CN202440470U - Coke oven gas cooling and tar ammonia water separating device - Google Patents
Coke oven gas cooling and tar ammonia water separating device Download PDFInfo
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- CN202440470U CN202440470U CN2012200615549U CN201220061554U CN202440470U CN 202440470 U CN202440470 U CN 202440470U CN 2012200615549 U CN2012200615549 U CN 2012200615549U CN 201220061554 U CN201220061554 U CN 201220061554U CN 202440470 U CN202440470 U CN 202440470U
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Abstract
The utility model discloses a coke oven gas cooling and tar ammonia water separating device which comprises a tapered tray, a raw coke oven gas outlet, a raw coke oven gas cooling and tar separating tower, an ammonia water regulating tank, a centrifugal machine, a liquid level meter, a surplus ammonia water tank, a surplus ammonia water pump, a tar tank, a tar pump, a submerged pump, a liquid level tank, a plate type heat exchanger, a cooling ammonia water return pipe, a tar squeezing pump, a circulating ammonia water pump, a high-pressure ammonia water pump and a raw coke oven gas inlet, wherein the raw coke oven gas outlet is arranged in the upper end of the raw coke oven gas cooling and tar separating tower, the raw coke oven gas inlet is arranged in the upper part of the side of the raw coke oven gas cooling and tar separating tower, the high-pressure ammonia water pump and the circulating ammonia water pump are arranged on the lower part of the side of the raw coke oven gas cooling and tar separating tower, the tar squeezing pump connected through a pipeline is arranged on the lower end of the raw coke oven gas cooling and tar separating tower, the ammonia water regulating tank is arranged on the lower part of the other side of the raw coke oven gas cooling and tar separating tower and is connected through a pipeline, and the liquid level meter is arranged on one side of the ammonia water regulating tank. The coke oven gas cooling and tar ammonia water separating device has the advantages of simple integral structure, convenience for operation and use, good stability and high reliability.
Description
Technical field
The utility model relates to the cooling and the tar ammonia tripping device of coal oven dithio-gas, relates in particular to coke-oven gas cooling and tar ammonia tripping device.
Background technology
Coal gas refrigerative flow process can be divided into three kinds of indirect coolings, directly cooling and cold-direct-cooled mixing cooling.Above-mentioned three kinds of flow processs respectively have relative merits, can select to adopt according to industrial scale, processing requirement and other conditions with suiting measures to local conditions.What China extensively adopted at present is indirect cooling.The indirect cooling of coal gas: be cooled to 80～85 ℃ at bridge tube, effuser with the cyclic ammonia water sprinkling at the raw gas that goes out the carbonization chamber; Partly arrive transverse pipe initial cooler through gas-liquid separator gas then and in transverse pipe initial cooler, raw gas is cooled to 21～23 ℃ or 25～30 ℃, the process electrical tar precipitator is after gas blower is transported to next operation then.Liquid portion arrives the tar ammonia separator through tar-removing device, in the tar ammonia separator, tar is separated with ammoniacal liquor, and the tar of separating passes through ultracentrifuge and goes out and be transported to the tar groove after the partial impurities.An ammoniacal liquor part of separating uses another part ammoniacal liquor after air-flotation type removes the tar device, to arrive next operation as remained ammonia as cyclic ammonia water.Raw gas has not only been cooled off in the direct cooling of raw gas, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in the coal gas all reduces in a large number.Advantages such as directly cooling has the evaporation efficiency height, and the gas pressure loss is little, and the capital construction cost is little; Shortcoming is that power consumption is bigger, the perishable easy obstruction of ammoniacal liquor cooling heat exchanger.China's utility model patent 200610020411 discloses " a kind of method by separating tar in the ammonia water by cooling coal oven dithio-gas "; A kind of method by separating tar in the ammonia water by cooling coal oven dithio-gas is disclosed; Step comprises: the mixed air that ammonia spray is cooled off ammoniacal liquor that raw gas forms and raw gas goes out the mixed solution of tar and ammoniacal liquor through gas-liquid separator separates; Send into dish piece type three-phase centrifuge to this mixed solution; Utilize difference in specific gravity and the spinning principle of whizzer between ammoniacal liquor, tar and the coke tar refuse, accomplish the sharp separation of ammoniacal liquor, tar and coke tar refuse.Isolated ammoniacal liquor from flowing into the cyclic ammonia water groove, is used for circulated sprinkling cooling raw gas through return line.Adopt three-phase centrifuge that ammonia water and tar oil is separated, can accelerate oily water separation speed greatly, shorten disengaging time, and can cancel the clarifying tank that former separation profit is used.The shortcoming power consumption is bigger, and it is little to the requirement of quality to cut cyclic ammonia water, and remained ammonia is had relatively high expectations to quality.
