Source: http://www.google.com/patents/US4464183?ie=ISO-8859-1&dq=5,987,610
Timestamp: 2014-08-27 22:06:57
Document Index: 669831174

Matched Legal Cases: ['art.\n4', 'art 28', 'art 28', 'art 42', 'art 42', 'art 147', 'art 195']

Patent US4464183 - Fluidized bed cooling; dedusting and tar removal - Google PatentsSearch Images Maps Play YouTube News Gmail Drive More »Sign in<nobr>Advanced Patent Search</nobr>PatentsAn overall process of cooling, dust removal, tar removal and heat recovery of high temperature gas generated in coal gasification furnaces, and apparatuses employed therefor are provided. In this process, specific apparatuses such as fluidized bed-cooler, fluidized bed-combustion furnace for regenerating...http://www.google.com/patents/US4464183?utm_source=gb-gplus-sharePatent US4464183 - Fluidized bed cooling; dedusting and tar removalAdvanced Patent SearchPublication numberUS4464183 APublication typeGrantApplication numberUS 06/492,638Publication dateAug 7, 1984Filing dateMay 9, 1983Priority dateJan 29, 1980Fee statusPaidAlso published asDE3102819A1, DE3102819C2, US4461629Publication number06492638, 492638, US 4464183 A, US 4464183A, US-A-4464183, US4464183 A, US4464183AInventorsKenji ArisakiOriginal AssigneeBabcock-Hitachi, Ltd.Export CitationBiBTeX, EndNote, RefManPatent Citations (5), Referenced by (10), Classifications (19), Legal Events (3) External Links: USPTO, USPTO Assignment, EspacenetFluidized bed cooling; dedusting and tar removalUS 4464183 AAbstract An overall process of cooling, dust removal, tar removal and heat recovery of high temperature gas generated in coal gasification furnaces, and apparatuses employed therefor are provided. In this process, specific apparatuses such as fluidized bed-cooler, fluidized bed-combustion furnace for regenerating granules, granular bed filter, gas cooler and, tar scrubber are successively and effectively employed. During the process, high, medium and low pressure steam, for example, are recovered by heat exchange in these apparatuses.
What is claimed is: 1. A process for the recovery of heat in coal gasification which comprises:generating gas in a coal gasification furnace providing a fluidized bed cooler containing fluidizing medium; introducing the gas as a gas flow into the fluidized bed cooler, thereby fluidizing the medium and heating it; providing heat transfer tubes disposed parallel to the direction of the gas flow, said heat transfer tubes having cooling medium passing therethrough; recovering the heat of the gas in a fluidized bed cooler as heated cooling medium; contacting the parallel tubes with the fluidizing medium, thereby cleaning the parallel tubes; adhering unnecessary substances including tar in the gas onto the fluidizing medium; and reducing the flow rate of the cooled gas at the top of the fluidized bed cooler to separate the cooled gas from the fluidizing medium then (a) passing the cooled separated gas through a moving granular bed filter to remove dust; (b) passing the gas from (a) through a gas cooler provided with a heat transfer pipe having cooling medium passing therethrough; (c) passing the gas from (b) through a gas scrubber; and (d) recovering the heat of the gas from (b) and (c) and wherein the cooling medium is water, the heat of the generated gas is recovered in the form of high pressure steam through the heat transfer tubes in the fluidized bed cooler, the waste heat in the gas cooler and scrubber is recovered in the forms of medium pressure steam and low pressure steam, respectively. 2. A heat recovery process according to claim 1, wherein char is produced in the furnace and further wherein heat exchange is carried out between char discharged from the coal gasification furnace and cooling medium to recover the heat of the char and combine this heat with that recovered in said fluidized bed-cooler.
