration of the multiphase flow must be increased, and the possibility of directing this to the gas turbine is not high. From turbine blade wear and damage due to the Therefore, it is necessary to reliably separate the multi-phase coolant into hot particles and single-phase gas introduced into the turbine upstream of the turbine to protect the turbine blades.

[0007] The method of heat exchange between particles and gas can be roughly classified into a separation type and a mixed type. The former separation type performs heat exchange between particles and gas through, for example, a heat transfer tube, and does not directly contact particles and gas, so that particles do not naturally enter the gas. However, the heat transfer mechanism of this method is a forced convection of a single-phase gas on the gas side and effective heat conduction in the porous body formed by the particle layer on the particle side, and has a large heat transfer resistance and low efficiency. In addition, it is necessary to move the particles in the outer region of the heat transfer tube, which complicates the moving mechanism of the particles, and causes problems such as adhesion of particles to the tube wall of the heat transfer tube, which is low in reliability. There is also a method of moving the particles by mixing them with a gas. However, this method only has an effect of improving the thermal resistance of the particles, and the heat transfer efficiency as a whole is also low.

In the latter mixing type, particles are mixed in a gas stream, heat is exchanged by bringing the gas into direct contact with the particles, and then the particles are separated by a cyclone or the like. Since the particles come into contact with the gas at a large specific surface area, heat is exchanged instantaneously, and the mechanism for moving the multiphase flow of the gas and the particles is simple and highly reliable. However, in this mixed type, the particles and the gas instantaneously reach the final equilibrium temperature as described above, and the temperature of the gas after heat exchange is equal to the temperature of the particles. Therefore, only the same efficiency as that of the parallel flow heat exchanger can be obtained.

In a mixed heat exchanger, the gas is allowed to flow upward at a speed lower than the gravitational sedimentation speed of the particles in the gas. Efficiency equivalent to a vessel can be obtained. However, in this case, the speed of the gas becomes extremely low, and the container becomes extremely large, so that it cannot be put to practical use at all.

As described above, a conventional heat exchanger between gas and particles has not been obtained which has the desirable characteristics such as high heat exchange efficiency, high reliability and miniaturization. For this reason, waste heat recovery from high-temperature solid particles in the equipment as described above, or in heat exchange between gas and particles in a future heat engine or the like, the high heat exchange efficiency as described above,
There has been a demand for a heat exchanger having desirable features such as high reliability and miniaturization.

[0011] Further, the problem of contact and separation between gas and particles as in the case of the mixed type heat exchanger as described above is as follows.
The present invention is not limited to a heat exchanger, but is common to, for example, a combustor for fine powder fuel, a device for performing a chemical reaction between gas and solid particles, and the like. That is, such particles are suspended in the gas, and the relative velocity between the particles and the surrounding gas instantaneously becomes substantially zero. This causes problems such as a reduction in the efficiency of the reaction.

[0012]

DISCLOSURE OF THE INVENTION The present invention has been made based on the above circumstances, and is intended to mix particles in a gas, bring them into direct contact, and perform heat exchange and chemical reaction between them. An object of the present invention is to provide a device for separating particles from a gas, which has high efficiency of heat exchange and chemical reaction, has high reliability, has a simple structure, and is easy to miniaturize.

[0013]

According to a first aspect of the present invention, there is provided a separation cylinder having a throttle portion at a lower portion arranged with a central axis directed substantially vertically, and an upper end of the separation cylinder in the separation cylinder. A swirling flow supply mechanism for ejecting a downward swirling flow of gas downward from a gas inlet in a peripheral portion, and a swirling flow supply mechanism that communicates with a center portion of an upper end portion of the separation cylinder and is ejected downward from the gas inlet. A gas outlet for reversing the swirling flow of gas upward in the separation cylinder and discharging the same, and a particle inlet opening at the center of the upper end of the separation cylinder and supplying solid particles to the center of the separation cylinder. It is provided.

Therefore, the particles supplied from the particle inlet to the central portion of the upper end in the separation cylinder are first mixed into the upwardly flowing gas into the above-mentioned gas outlet in a swirling flow of the gas. , And move outward by centrifugal force, and then come into contact with the swirling flow of downward gas ejected from the gas inlet, and further move outward and downward by centrifugal force. And separated from the gas.

