CN102277203B - New technology for directly cooling waste gas behind coke oven gas header and separating tar and ammonia - Google Patents
New technology for directly cooling waste gas behind coke oven gas header and separating tar and ammonia Download PDFInfo
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- CN102277203B CN102277203B CN 201110196443 CN201110196443A CN102277203B CN 102277203 B CN102277203 B CN 102277203B CN 201110196443 CN201110196443 CN 201110196443 CN 201110196443 A CN201110196443 A CN 201110196443A CN 102277203 B CN102277203 B CN 102277203B
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Abstract
The invention discloses a technology for directly cooling waste gas behind a coke oven gas header and separating tar and ammonia. A device for directly cooling waste gas behind a coke oven gas header and separating tar and ammonia comprises a taper-shaped tower tray, a waste gas outlet, a waste gas cooling tar separation tower, an ammonia regulating tank, a centrifugal machine, a liquidometer, a residual ammonia tank, a residual ammonia pump, a tar tank, a tar pump, a submerged pump, a low tank, a plate heat exchanger, a cooling ammonia pump, a tar pressing pump, a circulating ammonia pump, a high-pressure ammonia pump and a waste gas inlet, wherein the upper end of the waste gas cooling tar separation tower is provided with a waste gas outlet; the upper part of the side of the waste gas cooling tar separation tower is provided with a waste gas inlet; the lower part of the side of the waste gas cooling tar separation tower is provided with the high-pressure ammonia pump and the circulating ammonia pump; and the taper-shaped tower tray is arranged in the waste gas cooling tar separation tower. Direct cooling is adopted by the device, so that the device has the advantages of high cooling efficiency, small gas pressure loss, good integral stability, high reliability, small capital construction cost and simple technology and is convenient to operate.
Description
Technical field
The present invention relates to the cooling of coal oven dithio-gas and tar ammonia isolation technique, relate in particular to after coke oven collecting main directly cooling and tar ammonia separating technology of raw gas.
Background technology
The cooling flow process of coal gas can be divided into cooling, direct cooling and cold-three kinds of direct-cooled combination coolings indirectly.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 indirectly cooling.Coal gas indirectly cooling: spray with cyclic ammonia water at bridge tube, effuser at the raw gas that goes out carbonizing chamber and be cooled to 80～85 ℃, then partly arrive transverse pipe initial cooler through gas-liquid separator gas and raw gas is cooled to 21～23 ℃ or 25～30 ℃ in transverse pipe initial cooler, then be transported to next operation through electrical tar precipitator by gas blower.Liquid portion arrives tar ammonia water separator through tar-removing device, in tar ammonia water 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 partial impurities.An ammoniacal liquor part of separating uses another part ammoniacal liquor to arrive next operation as remained ammonia after the air-flotation type tar remover as cyclic ammonia water.Raw gas is cooling not only cooling raw gas directly, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in coal gas all reduces in a large number.The advantages such as directly cooling cooling efficiency is high, and the gas pressure loss is little, and the capital construction cost is little.The shortcoming power consumption is larger, the perishable easy obstruction of ammoniacal liquor cooling heat exchanger.Chinese patent 200610020411, a kind of method by separating tar in ammonia water by cooling coal oven dithio-gas is disclosed, step comprises: the ammoniacal liquor of the cooling raw gas formation of ammonia spray and the mixed air of raw gas are gone out the mixed solution of tar and ammoniacal liquor by gas-liquid separator separates, this mixed solution is sent into dish piece type three-phase centrifuge, utilize difference in specific gravity between ammoniacal liquor, tar and coke tar refuse and the centrifugation principle of whizzer, complete the sharp separation of ammoniacal liquor, tar and coke tar refuse.Isolated ammoniacal liquor enters oil-circulating ammonia water tank through the return line gravity flow, is used for the cooling raw gas of circulated sprinkling.Adopt three-phase centrifuge that ammonia water and tar oil is separated, can greatly accelerate oily water separation speed, shorten disengaging time, and can cancel the clarifying tank that former separation profit is used.The shortcoming power consumption is larger, cuts cyclic ammonia water little to the requirement of quality, and remained ammonia is had relatively high expectations to quality.
Summary of the invention
The object of the invention is to, overcome the deficiencies in the prior art part, directly cooling and tar ammonia separating technology of raw gas is provided after coke oven collecting main, makes the effect that synchronously realizes the cooling and tar ammonia initial gross separation of raw gas through the raw gas of effuser in the cooling tar separator of raw gas; Use low temperature ammoniacal liquor directly cooling to raw gas, guarantee cooling raw gas temperature and stability of flow; Low temperature ammoniacal liquor flushing liquor directly enters 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 be cleaned more.Remained ammonia does not need directly to use through tar-removing device again.