The utility model content
The purpose of the utility model is; Overcome the weak point of prior art; A kind of coke-oven gas cooling and tar ammonia tripping device are provided, and the raw gas of feasible process effuser realizes synchronously that in raw gas cooling tar separation device raw gas tentatively cools off and the effect of tar ammonia initial gross separation.Cold between again coal gas being carried out after using low temperature ammoniacal liquor that raw gas is directly cooled off, guarantee refrigerative raw gas temperature and stability of flow; Low temperature ammoniacal liquor flushing liquor directly gets into the tar ammonia tripping device; Use dish piece type three-phase centrifuge to make tar, ammoniacal liquor, coke tar refuse separated in synchronization simultaneously remained ammonia cleaned more.Remained ammonia does not need directly to use through tar-removing device again.
Described coke-oven gas cooling of the utility model and tar ammonia tripping device include taper tower tray, raw gas outlet, raw gas cooling tar separation tower, ammoniacal liquor regulating tank, whizzer, liquidometer, remained ammonia groove, remained ammonia pump, tar groove, tar pump B, submerged pump, Lower tank, tar pump A, plate-type heat exchanger, cooling ammoniacal liquor return line, tar press pump, cyclic ammonia water pump, aqueous ammonia pump of high pressure and raw gas inlet.Raw gas cooling tar separation tower is the main component of the utility model, and the upper end at raw gas cooling tar separation tower is provided with the raw gas outlet; Side top at raw gas cooling tar separation tower is provided with the raw gas inlet, in the side bottom of raw gas cooling tar separation tower; Be provided with aqueous ammonia pump of high pressure and cyclic ammonia water pump,, be provided with the tar press pump of pipe connection in the lower end of raw gas cooling tar separation tower; Another side bottom at raw gas cooling tar separation tower; Through pipe connection, be provided with the ammoniacal liquor regulating tank, a side of ammoniacal liquor regulating tank is provided with liquidometer.In raw gas cooling tar separation tower, be provided with the taper tower tray.Side at the remained ammonia groove; Be provided with cooling ammoniacal liquor return line; Cooling ammoniacal liquor return line is provided with the cooling aqua ammonia pump; The lower end of cooling ammoniacal liquor return line is connected to the plate-type heat exchanger of raw gas cooling tar separation tower, and the other end of plate-type heat exchanger is then through top one side of pipe connection to raw gas cooling tar separation tower.Bottom at raw gas cooling tar separation tower is connected to whizzer through pipeline and tar pump A.Middle part at raw gas cooling tar separation tower is connected to Lower tank through pipeline and submerged pump.Whizzer to the remained ammonia groove, to the tar groove, connects tar pump B through another road pipe connection through one road pipe connection behind the tar groove; Then connect the remained ammonia pump behind the remained ammonia groove.Raw gas directly cools off and the tar ammonia separating technology behind the described coke oven collecting main of the utility model, and main flow process is that the gas part got into water cooling tower through the raw gas outlet that is distributed on the taper tower tray after the raw gas in the effuser got into the middle part of raw gas cooling, tar separation tower; Liquid portion gets into the tar ammonia tripping device.The flushing liquor that the spray cooling produces directly gets into the tar ammonia tripping device by the taper tower tray.The space outerpace of taper tower tray is the passage that raw gas gets into refrigerating unit.The low temperature ammoniacal liquor that the raw gas cooling is used gets into low temperature ammoniacal liquor regulating tank by the ammoniacal liquor regulating tank after the low temperature aqua ammonia pump is through the interchanger cooling; The a plurality of risers that link to each other with spray column are arranged at the top of low temperature ammoniacal liquor regulating tank; Low temperature ammoniacal liquor regulating tank is equipped with liquidometer; The wide 1.5m of the high 1.5m of low temperature ammoniacal liquor regulating tank, low temperature ammoniacal liquor get into low temperature ammoniacal liquor regulating tank from the many places, top.The ammoniacal liquor that gets into low temperature ammoniacal liquor regulating tank links to each other with each water distributor, and water distributor links to each other with insufflation showerhead.Low temperature