In this case, for example, in a heat exchanger, the low-temperature gas supplied from the gas inlet is brought into contact with the low-temperature particles moving in the separation cylinder and heat-exchanged.
Since it comes into contact with high-temperature particles in the vicinity of the gas outlet, high heat exchange efficiency equivalent to a countercurrent heat exchanger can be obtained. Further, in a device that performs combustion and chemical reaction between gas and particles, the particles supplied from the particle inlet move radially outward while swirling in an upward swirling flow toward the gas outlet.
In this region, the relative velocities of the particles and the gas are large, and the combustion and chemical reaction therebetween are efficiently performed.

In addition, this device completes all contact and separation of particles and gas in a swirling flow that has been turned upside down while being formed in the separation cylinder, so that the structure is simple and highly reliable. The separation cylinder and the like are miniaturized, and the miniaturization of the entire apparatus is easy.

According to a second aspect of the present invention, there is provided a particle dispersion in which the particles supplied from the particle inlet are disposed radially outside the particle inlet in the separation cylinder. Is provided. Therefore, the particles supplied from the particle inlet are dispersed radially outward by the particle dispersion, and are surely mixed into the gas swirl flow,
This prevents the supplied particles from moving downward through the center of the separation cylinder as it is.

According to a third aspect of the present invention, the swirling flow supply mechanism includes a plurality of spiral vanes disposed around the gas outlet. Therefore, the structure is simple, the reliability is high, and the device can be formed small.

According to a fourth aspect of the present invention, there is provided a heat exchanger configured to perform a heat exchange operation between particles supplied from the particle inlet and gas supplied from the gas inlet. Is what it is. Therefore, as described above,
It is possible to obtain a heat exchanger that has all the desirable features such as high heat exchange efficiency, high reliability, and downsizing.

[0020]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below with reference to an embodiment shown in the drawings. In this embodiment, the present invention is applied to a gas-particle solid-gas multiphase flow type heat exchanger. Although the heat exchanger of this embodiment has the features that are the gist of the present invention, it is a small device manufactured experimentally, and the heat of the actual machine used in the various facilities and devices described above. In the case of the exchanger, it is possible that various changes can be made without departing from the scope of the present invention, such as changing the structure, shape, etc. of each part, or adding additional equipment in accordance with those specifications. Of course.

First, the entire heat exchanger of the present invention will be schematically described with reference to FIG. In the figure, reference numeral 1 denotes a main body which is a main part of the heat exchanger. In the main body 1, gas and particles are mixed, heat is exchanged between them, and after the heat exchange is completed, gas and particles are mixed. The particles are separated. The configuration of the main body 1 will be described later in detail.

A low-temperature gas is supplied to the main body 1 through a gas supply pipe 3 by, for example, a blower 2. Reference numeral 4 denotes a gas flow detector, and reference numeral 5 denotes a control valve mechanism, which sends a signal to a controller (not shown) and is controlled by the controller. The high-temperature gas that has undergone heat exchange in the main body 1 is discharged via a gas discharge pipe 6.
In the middle of the gas discharge pipe 6. A cyclone separator 7 is provided, and when particles are undesirably mixed into the gas, the particles are reliably separated.

Reference numeral 8 in the figure denotes a hopper for temporarily storing high-temperature particles. The hopper 8 is supplied with, for example, equipment for discharging high-temperature particles or high-temperature particles separated from a solid-gas multiphase flow of a coolant of a fusion reactor.
The high-temperature particles stored in the hopper 8 are supplied into the main body 1 by a supply mechanism (not shown). In addition, a valve mechanism 9 for controlling the supply amount of high-temperature particles is provided below the hopper 8.

A particle recovery tank 10 is connected to a lower portion of the main body 1 to recover low-temperature particles separated after heat exchange. The collected low-temperature particles are sent by a moving mechanism (not shown) through the control valve mechanism 11 into the processing equipment or the coolant of the nuclear fusion reactor.

Next, the structure of the main body 1 will be described with reference to FIGS. The main body 1 includes a separation tube 20 for bringing gas and particles into contact with each other and separating the gas and particles, and a swirling flow supply mechanism 23 provided at an upper portion thereof and supplying a low-temperature gas into the separation tube as a swirling flow.