3. A heat recovery process according to claim 1 wherein said fluidized bed-cooler comprises a body consisting of a vertical type vessel comprising a cylindrical part and an empty column part, said cylindrical part comprising a downcomer through which cooling medium flows down, passing through the axially central part of the fluidized bed of a fluidizing medium to be formed inside the body; a manifold provided at the lower end part of said downcomer; a group of heat transfer tubes extending radially from said manifold and then extending upwards in parallel to the flow of gas to be sent from the lowerpart of said body; and a header connected to the upper ends of said heat transfer tubes, said empty column part located above said cylindrical part and having a larger cross-sectional area than said cylindrical part.
4. A heat recovery process according to claim 1 wherein the fluidizing medium contained in said fluidized bed-cooler, onto which fluidizing medium unnecessary substances contained in the gas have adhered, is withdrawn from said fluidized bed-cooler and subjected to combustion treatment in a fluidized bed-combustion furnace to regenerate the fluidizing medium for recyclic use, and at the same time the heat generated by said combustion treatment is recovered by heat exchange with cooling medium contained in heat transfer tubes provided in said fluidized bed-combustion furnace.
5. The process of claim 1 further including removing dust from the gas before it is introduced into the fluidized bed cooler.
6. The process of claim 3, wherein the cooling medium is water, wherein steam having pressure in the range of 60 to 100 kg/cm2 G. is produced from said water by heat exchange, wherein the temperature of the surface of the heat transfer tubes is maintained at a range of 400�-500� C. and further wherein the gas is cooled to a temperature in the range of 400�-500� C.
7. The process of claim 1 wherein the cooling medium is water, wherein medium pressure steam having a saturated temperature corresponding to 200� to 250� C. is produced, wherein temperature of the surface of the heat transfer pipe is maintained above 200� C. and further wherein the gas is cooled to a temperature of approximately 250� C.
This is a continuation application of application Ser. No. 228,775, filed Jan. 27, 1981 now abandoned.
SUMMARY OF THE INVENTION An object of this invention is to provide a process for removing dust from the high temperature gas generated from the plants for coal gasification and also cooling the gas without any adhesion and solidification of tar and the like.
According to the present invention, a process is provided which mainly comprises passing the gas generated in coal gasification furnaces through a fluidized bed-cooler provided therein with heat tranfer tubes having cooling medium such as water passed therethrough, to thereby cool the generated gas and recover the heat of the gas in the form of hot water or steam, for example, and at the same time remove unnecessary substances contained in the gas through adhesion thereof onto the fluidizing medium constituting the fluidized bed.
As the fluidized bed-cooler employed in the present invention, an apparatus is preferable which comprises a body consisting of a verticle-type vessel; a downcomer through which cooling medium is passed, passing through the axially central part of the fluidized bed of a fluidizing medium to be formed inside the body; a manifold provided at the lower end part of the downcomer; a group of heat transfer tubes extending radially from the manifold and then extending upwards in parallel to the flow of gas to be sent from the lower part of the body; and a header connected to the upper ends of the heat transfer tubes.
Further, according to the present invention, an overall process for cooling, dust removal from and heat recovery from the gas generated in coal gasification furnaces is provided which comprises; a step of introducing the gas into a granular bed means such as a fluidized bed cooler and/or a moving bed filter, cooling the gas by cooling medium passed through heat transfer tubes provided inside said granular means and at the same time recovering heat from the generated gas by heat exchange with the cooling medium; and a step of passing the gas cooled in said granular bed means, successively through a gas cooler and a scrubber, to cool the gas and remove dust and tar-mist therefrom, and through the cooling and scrubbing of the gas in said gas cooler and said scrubber, recovering waste heat from the gas.
As the granular bed filter employed in the above process, an apparatus is preferable which comprises a body consisting of a vertical type vessel; a gas-introducing passage provided at the axially central part of the body; a plurality of louver-form walls provided so as to concentrically surround the gas-introducing passage; a means for forming moving beds by feeding medium of granules in the respective ring-form space between these louver-form walls; and nozzles for discharging the gas having passed through the louver-form walls and the moving beds of granules to the outside of the body, the respective upper ends of the louver-form walls being fixed onto the body by a granule-feeding duct, the respective lower ends of the louver-form walls being connected to a granule-discharging duct, and the respective granule-discharging duct being slidably contacted with the opening part of the body at the end part thereof so as to allow these granule-discharging ducts to expand thermally.