ammoniacal liquor regulating tank semi-ring is on the cooling spray column.The very for a short time 0.015MPa that is no more than of spray pressure; The tower internal resistance is between 400～600pa; Superficial velocity 0.35～0.55m/s; Liquid-gas ratio is 9～12L/ m3, and total sprinkling amount of cooling ammoniacal liquor is controlled between 10～20 m3/m2h, and the littler one-level spray of amount that the bigger secondarys of the flow that one-level is sprayed spray and the distance of secondary spray should be controlled between 1.5～2m.The one-level spray is vertical each other with the water distributor of secondary spray, and the shower nozzle of secondary spray is distributed in the water distributor top of one-level spray.The selecting for use of water-distribution nozzle use that resistance is less should not to stop up the shower nozzle that should not come off, and preferably uses cooling tower nozzle specially used.Low temperature ammoniacal liquor is controlled between 22～24 ℃ summer, and cooled coal gas is controlled at about 24 ℃; Winter, cooled coal gas was controlled at about 22 ℃ owing to do not need low-temperature circulating water can low temperature ammoniacal liquor be controlled at 20～22 ℃, required low temperature ammoniacal liquor and gas temperature to change according to different processes.Cooled coal gas gets into electrical tar precipitator by cat head, in electrical tar precipitator, further removes tar and ammoniacal liquor.Spray cooling lime set taper tower tray is that the bottom that links to each other of the outer wall as a funnel top and raw gas cooling tar separation device is deep into below the liquid level of tar ammonia tripping device.The lower ending opening of spray cooling lime set taper tower tray between 1.0～1.5 meters, is provided with a plurality of raw gas outlets more greatly on the taper tower tray, raw gas outlet top is equipped with conical blast cap.The cross-sectional area sum of raw gas outlet here should be near the cross-sectional area of raw gas import.Generally between 40～60cm, the height of raw gas outlet should be between 30～50cm for the diameter of raw gas outlet, and the cone bottom diameter of blast cap exports greater than raw gas.The angle that taper tower tray and liquid level form is between 20～35 °.Tar can be on the taper tower tray coagulating sedimentation only otherwise influence phlegma normally gets into the tar ammonia tripping device and stop up raw gas and export and just need not manage it.Regular switched system steams the tar that tower will condense on the tower tray for a long time and all melts.The inside of tar ammonia separator is to be inverted a cone to be called inner cone; The auger footpath of inner cone is less than outer wall 40～60cm; Inner cone top is the taper plate of laying down, and the lay down top of plate of taper is connected with the outer wall of tar ammonia separator, and the bottom is goed deep into about the 50cm of cone inside.The taper plate of laying down is connected with inner cone near the raw gas import, rest part both at a distance of about 30cm.The bottom of spray cooling lime set taper tower tray also is lower than about the about 5～10cm of height of cone.Raw gas gets into the liquid portion of back generation and sprays phlegma and just directly gets into inner cone like this, and the tar process precipitates the bottom that arrives inner cone, and ammoniacal liquor will pass through the plate of laying down and above through inner cone, arrive outer cone.Be equipped with snakelike steam coils in the inner cone bottom of tar ammonia tripping device the tar of bottom is carried out temperature control, bottoms tar is controlled between 80～90 ℃, and top is controlled between 70～80 ℃.The height of sinuous coil about 1.5m, the mixture of initial gross separation tar and ammoniacal liquor at the middle part of snakelike steam coils by the tar pump delivery to dish piece type three-phase centrifuge, realize separating of tar, coke tar refuse and ammoniacal liquor.The tar of sinuous coil bottom is separated by the top that the tar press pump is transported to the tar ammonia tripping device with coke tar refuse again.Solid matter is pulverized in press pump, and tar presses the amount of pulp pump very little generally about 3-5m3/h.The ammoniacal liquor regulating tank in addition that links to each other with tar ammonia tripping device outer cone, the bottom of ammoniacal liquor regulating tank, middle part and top link to each other with tar ammonia tripping device outer cone respectively.The ammoniacal liquor that when system is unstable, produces can come the adjusting of short period of time more or less the time with the