The direct cooling and tar ammonia separating technology of raw gas after coke oven collecting main of the present invention, after its coke oven collecting main raw gas directly cooling and tar ammonia tripping device include taper tower tray, raw gas outlet, the cooling tar separation tower of raw gas, 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 aqua ammonia pump, tar press pump, cyclic ammonia water pump, aqueous ammonia pump of high pressure and raw gas entrance composition.the cooling tar separation tower of raw gas is main component of the present invention, upper end at the cooling tar separation tower of raw gas, be provided with the raw gas outlet, side top at the cooling tar separation tower of raw gas, be provided with the raw gas entrance, side bottom at the cooling tar separation tower of raw gas, be provided with aqueous ammonia pump of high pressure and cyclic ammonia water pump, lower end at the cooling tar separation tower of raw gas, be provided with the tar press pump that pipeline connects, another side bottom at the cooling tar separation tower of raw gas, connect by pipeline, be provided with the ammoniacal liquor regulating tank, one side of ammoniacal liquor regulating tank is provided with liquidometer.In the cooling tar separation tower of raw gas, be provided with the taper tower tray.In ammoniacal liquor regulating tank one side, be provided with the plate-type heat exchanger that is connected to the cooling tar separation tower of raw gas by pipeline and cooling aqua ammonia pump, the other end of plate-type heat exchanger is connected to top one side of the cooling tar separation tower of raw gas by pipeline.In the bottom of the cooling tar separation tower of raw gas, be connected to whizzer by pipeline and tar pump A.At the middle part of the cooling tar separation tower of raw gas, be connected to Lower tank by pipeline and submerged pump.Whizzer is connected to the remained ammonia groove by one road pipeline, is connected to the tar groove by another road pipeline, connects tar pump B after the tar groove; Connect the remained ammonia pump after the remained ammonia groove.The direct cooling and tar ammonia separating technology of raw gas after coke oven collecting main of the present invention, main flow process are that the raw gas in effuser enters that raw gas is cooling, the raw gas outlet of gas part through being distributed on the taper tower tray enters water cooling tower behind the middle part of tar separation tower; Liquid portion enters the tar ammonia tripping device.The flushing liquor that spraying cooling produces directly enters the tar ammonia tripping device by the taper tower tray.The space outerpace of taper tower tray is the passage that raw gas enters refrigerating unit.The low temperature ammoniacal liquor of the cooling use of raw gas is entered low temperature ammoniacal liquor regulating tank after the low temperature aqua ammonia pump is cooling by interchanger by the ammoniacal liquor regulating tank, a plurality of overflow ports that are connected 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 enter low temperature ammoniacal liquor regulating tank from the many places, top.The ammoniacal liquor that enters low temperature ammoniacal liquor regulating tank is connected with each water distributor, and water distributor is connected with insufflation showerhead.Low temperature ammoniacal liquor regulating tank partly is looped around cooling spray and spills on tower.The very little 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, total sprinkling amount of cooling ammoniacal liquor is controlled between 10～20 m3/m2h, and the less one-level spray of amount that the larger 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 mutually vertical 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 of water-distribution nozzle use that resistance is less should not 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 24 ℃ of left and right; Winter, cooled coal gas was controlled at 22 ℃ of left and right, changes according to different processing requirement low temperature ammoniacal liquor and gas temperature owing to not needing low-temperature circulating water low temperature ammoniacal liquor can be controlled at 20～22 ℃.Cooled coal gas enters electrical tar precipitator by tower top, further removes tar removing and ammoniacal liquor in electrical tar precipitator.Spray phlegma taper tower tray is to be deep into below the liquid level of tar ammonia tripping device as the bottom that is connected with the outer wall of the cooling tar separator of raw gas, a funnel top.The lower ending opening of spray phlegma 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, be equipped with conical blast cap above the raw gas outlet.The cross-sectional area sum of raw gas outlet herein 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 affect phlegma normally enters the tar ammonia tripping device and stop up raw gas and export and just need not manage it.Regular switched system steams for a long time the tar that tower will condense on tower tray and all melts.The inside of tar ammonia tripping device is to be inverted a cone to be called the 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 taper the lay down top of plate is connected with the outer wall of tar ammonia tripping device, and the bottom is goed deep into about the inner 50cm of cone.The taper plate of laying down is connected with inner cone near the raw gas import, rest part both at a distance of the 30cm left and right.The bottom of spray phlegma taper tower tray is also lower than the about 5～10cm left and right of the height of cone.Raw gas enters the liquid portion of rear generation and sprays phlegma and just directly enters inner