The separation cylinder 20 is a cylindrical contact cylinder 21
And a throttle portion 22 connected to the lower portion of the contact cylinder 21 and having a diameter reduced downward. The separation cylinder 20 is installed vertically with its central axis substantially along the vertical direction. Further, the lower end of the above-described restriction tube 22, that is, the lower end of the separation tube 20 is connected to the particle collection tank 10.
It communicates with the upper end.

The contact cylinder 21 is made of a transparent material such as a hard and heat-resistant glass material, and is configured so that the behavior of particles and gas inside the contact cylinder 21 can be measured. Note that such a structure is a structure adopted because the device of this embodiment is a trial device. Therefore, in an actual machine, the separation cylinder 20 is adapted to various conditions and uses such as the size and properties of particles, the type of gas, the temperature of particles, and the supply amount of particles and gas. It is needless to say that the shape and dimensions are designed so that the separation is most efficiently performed.

In the case of this embodiment, the above-mentioned swirling flow supply mechanism 23 is composed of an outer cylinder 24 and an inner cylinder 25. The inner cylinder 25 is airtightly attached to the inner peripheral surface of the outer cylinder 24. They are tightly fitted. A groove-shaped gas supply passage 26 is formed on the outer periphery of the inner cylinder 25. The gas supply passage 26 is continuous in the circumferential direction, and its cross-sectional area is continuously reduced in the circumferential direction. Shape. The start end of the gas supply passage 26 is connected to the outer cylinder 24.
Is connected to a supply port 39 formed tangentially on the peripheral wall of
The supply port 39 is connected to the gas supply pipe 3 via a supply nozzle 37.

A plurality of spiral vanes 30 are integrally formed on the outer periphery of the inner cylinder 25 located below the gas supply passage 26. A gas outlet 27 is formed at the center of the inner cylinder 24.
Is opened downward at the center of the upper end in the separation tube 20. The outside of the gas outlet 27 and the outer cylinder 24
An annular gas inlet 28 is formed between the inner periphery of the gas outlet 27 and the gas inlet 28. The gas inlet 28 surrounds the outside of the gas outlet 27 and opens downward at the upper end in the separation tube 20. are doing.

The low-temperature gas supplied into the gas supply passage 26 is swirled by the vane 30 and is ejected downward from the gas inlet 28 into the separation cylinder 20. The swirling flow of the gas ejected in this manner is turned upside down in the separation tube 20, becomes an upward swirling flow, and is discharged upward from the gas outlet 27. In this case, the swirling flow of the gas is inverted up and down as described above, but the swirling direction is of course the same.

A cusp portion 38 having a predetermined shape and an enlarged diameter is formed on the inner periphery of the lower end opening of the gas outlet 27. In the cusp portion 38, the gas inlet 28
Since the downward gas flow ejected from the nozzle and the upward gas flow flowing into the gas outlet 27 are adjacent to each other, a gas vortex is generated in this portion. And this cusp part 38
Is set in such a shape that such a vortex is formed strongly and stably.

The gas outlet 27 is connected to the inner cylinder 2.
5 and extends upward, and a cylindrical gas outlet tube 31 projects integrally from the upper end of the inner tube 25. An ascending cylinder 32 is connected to the upper end of the gas outlet cylinder 31, and the ascending cylinder 32 extends substantially vertically upward. The upper end of the ascending tube 32 is
6 is connected to the above-described gas discharge pipe 6.

The gas outlet 27 and the rising cylinder 3
The particle supply pipe 33 is provided substantially vertically along the axial direction at the center of the second. The upper end of the particle supply pipe 33 is connected to the hopper 8 to supply high-temperature particles. The lower end of the particle supply pipe 33 opens downward into the separation tube 20 at the center of the opening of the gas outlet 27, and the lower end opening is formed as a particle inlet 34. In this embodiment, the particle inlet 3
4. The gas outlet 27 and the gas inlet 28 are opened at substantially the same height, but as described above, the height of these openings can be set appropriately according to various conditions.

In the center of the above-mentioned separation cylinder 20,
Below the particle outlet 34, a particle dispersion 35 is provided concentrically with the particle outlet. Although not shown, the particle dispersion is held at a predetermined position by an appropriate stay that does not hinder the flow of gas and particles.

As shown in FIG. 4, for example, the particle dispersion 35 has a substantially spindle-shaped upper end and a lower end formed in a conical shape. Then, the particle dispersion 35 deflects the flow of the particles discharged downward from the particle inlet 34 radially outward. Since the lower end of the particle dispersion 35 is also formed in a conical shape, the particle dispersion 35 is configured so as not to hinder the swirling flow of the upward gas in the center of the separation tube 20.