ammoniacal liquor regulating tank.When switched system, need replenish ammoniacal liquor to another system through the ammoniacal liquor regulating tank.Generally the top of the system of ammoniacal liquor regulating tank and operation and middle valve are opened, and bottom valve is closed.The ammoniacal liquor regulating tank is provided with the ammoniacal liquor height that liquidometer can be measured tar ammonia tripping device outer cone accurately.When liquid level is very low, need open bottom valve and replenish ammoniacal liquor to outer cone.When liquid level is very high is can be to another system's discharging ammoniacal liquor.The ammoniacal liquor that is used for cooling off raw gas is transported to low temperature ammoniacal liquor regulating tank through aqua ammonia pump through multi-group heat exchanger, and interchanger and pipeline use impregnating material or through rotproofing, interchanger preferably uses plate-type heat exchanger so that cleaning.Be provided with the tar outlet conduit at the middle part of sinuous coil, the tar of initial gross separation gets into dish piece type three-phase centrifuge by the tar pump, in dish piece type three-phase centrifuge, realizes separating of tar, coke tar refuse and ammoniacal liquor.The output that the amount that gets into the tar ammonia mixture of three-phase centrifuge equals amount and the tar of remained ammonia is added the amount of coke tar refuse.Control the amount of the tar ammonia mixture that gets into dish piece type three-phase centrifuge with the usage quantity of remained ammonia.The amount of generalized case remained ammonia is more than 6 times of tar output.It is parallel running that raw gas cooling, tar separation tower are two; Chilling spray tower internal pressure is controlled at-400～-600pa between; Tar ammonia tripping device top pressure is controlled at 0～-25pa between; Guarantee gas pressure-5 in the effuser～-10pa between, fluctuation is controlled at ± the 10pa scope in, change according to the technology different pressures.Unknown cause pressure should not be controlled and chilling spray tower internal resistance timely switched system when little in effuser occurring, timely switched system when hydrops is serious in definite taper tower tray.Normal circumstances should be switched primary system every month and normally move with the assurance system.The spray quench liquid gets into the tar ammonia tripping device can not produce big variation to the temperature of cyclic ammonia water.If the temperature of the heat cyclic ammonia water that the big steam sinuous coil of the amount transmission of spray quench liquid comes has regulating effect, the temperature of cyclic ammonia water is controlled at about 70 ℃.The waste water that other regional phlegma, ammoniacal liquor, tar and being difficult for is transported to WWT gets into Lower tank, is transported to the top of tar ammonia tripping device through submerged pump.
Described coke-oven gas cooling of the utility model and tar ammonia tripping device, one-piece construction is simple, and is easy for operation, good stability, safety is high.Use described coke-oven gas cooling of the utility model and tar ammonia tripping device, ammoniacal liquor is cooled off by horizontal water-tube cooler after passing through and directly raw gas being sprayed cooling after interchanger cools off again.Raw gas has not only been cooled off in the direct cooling of raw gas, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in the coal gas all reduces in a large number.Advantages such as directly the cooling evaporation efficiency is high, and the gas pressure loss is little, and the capital construction cost is little.Raw gas gets into the refrigerated separation tower and realizes that at first tar ammonia separates, and the top cooling sprayer that raw gas gets into tower cools off raw gas, and spray liquid gets into the bottom tar ammonia tripping device of tower and realizes that tar ammonia separates.Raw gas gets into the refrigerated separation tower and has realized that promptly the refrigerative effect has realized the purpose of tar ammonia initial gross separation again.The cooling of the raw gas of the utility model, knockout tower with gas-liquid separator, tar slag scraper, tar ammonia separator, etc. the effect of equipment all replace.Technology simply is convenient to operation, and greatly reduces the height of horizontal water-tube cooler.The tar that the tar ammonia tripping device comes out is realized separating of ammonia water and tar oils and coke tar refuse through three ultracentrifuges, and the ammoniacal liquor of separating uses as remained ammonia.