Further, the scrubber is further connected to a gas-liquid separator such as cyclone and is provided with a means for recirculating the tar condensed in the gas-liquid separator to the scrubber and also a heat exchange means for recovering the heat of the recovered tar in the form of low pressure steam of 3 kg/cm2 G.
BRIEF DESCRIPTION OF THE DRAWING FIG. 1 shows a flow diagram illustrating a process of cooling, dust removal, tar removal and heat recovery of the gas generated in coal gasification furnaces, in which process a fluidized bed-cooler is employed.
FIG. 10 shows a flow diagram illustrating a gas cooler and a scrubber for further cooling the gas discharged from the granular bed filter and removing tar mist therefrom.
DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of a process for cooling, dust removal, tar removal and waste-heat recovery of coal gas, employing a fluidized bed-cooler is illustrated in FIG. 1.
Coal inside a hopper 2 is fed to a reaction zone 5 inside a coal gasification furnace 1 where a gasification reaction is carried out at a high temperature and a high pressure together with a gasifying agent 3 such a hydrogen, steam (H2 O), etc. introduced therein. The gas generated by this reaction is led from the top of the furnace 1 into a dust collector 7 such as cyclone where dust contained in the gas is removed, and the collected dust is returned to the furnace 1. Residual char (abbreviated hereinafter to "Char") formed by the gasification reaction is discharged from the lower part of the furnace and flows into a char cooler 6 where heat exchange is carried out between the char and cooling water W fed through a piping 15A from a drum 13 to recover the heat of the char while the char being cooled. On the other hand, the reaction gas having left the dust collector 7 is led into a fluidized bed-cooler 9 wherein heat transfer tubes 14 are provided and a fluidizing medium such as sand is fluidized by introducing the reaction gas to form a fluidized bed 20. Cooling water W is flown from the drum 13 via a piping 15B into the heat transfer tube 14 inside the fluidized bed 20 to effect heat exchange between the cooling water and the reaction gas, resulting in the gas being cooled. At that time, tar, pitch, oil mist, etc. contained in the reaction gas adhere onto the surface of the fluidizing medium constituting the fluidized bed, which results in removal of unnecessary components contained in the reaction gas. After completion of the cooling and the removal of unnecessary components, the reaction gas enters a dust collector 12 where dust is removed, and then discharged to the outside of the system. On the other hand, a part of the fluidizing medium inside the fluidized bed-cooler 9, having unnecessary components adhered thereonto, is extracted at the lower part of the cooler to the outside and led into a hopper 11 for the extracted medium. The medium inside the hopper 11 is fed through a metering feeder 21 such as rotary feeder into a regeneration furnace 22 wherein organic components such as tar adhering to the medium are burnt. This regeneration furnace 22 is a fluidized bed furnace wherein a fluidized bed is formed by the medium extracted from the cooler 9 and fluidizing air A, and the components adhering onto the surface of the fluidizing medium are burnt. At that time, as in the cases of the char cooler 6 and the cooler 9, cooling water W inside the drum 13 is fed via a piping 15C into a heat transfer tube 23 inside the fluidized bed for heat recovery. After completion of the regeneration by burning, the fluidizing medium is transferred to a hopper 10 for the fluidizing medium and then fed via a valve 25 into the fluidized bed-cooler 9.
In the above-mentioned process, the respective portions of cooling water W, after having effected heat exchange in the char cooler 6, the fluidized bed-cooler 9 and the regeneration furnace 22, are returned via piping 24A, 24B and 24C to the drum 13, in the form of hot water or steam, and a portion of the stean is then discharged via a piping 17 to the outside of the system for utilization. Numeral 16 shows a pipe for feeding water W to the drum 13.