Next, the operation of the above-described heat exchanger will be described. FIG. 5 schematically shows the state of the flow of gas and particles in the separation cylinder 20. In FIG. 5, the arrow lines indicate the gas flow, and the black circles P indicate the trajectories of the particles. As described above, the low-temperature gas supplied into the gas supply passage 26 is turned into a strong swirling flow by the vane 30 of the swirling flow supply mechanism, and is ejected downward from the gas inlet 28 into the separation cylinder 20 to descend. A flow region A is formed. On the other hand, since the gas outlet 27 is opened downward at the upper part in the separation tube 20, the gas flows in the middle part of the separation tube 20 in the axial direction, that is, the flow direction in the vertical direction is reversed. 20
In the central portion of, an upward swirling flow toward the gas outlet 27 is generated, and an upward flow region is formed. As described above, the swirling direction of the swirling flow in the downward flow region and the upward flow region is the same.

Then, high-temperature particles are supplied downward into the upward flow region B from the particle inlet 34 opened at the center of the upper end of the separation tube 20, and the high-temperature particles come into contact with the gas to cause heat exchange. Be started. At the same time, these particles swirl together with the swirling flow of the gas, and move radially outward due to the centrifugal force. The particles are more efficiently deflected radially outward by the particle dispersion 35 described above.

These particles move outward in the radial direction, and further move to the downflow region A. In this downward flow region A,
Since the swirling direction is the same, these particles P also continue to swirl in the downflow region A while contacting the gas and exchanging heat, and reach the inner peripheral surface of the separation tube 20 by centrifugal force. Then, these particles continue to swirl along the inner peripheral surface of the separation cylinder 20, and gradually move downward by gravity and the downward gas flow of the descending flow area A, and are collected in the above-described particle collection tank 10.

As shown in FIG. 5, the above-mentioned vortex is generated between the descending flow region A and the ascending flow region B, and the particles trapped by the vortex cause the inner surface of the cusp portion 38 or A boundary point that collides with the inner surface of the gas outlet 27 and flows downward and outward, that is, a reattachment point R to the wall surface is formed.
The particles that have moved to a lower region eventually move downward along the inner peripheral surface of the separation tube 20 and are collected in the particle collection tank 10. Therefore, by appropriately setting the positions and dimensions of the particle inlet 34, the gas outlet 27, the gas inlet 28, etc., and the shape and size of the separation tube 20 in accordance with various conditions, the particles supplied from the particle inlet 34 can be reduced. If it is set so as to surely move below the reattachment point R, the particles can be almost completely separated.

The above-described particle separation characteristics are not affected only by the reattachment point R as described above.
Generally, if the angle of the vane 30 is made shallow and gas is ejected at a shallower angle, or if the diameter of the separation tube 20 is increased, the efficiency of separating these particles is improved.

Next, the heat exchange characteristics of the heat exchanger will be described. FIG. 6 shows the amount of movement of the gas and the particles, for example, the distance from the particle inlet 34 and the change in the temperature thereof. In the figure, p indicates the temperature change characteristics of the particles, and g indicates the temperature change characteristics of the gas. As is clear from this figure, the temperature of the gas flowing from the gas inlet and starting to exchange heat with the particles has a parallel flow type characteristic in the downflow region, but shows a cross-current type characteristic in the upflow region. The gas is discharged in contact with the hot particles just after the last supply. In this embodiment, since the gas and the particles do not come into contact with each other in the region where the gas flow is reversed, the temperature of the gas shifts from point q to point q ′ in the drawing.

Although the heat exchanger is not a pure countercurrent type as described above, it is a heat exchange system with less irreversible loss than a pure parallel flow type, and a heat exchange efficiency close to the countercurrent type can be achieved. It is.