Description of drawings
Accompanying drawing 1 is the structural representation of said coke-oven gas cooling of the utility model and tar ammonia tripping device.1-taper tower tray, 2-raw gas outlet, 3-raw gas cooling tar separation tower, 4-ammoniacal liquor regulating tank, 5-whizzer, 6-liquidometer, 7-remained ammonia groove, 8-remained ammonia pump, 9-tar groove, 10-tar pump B, 11-submerged pump, 12-Lower tank, 13-tar pump A, 14-plate-type heat exchanger, 15-cooling ammoniacal liquor return line, 16-tar press pump, 17-cyclic ammonia water pump, 18-aqueous ammonia pump of high pressure, 19-raw gas inlet.
Embodiment
Existing with reference to accompanying drawing 1; Explain as follows in conjunction with embodiment: described coke-oven gas cooling of the utility model and tar ammonia tripping device include taper tower tray 1, raw gas outlet 2, raw gas cooling tar separation tower 3, ammoniacal liquor regulating tank 4, whizzer 5, liquidometer 6, remained ammonia groove 7, remained ammonia pump 8, tar groove 9, tar pump B10, submerged pump 11, Lower tank 12, tar pump A13, plate-type heat exchanger 14, cooling ammoniacal liquor return line 15, tar press pump 16, cyclic ammonia water pump 17, aqueous ammonia pump of high pressure 18 and raw gas inlet 19.Raw gas cooling tar separation tower 3 is main components of the utility model, and the upper end at raw gas cooling tar separation tower 3 is provided with raw gas outlet 2; Side top at raw gas cooling tar separation tower 3 is provided with raw gas inlet 19, in the side bottom of raw gas cooling tar separation tower 3; Be provided with aqueous ammonia pump of high pressure 18 and cyclic ammonia water pump 17,, be provided with the tar press pump 16 of pipe connection in the lower end of raw gas cooling tar separation tower 3; Another side bottom at raw gas cooling tar separation tower 3; Through pipe connection, be provided with ammoniacal liquor regulating tank 4, a side of ammoniacal liquor regulating tank 4 is provided with liquidometer 6.In raw gas cooling tar separation tower 3, be provided with taper tower tray 1.Side at remained ammonia groove 7; Be provided with cooling ammoniacal liquor return line 15; Cooling ammoniacal liquor return line 15 is provided with the cooling aqua ammonia pump; The lower end of cooling ammoniacal liquor return line 15 is connected to the plate-type heat exchanger 14 of raw gas cooling tar separation tower, and the other end of plate-type heat exchanger 14 is then through top one side of pipe connection to raw gas cooling tar separation tower 3.Bottom at raw gas cooling tar separation tower 3 is connected to whizzer 5 through pipeline and tar pump A13.Middle part at raw gas cooling tar separation tower 3 is connected to Lower tank 12 through pipeline and submerged pump 11.To remained ammonia groove 7, to tar groove 9, tar groove 9 backs connect tar pump B10 to whizzer 5 through another road pipe connection through one road pipe connection; Then connect remained ammonia pump 8 behind the remained ammonia groove 7.Cooling of the described coke-oven gas of the utility model and tar ammonia tripping device, main flow process are that the gas part got into water cooling tower through the raw gas outlet that is distributed on the taper tower tray after the raw gas in the effuser got into the middle part of raw gas cooling, tar separation tower; Liquid portion gets into the tar ammonia tripping device.The flushing liquor that the spray cooling produces directly gets into the tar ammonia tripping device by taper tower tray 1.The space outerpace of taper tower tray 1 is the passage that raw gas gets into refrigerating unit.The low temperature ammoniacal liquor that the raw gas cooling is used gets into low temperature ammoniacal liquor regulating tank 4 by ammoniacal liquor regulating tank 4 after the low temperature aqua ammonia pump is through the interchanger cooling; The a plurality of risers that link to each other with spray column are arranged at the top of low temperature ammoniacal liquor regulating tank 4; Low temperature ammoniacal liquor regulating tank 4 is equipped with liquidometer 6; The wide 1.5m of low temperature ammoniacal liquor regulating tank 4 high 1.5m, low temperature ammoniacal liquor get into low temperature ammoniacal liquor regulating tank 4 from the many places, top.The ammoniacal liquor that gets into low temperature ammoniacal liquor regulating tank 4 links to each other with each water distributor, and water distributor links to each other with insufflation showerhead.Low temperature ammoniacal liquor regulating tank 4 semi-rings are on the cooling spray column.The very for a short time 0.015MPa that is no more than of spray pressure, tower internal resistance are between 400～600pa, and superficial velocity 0.35～0.55m/s, liquid-gas ratio are 9～12L/ m