Reaction gas 38 at a high temperature flows into the body 26 through nozzle 40 provided at the spouting part 28, and fluidizes the fluidizing medium during its ascending inside the body 26, to form a fluidized bed 20. The high temperature gas 38 transfers its heat to the fluidizing medium and heat transfer tubes and is cooled during its passage through the fluidized bed 20, while the components contained in the reaction gas, i.e. tar, pitch, oil mist, etc. adhere to the fluidizing medium and are removed from the gas. Next, the fluidizing medium having a temperature elevated by the heat exchange between the medium and the reaction gas and having the components adhered thereto, is withdrawn from the body through a nozzle 44, while a fresh fluidizing medium is fed through a nozzle 46 to thereby keep the height of the fluidized bed at a definite one.
On the other hand, the heat transfer medium 48 (cooling medium) such as water passes through the downcomer 30 which descends through the central part of the fluidized bed 20 toward the spouting part 28, to the manifold 32 as a distributor, where the medium reverses its direction and ascends through heat transfer tubes 36. Thus, the heat transfer medium 48 inside the heat transfer tubes effects heat exchange between the medium and the reaction gas to cool itself, while the medium the gas is heated and discharged to the outside of the system in the form of hot water or steam (in the case where the heat transfer medium is water). After completion of the heat exchange, the reaction gas is led through the fluidized bed 20 to an empty column part 42. Since this empty column part 42 has a larger cross-sectional area than that of the cylindrical part located therebelow, the gas flow rate is reduced to cause the fluidizing medium whirled up by the gas flow to fall down, while the gas is discharged from an exit nozzle 50.
As to the granules 82 in the granular bed, those of the same specification as in the fluidized bed-cooler may be conveniently employed. The granules withdrawn from the granuler bed 60 are then treated in the regeneration furnace 22 which is a fluidized bed-combustion furnace and in which the granules are fluidized by combustion air 92 and dust and substances adhering onto the surface of the granules are subjected to combustion treatment by the aid of a combustion-aiding oil. Numeral 91 shows the granular fluidized bed. Numeral 93 and 95 each show a heat transfer tube provided inside the fluidized bed and at the top of the column, respectively. Numeral 97 shows a gas-discharging pipe.
The gas free of dust is further cooled by the cooler 62 and led through a short pipe 110 to the scrubber 64. The cooler 62 has a heat transfer pipe 113 through which cooling water is passed, which is connecteed to a boiler drum 109 via a riser pipe 111 and a downcomer 112. Feed water 114 to the boiler drum 109 is introduced into the drum 109, vaporized and withdrawn therefrom in the form of medium pressure steam 115. The tar contained in the gas has a limitation to fluidity in the vicinity of 150� C.; hence unless the inside of the cooler 62 is maintained above the temperature of 150� C., adhesion and solidification of tar occur. Thus, heat recovery in the cooler 62 is made so as to give steam whose saturation temperature corresponds to 200� to 250� C. As one of examples designed, a medium pressure steam of 15 kg/cm2 G at a gas temperature after cooling, of 250� C. and a wall temperature of the heat transfer tube above 200� C. may be employed.
Even if the bed of the granular bed filter 60 is provided in a pluraltiy of stages, the efficiency of dust removal has a limitation, but in the case where the scrubber 64 is further provided as mentioned above, a sufficient dust removal can be effected.
In general, such a dust-removing means of the granular bed type is effective for treating gases at high temperatures and high pressures. According to such a means, when a dust-containing gas is passed through a moving bed of slowly moving granules (abbreviated hereinafter to "bed"), the dust is caught by the granules, separated from the gas, and withdrawn from the bed along with the granules. Although there is the so-called kies-bed means employing fine particles such as sand, the granular bed means generally refers to the one employing granulated, calcined granules of e.g. alumina having a granular diameter of 1 to 2 mm. As to the efficiency of dust removal, for example in case where the dust removal is applied to a process for low calory gasification of coal by a partial oxidation with air, experimental results show that when the thickness of the bed through which the gas passes is in the range of 300 to 600 mm, the efficiency of dust removal at one stage (one layer) is in the vicinity of 90%, whatever moving rate of alumina granules may be employed. Thus, in order to sufficiently elevate the efficiency of dust removal up to 95% or higher, it is required to employ a plurality of stages as the bed. Further, the granules should be moved at a definite rate by metering charge and discharge between partition walls. In the case of high temperature gas, a countermeasure to absorption of the thermal expansion of members constituting these partition walls is required, and moreover, it is also required to pay attention so that the gas may not be shorted.