In general, the heat exchange performance of this heat exchanger is described as follows.
s, Gg [kg / s], and these specific heats are converted to Cs, Cg [J
/ KgK], and the temperature difference between these inlet and outlet is ΔT
Assuming that s and ΔTg [K], these exchanged heat amounts are as follows: GsCsΔTs = GgCgΔTg (1) Since the heat transfer between the fine particles and the gas is good and the irreversible loss corresponding to the normal heat passage resistance is small, in order to minimize the irreversible loss in an ideal countercurrent heat exchanger, ΔTs = ΔTg is required, and together with the expression (1), Γth = (GsCs) / (GgCg) = Γ (Cs / Cg) = ΔTg / ΔTs = 1 (2) Here, the mixed heat loading ratio Δth is defined as the ratio of the heat capacity of the blown gas [J / s · K] to the heat capacity of the supplied particles per unit time [J / s · K]. That is, use at a mixed heat loading ratio of around 1 is preferable from the viewpoint of heat exchange performance.

Further, when this heat exchange apparatus is used under the condition of high particle concentration (mixing heat loading ratio is 1 or more), particles supplied from the particle inlet 34 are maintained at a high concentration while maintaining a high concentration. It falls into the particle collection tank 10 linearly. For this reason, the gas introduced from the gas inlet 28 does not come into contact with the high concentration region of the particles, but flows into the gas outlet 27 with only slight contact with the particles immediately after the introduction, and the mixing thereof is not sufficiently performed. .

In order to improve such disadvantages, it is preferable to provide the above-mentioned particle dispersion 35. The high-concentration particles supplied from the particle inlet 34 are deflected radially outward by the particle dispersion 35 and diffused in a gas into a thin cloud, and come into good contact with the gas. High specific efficiency is achieved by the specific surface area. In addition,
In the particle dispersion 35 of this embodiment, since the upper end and the lower end have a tapered conical shape, the flow of particles can be reliably diffused radially outward as described above, and the gas flow There is an advantage of not hindering.

The results of a test performed to confirm the effect of the above particle dispersion 35 are shown in FIGS. In this test, glass beads having a particle diameter of 56 μm were used as the particles in the apparatus of the above-described embodiment, the blowing speed of the low-temperature gas was maintained at 12 m / s, and the hot-mixing loading ratio was kept close to 1 throughout the test. In addition, two thermocouple thermometers are provided at the inlet and the outlet of the particles and the gas, respectively, and six thermocouple thermometers are provided at each location to measure the temperature distribution in the apparatus. Data was collected and heat transfer performance was determined.

FIGS. 7 and 8 show the particle dispersion 35 described above.
Is removed, and particles are supplied at a high concentration with a mixed heat loading ratio Δth of 1.1. In this case,
As shown in FIG. 7, the temperature difference between the supplied particles and the recovered particles even after a lapse of time, and the temperature difference between the gas inlet and the gas outlet did not increase so much. Decreases only from 210 ° C to 100 ° C,
The gas temperature also rises only from 35 ° C. to 65 ° C., and the temperature at the gas outlet is much lower than the temperature of the recovered particles, and sufficient heat exchange is not performed.

On the other hand, when the above-mentioned particle dispersion 35 is provided, as shown in FIGS. 9 and 10, when the mixed heat loading ratio Δth is supplied at a high concentration of 1.0, As shown in FIG. 9, the temperature difference between the supplied particles and the recovered particles over time, and the difference between the gas inlet temperature and the gas outlet temperature increases, and as shown in FIG. From 70 ° C. to 70 ° C., the gas temperature also increases from 30 ° C. to 120 ° C., the temperature at the gas outlet rises significantly from the temperature of the recovered particles, and heat exchange is performed with high efficiency.

In the above test, when the above particle dispersion 35 was provided, this apparatus achieved high heat exchange efficiency. The heat efficiency of this heat exchange device is defined as η = heat received by gas / heat supplied by particles, and the above device also obtained a high value of about 50%. The apparatus of this embodiment is a small test apparatus as described above, and the heat loss, that is, the heat loss of the apparatus with respect to the amount of heat flowing into the apparatus is as high as about 25%. Correction calculation with the heat loss of this device as zero gave a high value of thermal efficiency of about 86%. Incidentally, in the case of the conventional simple mixing, solid-gas re-separation type solid-gas heat exchanger, even under the condition that the heat loss to the apparatus is substantially zero, the heat efficiency is about 50%. In comparison, it is clear that the efficiency of the heat exchanger according to the invention is very high.

The present invention is not limited to the above embodiment. As described above, the actual heat exchanger of the present invention is appropriately designed in accordance with various conditions such as the properties of gas and particles, the capacity and size of the device, and the like. Therefore, the shape and arrangement of the separation cylinder, the particle dispersion, the swirling flow generating mechanism, and the inlet and outlet of the particles and gas are appropriately set according to these conditions, and are not limited to the above embodiment. Absent.