3, total sprinkling amount of cooling ammoniacal liquor is controlled at 10～20 m
3/ m
2Between the h, the littler one-level spray of amount that the bigger secondarys of the flow that one-level is sprayed spray and the distance of secondary spray should be controlled between 1.5～2m.The one-level spray is vertical each other with the water distributor of secondary spray, and the shower nozzle of secondary spray is distributed in the water distributor top of one-level spray.The selecting for use of water-distribution nozzle use that resistance is less should not to stop up the shower nozzle that should not come off, and preferably uses cooling tower nozzle specially used.Low temperature ammoniacal liquor is controlled between 22～24 ℃ summer, and cooled coal gas is controlled at about 24 ℃; Winter, cooled coal gas was controlled at about 22 ℃ owing to do not need low-temperature circulating water can low temperature ammoniacal liquor be controlled at 20～22 ℃, required low temperature ammoniacal liquor and gas temperature to change according to different processes.Cooled coal gas gets into electrical tar precipitator by cat head, in electrical tar precipitator, further removes tar and ammoniacal liquor.Spray cooling lime set taper tower tray is that the bottom that links to each other of the outer wall as a funnel top and raw gas cooling tar separation device is deep into below the liquid level of tar ammonia tripping device.The lower ending opening of spray cooling lime set taper tower tray between 1.0～1.5 meters, is provided with a plurality of raw gas outlets more greatly on the taper tower tray, raw gas outlet top is equipped with conical blast cap.The cross-sectional area sum of raw gas outlet here should be near the cross-sectional area of raw gas import.Generally between 40～60cm, the height of raw gas outlet should be between 30～50cm for the diameter of raw gas outlet, and the cone bottom diameter of blast cap exports greater than raw gas.The angle that taper tower tray and liquid level form is between 20～35 °.Tar can be on the taper tower tray coagulating sedimentation only otherwise influence phlegma normally gets into the tar ammonia tripping device and stop up raw gas and export and just need not manage it.Regular switched system steams the tar that tower will condense on the tower tray for a long time and all melts.The inside of tar ammonia separator is to be inverted a cone to be called inner cone; The auger footpath of inner cone is less than outer wall 40～60cm; Inner cone top is the taper plate of laying down, and the lay down top of plate of taper is connected with the outer wall of tar ammonia separator, and the bottom is goed deep into about the 50cm of cone inside.The taper plate of laying down is connected with inner cone near the raw gas import, rest part both at a distance of about 30cm.The bottom of spray cooling lime set taper tower tray also is lower than about the about 5～10cm of height of cone.Raw gas gets into the liquid portion of back generation and sprays phlegma and just directly gets into inner cone like this, and the tar process precipitates the bottom that arrives inner cone, and ammoniacal liquor will pass through the plate of laying down and above through inner cone, arrive outer cone.Be equipped with snakelike steam coils in the inner cone bottom of tar ammonia tripping device the tar of bottom is carried out temperature control, bottoms tar is controlled between 80～90 ℃, and top is controlled between 70～80 ℃.The height of sinuous coil about 1.5m, the mixture of initial gross separation tar and ammoniacal liquor at the middle part of snakelike steam coils by the tar pump delivery to dish piece type three-phase centrifuge, realize separating of tar, coke tar refuse and ammoniacal liquor.The tar of sinuous coil bottom is separated by the top that the tar press pump is transported to the tar ammonia tripping device with coke tar refuse again.Solid matter is pulverized in press pump, and tar presses the amount of pulp pump very little generally about 3-5m3/h.The ammoniacal liquor regulating tank in addition that links to each other with tar ammonia tripping device outer cone, the bottom of ammoniacal liquor regulating tank, middle part and top link to each other with tar ammonia tripping device outer cone respectively.The ammoniacal liquor that when system is unstable, produces can come the adjusting of short period of time more or less the time with the ammoniacal liquor regulating tank.When switched