The bed 145 placed between the concentric, ring-form louvers 144 has a bed thickness of e.g. 500 to 600 mm in which the granules are filled, and the end part of the outer louver 144 is connected to a downcomer 157 through a cone 156, which downcomer 157 is fit in a sleeve 158 connected to an exit nozzle 159, in a loose contact manner, to form the so-called thermal sleeve. The taper angle of the cone 156 is made sufficiently smaller than the angle or repose of the granules so that the granules may fall easily. By constructing the first stage bed 145 as described above, it is possible to easily pass the gas through the bed 145 and also to permit the granules to fall smoothly without their springing out of the bed.
The second stage bed 146 is similar to the first one in the construction except that the second stage is larger in the diameter and concentrically inserted outside the first one. Namely, the second stage bed 146 consists of a bed of the granules placed between cylindrical louvers 148, the upper part of the outer louver being connected to an inlet nozzle 160 through a cone 161, and the lower part thereof being connected to a sleeve 163 through a cone 162. The sleeve 163 is loosely contacted with a lower opening part of the body 134 with a certain allowance, and a nozzle 164 is fixed to this lower opening part through a sleeve 165. In addition, a guide plate 166 is provided so that the granules may be easily discharged from the nozzle 164. Further, for the gas seal of the space part 147 between the beds 145 and 146, partitioning plates 168 are provided at the upper and lower parts of the space part, respectively, and also for the gas seal of the outer side space 149, a partitioning plate 170 is provided. In addition, the upper part of the outer side space 149 constitutes a gas passage 151 as mentioned above. Since the thickness of the beds makes the resistance to the gas flow, a higher resistance to the as flow than those brought about by the thickness of the beds is provided at any other opening parts, whereby there is no fear of the short-circuit of the gas, e.g. a gas leak from the bed 145 to the exit nozzle 159, a gas leak from the bed 146 to the nozzle 164, etc.
As the granules of the first stage bed 145 and the second stage bed 146, spheres of calcined alumina, etc. having a diameter of 1 to 2 mm may be preferably employed, and the granules of the first stage bed 172 (indicated by X marks) and those of the second stage bed 174 (indicated by 0 marks) may have either the same specification or different ones. The same specification may be convenient in the point of regeneration of granules after withdrawal from the vessel. In order to elevate the efficiency of dust removal in the second stage bed 146, for example the diameter of the graunules 174 may be made somewhat smaller.
According to the above-mentioned granular bed filler, wherein a plurality of stages of granular beds are formed inside the pressure vessel, it is possible to elevate the efficiency of dust removal and at the same time make the apparatus smaller or compact. Further, since the inside structures are constructed in a suspended manner and also the thermal sleeves are employed, the thermal expansion of the apparatus can be absorbed easily, and the thermal deformation of the apparatus as well as the short-circuit of the gas can be prevented.
Coal gas to be introduced into the granular bed filter 60 has a temperature of 400� to 500� C. and a pressure of 20 to 30 kg/cm2 G, and if the regeneration furnace 22 connected to this granular bed filter 60 is also under such a high pressure, the amount of combustion air i.e. fluidization air increases proportionally by an amount corresponding to the pressure. As a result, the amount of auxiliary fuel also increases. Further, the combustion exhaust gas will be also under pressure, resulting in necessity of recovering power by e.g. an expansion turbine, which makes the apparatus complicated. Thus, from the standpoint of the economy of the system, it is preferable to operate the regeneration furnace 22 under normal pressures.