Furthermore, the present invention is not limited to a heat exchange device between particles and gas as described above. INDUSTRIAL APPLICABILITY The present invention makes it possible to efficiently bring particles and gas into contact with each other and to separate these particles reliably and efficiently. This characteristic allows application to various devices. For example, the present invention can be applied to a combustor that burns fine solid fuel, various chemical devices that chemically react particles and gas, and the like.

[0052]

As described above, according to the present invention, all the contact and separation of particles and gas are completed in a swirling flow that is turned upside down while being formed in the separation tube, so that the structure is simple and reliable. In addition, the separation cylinder and the like are downsized, and the size of the entire apparatus can be easily reduced. In a heat exchanger, for example, the low-temperature gas supplied from the gas inlet contacts the low-temperature particles that have moved inside the separation tube and undergoes heat exchange, and then the high-temperature particles near the gas outlet. As a result, high heat exchange efficiency equivalent to that of the countercurrent heat exchanger can be obtained. Also, in a device that performs a chemical reaction between gas and particles,
The particles supplied from the particle inlet move radially outward while swirling in an upward swirling flow toward the gas outlet, so that the relative velocity between the particles and the gas is high in this region, and combustion and chemical The effect is great, such as efficient reaction.

[Brief description of the drawings]

FIG. 1 is a schematic diagram of a heat exchange device according to an embodiment of the present invention.

FIG. 2 is a longitudinal sectional view of a main part along line 2-2 in FIG. 1;

FIG. 3 is an exploded perspective view of a main part of the heat exchange device according to the embodiment.

FIG. 4 is a side view of the particle dispersion.

FIG. 5 is a diagram schematically showing the flow of particles and gas in a separation cylinder.

FIG. 6 is a diagram showing heat exchange performance.

FIG. 7 is a diagram showing a time series of temperature changes of particles and gas in the case where there is no particle dispersion.

FIG. 8 is a diagram spatially showing temperature changes of particles and gas in the case where no particle dispersion is provided.

FIG. 9 is a diagram showing a time series of temperature changes of particles and gas in the case where a particle dispersion is present.

FIG. 10 is a diagram spatially showing temperature changes of particles and gas in the case where there is a particle dispersion.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Main body part 2 Blower 8 Hopper 10 Particle recovery tank 20 Separation cylinder 23 Swirling flow supply mechanism 27 Gas outlet 28 Gas inlet 30 Vane 33 Particle supply pipe 34 Particle inlet 35 Particle dispersion

──────────────────────────────────────────────────続 き Continuation of front page (58) Field surveyed (Int.Cl. ⁷ , DB name) F28C 3/12

Claims (4)

(57) [Claims] 1. A separation cylinder arranged with a central axis directed substantially vertically and having a throttle portion at a lower portion, and a swirling flow of gas flowing downward from a gas inlet at a peripheral portion of an upper end portion into the separation cylinder. A swirl flow supply mechanism that forms a downward swirl flow downflow region in the peripheral portion of the separation tube, and communicates with the center of the upper end of the separation tube to flow the gas in the downflow region. A gas outlet for inverting and forming an upward flow region of an upward swirling flow in the center portion of the separation tube to discharge the gas, and opening the center portion of the upper end portion of the separation tube to allow the solid particles to A particle inlet for supplying the ascending flow region, and the solid particles supplied to the ascending flow region contact the gas and pass through the descending flow region by centrifugal force to reach the inner surface of the separation cylinder. A contact separation apparatus for separating gas and particles, wherein the separation is performed by separation. 2. A particle dispersion, which is disposed below the particle inlet and disperses particles supplied from the particle inlet radially outward in the separation cylinder. An apparatus for separating gas and particles according to claim 1. 3. A gas and particle as claimed in claim 1, wherein said swirling flow supply mechanism comprises a plurality of spiral vanes arranged around said gas outlet. Contact separation device. 4. The solid particles supplied to the upward flow region contact the gas, pass through the downward flow region by centrifugal force, and exchange heat with the gas in a counter-current type to form the separation cylinder. 2. The apparatus according to claim 1, wherein the apparatus is configured as a heat exchanger that reaches the inner surface and is separated therefrom.