system, need replenish ammoniacal liquor to another system through the ammoniacal liquor regulating tank.Generally the top of the system of ammoniacal liquor regulating tank and operation and middle valve are opened, and bottom valve is closed.The ammoniacal liquor regulating tank is provided with the ammoniacal liquor height that liquidometer can be measured tar ammonia tripping device outer cone accurately.When liquid level is very low, need open bottom valve and replenish ammoniacal liquor to outer cone.When liquid level is very high is can be to another system's discharging ammoniacal liquor.The ammoniacal liquor that is used for cooling off raw gas is transported to low temperature ammoniacal liquor regulating tank through aqua ammonia pump through multi-group heat exchanger, and interchanger and pipeline use impregnating material or through rotproofing, interchanger preferably uses plate-type heat exchanger so that cleaning.Be provided with the tar outlet conduit at the middle part of sinuous coil, the tar of initial gross separation gets into dish piece type three-phase centrifuge by the tar pump, in dish piece type three-phase centrifuge, realizes separating of tar, coke tar refuse and ammoniacal liquor.The output that the amount that gets into the tar ammonia mixture of three-phase centrifuge equals amount and the tar of remained ammonia is added the amount of coke tar refuse.Control the amount of the tar ammonia mixture that gets into dish piece type three-phase centrifuge with the usage quantity of remained ammonia.The amount of generalized case remained ammonia is more than 6 times of tar output.It is parallel running that raw gas cooling, tar separation tower are two; Chilling spray tower internal pressure is controlled at-400～-600pa between; Tar ammonia tripping device top pressure is controlled at 0～-25pa between; Guarantee gas pressure-5 in the effuser～-10pa between, fluctuation is controlled at ± the 10pa scope in, change according to the technology different pressures.Unknown cause pressure should not be controlled and chilling spray tower internal resistance timely switched system when little in effuser occurring, timely switched system when hydrops is serious in definite taper tower tray.Normal circumstances should be switched primary system every month and normally move with the assurance system.The spray quench liquid gets into the tar ammonia tripping device can not produce big variation to the temperature of cyclic ammonia water.If the temperature of the heat cyclic ammonia water that the big steam sinuous coil of the amount transmission of spray quench liquid comes has regulating effect, the temperature of cyclic ammonia water is controlled at about 70 ℃.The waste water that other regional phlegma, ammoniacal liquor, tar and being difficult for is transported to WWT gets into Lower tank, is transported to the top of tar ammonia tripping device through submerged pump.Described coke-oven gas cooling of the utility model and tar ammonia tripping device, one-piece construction is simple, and is easy for operation, good stability, safety is high.Use described coke-oven gas cooling of the utility model and tar ammonia tripping device, ammoniacal liquor is cooled off by horizontal water-tube cooler after passing through and directly raw gas being sprayed cooling after interchanger cools off again.Raw gas has not only been cooled off in the direct cooling of raw gas, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in the coal gas all reduces in a large number.Advantages such as directly the cooling evaporation efficiency is high, and the gas pressure loss is little, and the capital construction cost is little.Raw gas gets into the refrigerated separation tower and realizes that at first tar ammonia separates, and the top cooling sprayer that raw gas gets into tower cools off raw gas, and spray liquid gets into the bottom tar ammonia tripping device of tower and realizes that tar ammonia separates.Raw gas gets into the refrigerated separation tower and has realized that promptly the refrigerative effect has realized the purpose of tar ammonia initial gross separation again.The cooling of the raw gas of the utility model, knockout tower with gas-liquid separator, tar slag scraper, tar ammonia separator, etc. the effect of equipment all replace.Technology simply is convenient to operation, and greatly reduces the height of horizontal water-tube cooler.The tar that the tar ammonia tripping device comes out is realized separating of ammonia water and tar oils and coke tar refuse through three ultracentrifuges, and the ammoniacal liquor of separating uses as remained ammonia.