FIG. 8 shows a systematic view of an apparatus for operating the regeneration furnace 22 connected to the granular bed filter 60 under normal pressures. On the pipeline connecting the granular bed filter 60 to the regeneration furnace 22 are successively provided a rotary valve 180, a lock valve 181, a lock hopper 182, a lock valve 183, a hopper 184 and a rotary valve 185. Further, on the pipeline for recirculating the granules regenerated in the regeneration furnace 22 to the granular bed filter 60, are successively provied a granule-blowing-up means 96, a primary hopper 100, a secondary hopper 186, a lock valve 187, a lock hopper 188, a rotary valve 189, and a lock valve 190.
Next, the medium granules are cooled down to a temperature approximate to the operation temperature of the granular bed in the regeneration furnace 22 and then sent by means of compressed air 99 through the blowing-up means 96 and the pipeline 98 to the upper hopper 100. Then, the hopper 186, lock valve 187, lock hopper 188, rotary valve 189 and lock valve 190 are successively opened or closed to elevate the pressure of the atmosphere of the granules, followed by feeding the graules to the granular bed filter 60. By operating the regeneration furnace under normal pressures, a small amount of the air 92 fed to the regeneration furnace may be sufficient.
FIG. 9 shows a preferred embodiment of the regeneration furnace 22. This furnace consists of two stage fluidized beds of an upper stage fluidized bed 91A and a lower stage fluidized bed 91B connected to the bed 91A through an overflow pipe 198. Tar, etc. adhering to the granules are burnt in the upper stage fluidized bed 91A, and air to be used for combustion in the upper stage fluidized bed 91A is preheated in lower stage fluidized bed 91B and at the same time the regenerated granules are cooled therein. The granules in a hopper 184 are fed through a rotary valve 185 and a feed pipe 193 to the upper stage fluidized bed 91A. Air preheated in the lower stage fluidized bed 91B is sent through a perforated plate 194 into the upper fluidized bed 91A, wherein tar, etc. adhering to the granules are burnt to regenerate the granules. If the amount of heat is insufficient, an aauxiliary fuel 128 is fed, while if it is in excess, the excess amount of heat can be recovered by means of a heat transfer coil 93 provided in the fluidized bed 91A. The resulting combustion waste gas is subjected to cooling and heat recovery by means of a waste heat recovery coil 95 provided inside an empty column part 195; sent through a duct 97 to a dust-collector 196 where dust is finally caught; and exhausted through a pipeline 197 as a clean gas. The granules subjected to combustion treatment in the upper fluidized bed 91A descend through the overflow pipe 198 provided inside the upper stage fluidized bed, to the lower stage fluidized bed 91B where the granules are cooled by contacting directly with the combustion air 92, and on the other hand, the combustion air is heated. The cooled granules are transported through the duct 94 to the top of the granular bed by means of the blowing-up means 96. The temperature of the medium of granules leaving the fluidized bed 91B is preferably made similar to that of the granular bed to maintain heat balance between them, which is easily designed by selecting the height of the lower stage fluidized bed and the superficial velocity in the column.
According to the above-metioned embodiment, it is possible to regenerate the granules contained in the granular bed filter 60 under normal pressures; hence it is possible to reduce the respective amounts of combustion air and auxiliary fuel down to smaller ones than those under high pressures, and also simplify the structure of the apparatus.