Claims (3)
1. coke-oven gas cools off and the tar ammonia tripping device, and raw gas cooling tar separation tower (3) is a main component, it is characterized in that the upper end at raw gas cooling tar separation tower (3); Be provided with raw gas outlet (2),, be provided with raw gas inlet (19) on the side top of raw gas cooling tar separation tower (3); Side bottom at raw gas cooling tar separation tower (3); Be provided with aqueous ammonia pump of high pressure (18) and cyclic ammonia water pump (17),, be provided with the tar press pump (16) of pipe connection in the lower end of raw gas cooling tar separation tower (3); Another side bottom at raw gas cooling tar separation tower (3); Through pipe connection, be provided with ammoniacal liquor regulating tank (4), a side of ammoniacal liquor regulating tank (4) is provided with liquidometer (6); Side at remained ammonia groove (7); Be provided with cooling ammoniacal liquor return line (15); Cooling ammoniacal liquor return line (15) is provided with the cooling aqua ammonia pump; The lower end of cooling ammoniacal liquor return line (15) is connected to the plate-type heat exchanger (14) of raw gas cooling tar separation tower, and the other end of plate-type heat exchanger (14) is then through top one side of pipe connection to raw gas cooling tar separation tower (3).
2. coke-oven gas cooling according to claim 1 and tar ammonia tripping device is characterized in that in raw gas cooling tar separation tower (3), being provided with taper tower tray (1); Bottom at raw gas cooling tar separation tower (3) is connected to whizzer (5) through pipeline and tar pump A (13).
3. coke-oven gas cooling according to claim 1 and tar ammonia tripping device is characterized in that being connected to Lower tank (12) at the middle part of raw gas cooling tar separation tower (3) through pipeline and submerged pump (11); To remained ammonia groove (7), to tar groove (9), tar groove (9) back connects tar pump B (10) to whizzer (5) through another road pipe connection through one road pipe connection; Remained ammonia groove (7) back connects remained ammonia pump (8).
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012200615549U CN202440470U (en) | 2012-02-24 | 2012-02-24 | Coke oven gas cooling and tar ammonia water separating device |
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| CN2012200615549U CN202440470U (en) | 2012-02-24 | 2012-02-24 | Coke oven gas cooling and tar ammonia water separating device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103289753A (en) * | 2013-06-29 | 2013-09-11 | 济钢集团有限公司 | Novel liquid discharge device of coke oven coal gas |
| CN104232133A (en) * | 2013-06-21 | 2014-12-24 | 上海宝钢化工有限公司 | Method and device for reducing potassium and sodium ion content of coal tar |
| CN104261515A (en) * | 2014-10-16 | 2015-01-07 | 华东理工大学 | Method and device for separating tar from surplus ammonia solution |
| CN112058498A (en) * | 2020-08-26 | 2020-12-11 | 包头钢铁（集团）有限责任公司 | Fault processing method for coal gas purification electric tar precipitator |
-
2012
- 2012-02-24 CN CN2012200615549U patent/CN202440470U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104232133A (en) * | 2013-06-21 | 2014-12-24 | 上海宝钢化工有限公司 | Method and device for reducing potassium and sodium ion content of coal tar |
| CN104232133B (en) * | 2013-06-21 | 2017-05-31 | 上海宝钢化工有限公司 | Potassium, the method and device of sodium ions content in a kind of reduction coal tar |
| CN103289753A (en) * | 2013-06-29 | 2013-09-11 | 济钢集团有限公司 | Novel liquid discharge device of coke oven coal gas |
| CN104261515A (en) * | 2014-10-16 | 2015-01-07 | 华东理工大学 | Method and device for separating tar from surplus ammonia solution |
| CN112058498A (en) * | 2020-08-26 | 2020-12-11 | 包头钢铁（集团）有限责任公司 | Fault processing method for coal gas purification electric tar precipitator |
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