In FIG. 10, gas coolers 62A and 62B each have a plurality of heat transfer tubes 200 vertically arranged in a vertical type vessel and the lower ends of these heat transfer tubes 200 are opened inside respective scrubbers 64A and 64B. Further the respective coolers 62A and 62B are connected to a drum 109 through risers 111A and 111B and downcomers 112A and 112B, and also function as a waste heat boiler. The drum 109 is provided with a water feed line 114 and a steam discharge line 115. If only one cooler of large capacity is employed, gas distribution to the heat transfer tubes 200 becomes uneven and hence the descending condition of steam inside the heat transfer tubes 200 is unbalanced. For this reason, and for making its open sweeping easier, a plurality of coolers of small capacity are employed. Although two coolers 62A and 62B are shown in the figure, in the case of an amount to be treated, of 1000t/day, e.g. 6 coolers may be employed. On the other hand, the respective scrubbers 64A and 64B provided just below the coolers 62A and 62B have therein a nozzle 201 for spraying recovered tar sent through a line 127, and by spraying recovered tar through the nozzle 201 and contacting the recovered tar directly with the gas, gas cooling and recovery of tar mist are at the same time effected.
Coal gas cooled in advancwe down to 400� to 500� C. is passed through a line 88, then branched, passed through lines 88A and 88B and introduced into gas coolers 62A and 62B. In the respective gas coolers, in order to prevent adhesion and solidification of tar onto the wall of the heat transfer tubes 200 and also to prevent uneven heat transfer of the tubes, the wall temperature of the heat transfer tubes is maintained at about 200� C. or higher. Thus, there may be selected such a saturation temperature of the discharge steam, e.g. 15 kg/cm2 G in terms of the steam pressure on the line 115 from the drum 109, that the gas temperature after cooling (the exit temperature of the heat transfer tubes 200) and the wall temperature of the heat transfer tubes 200 can be maintained e.g. at 250� C. and 200� C. or higher, respectively. Accordingly, the temperature inside the tubes is not reduced to 200� C. or lower, and the total surface of the heat transfer tubes is maintained at a uniform temperature. The exit gas of the heat transfer tubes contains tar mist, which is removed by contacting it with recovered tar having a temperature of about 150� C. in the scrubbers 64A and 64B directly following the heat transfer tubes. The above-mentioned temperature (150� C.) of recovered tar sprayed inside the scrubbers has been selected taking into consideration the fluidity and pumping of the tar inside the tubes. If the fluidity of tar is not hindered, temperatures lower than 150� C. may be employed. Thus, the tar and gas inside the scrubbers 64A and 64B are cooled down to about 200� C.; in the state of a gas-liquid mixed phase, passed through ducts 108A and 108B connected to the lower end nozzles 202A and 202B; and introduced into a gas-liquid separator 116 where they are separated from each other. This separator 116 is preferred to be of a cyclone type. It is possible to simplify the apparatus by providing one separator per two coolers as shown in the figure. Purfied gas obtained by separating tar mist is exhausted through a duct 118 to the outside of the system. On the other hand, recovered tar is collected through a piping 120 into a pot 122 and transported through a duct 124 and a pump 125 to a low pressure boiler 126. Excess tar is discharged through a duct 128 to the outside of the system and most part of the remainder is cooled down to e.g. 150� C. in the low pressure boiler 126 and then delivered through a duct 127 to a scrubber nozzle 201. As to the low pressure boiler 126, it is necessary to maintain the wall temperature of the heat transfer tubes at a temperature of 150� C. or higher at which the tar fluidity is kept, as in the case of the coolers; hence it is preferable to make the pressure inside the tubes a saturated vapor pressure corresponding to the above temperature. As a concrete example, the boiler 126 is so designed as to give 3 kg/cm2 G as the pressure of generated steam 204 (saturation temperature: about 140� C.) and 150� C. or higher as the tar temperature inside the heat transfer tubes in the boiler 126, while the temperature of feed water 203 is normal.
According to the above-mentioned embodiment, when the gas containing mist of adherent substances such as tar is cooled, it is possible to prevent adhesion and solidification of these adherent substances and effect waste heat recovery such as heat-exchange type recovery through steam formation; hence the thermal economy of plant is improved. Further, by employing recovered tar for the scruffers, cooling, dust removal and tar removal become easier without introducing any cooling medium from the outside of the system; hence it is possible to effectively utilize the tar which causes obstacles to the utilities of plant.
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