cone like this, and tar arrives the bottom of inner cone through precipitation, and ammoniacal liquor will arrive outer cone through the plate of laying down above through inner cone.Be equipped with snakelike steam coils in the inner cone bottom of tar ammonia tripping device and 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 is in 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 again with coke tar refuse.Solid matter is pulverized in press pump, and tar presses the amount of pulp pump very little generally in the 3-5m3/h left and right.The ammoniacal liquor regulating tank in addition that is connected with tar ammonia tripping device outer cone, the bottom of ammoniacal liquor regulating tank, middle part and top are connected with tar ammonia tripping device outer cone respectively.The ammoniacal liquor that produces when system is unstable can come with the ammoniacal liquor regulating tank adjusting of short period of time more or less the time.Need to replenish ammoniacal liquor to another system by the ammoniacal liquor regulating tank when switched system.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.Need to open bottom valve and replenish ammoniacal liquor to outer cone when liquid level is very low.Can be to another system's discharging ammoniacal liquor when liquid level is very high.The ammoniacal liquor that is used for cooling 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 enters dish piece type three-phase centrifuge by the tar pump, realizes separating of tar, coke tar refuse and ammoniacal liquor in dish piece type three-phase centrifuge.The output that the amount that enters the tar ammonia mixture of three-phase centrifuge equals the amount of remained ammonia and tar is added the amount of coke tar refuse.Control the amount of the tar ammonia mixture that enters 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 yield.Raw gas is cooling, to be two be parallel running to the tar separation tower, 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 effuser～-10pa between, the fluctuation be controlled at ± the 10pa scope in, change according to the technique different pressures.Unknown cause pressure should not be controlled and chilling spray tower internal resistance timely switched system when little within effuser occurring, timely switched system when in definite taper tower tray, hydrops is serious.Normal circumstances should be switched primary system every month and normally move with the assurance system.Spraying cooling liquid enters the tar ammonia tripping device can not produce large variation to the temperature of cyclic ammonia water.If the temperature of the heat cyclic ammonia water that the transmission of the large steam sinuous coil of the amount of spraying cooling liquid comes has regulating effect, the temperature of cyclic ammonia water is controlled at 70 ℃ of left and right.The waste water that other regional phlegma, ammoniacal liquor, tar and being difficult for is transported to sewage disposal enters Lower tank, is transported to the top of tar ammonia tripping device through submerged pump.
After coke oven collecting main of the present invention, the direct cooling and tar ammonia separating technology of raw gas, say good stability on the whole, and reliability is high.Original technology raw gas carries out gas-liquid in transverse pipe initial cooler indirectly cooling, and water coolant passes through the cooling raw gas of conduction at pipe interior.The present invention uses directly cooling method of gas-liquid, directly raw gas is carried out spraying cooling after ammoniacal liquor is cooling through interchanger.Raw gas is cooling not only cooling raw gas directly, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in coal gas all reduces in a large number.The advantages such as direct cooling cooling efficiency is high, and the gas pressure loss is little, and the capital construction cost is little.After prior art was all generally the raw gas process gas-liquid separator of coke oven, it is in primary cooler, that raw gas is cooling that gas partly enters out transverse pipe initial cooler.Liquid portion enters tar ammonia water separator and realizes that tar ammonia separates after the tar slag scraper.And technology of the present invention is: raw gas enters the refrigerated separation tower and realizes that at first tar ammonia separates, and raw gas enters the top cooling sprayer of tower, and raw gas is cooling, and spray liquid enters the bottom tar ammonia tripping device of tower and realizes that tar ammonia separates.Raw gas enters the refrigerated separation tower and has realized that namely cooling effect has realized again the purpose of tar ammonia initial gross separation.The ammoniacal liquor that cooling ammoniacal liquor separates from the tar ammonia tripping device.Raw gas of the present invention is cooling, knockout tower all replaces the effect of the equipment such as gas-liquid separator, tar slag scraper, tar ammonia water separator, transverse pipe initial cooler.The simple convenient operation of technique.
Description of drawings
Accompanying drawing 1 is the direct structural representation of the cooling tar separator of raw gas of cooling and tar ammonia separating technology of raw gas after coke oven collecting main of the present invention.The cooling tar separation tower of 1-taper tower tray, 2-raw gas outlet 3-raw gas 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 aqua ammonia pump 16-tar press pump 17-cyclic ammonia water pump 18-aqueous ammonia pump of high pressure 19-raw gas entrance.
Embodiment
referring now to accompanying drawing 1, be described as follows in conjunction with the embodiments: the direct cooling and tar ammonia separating technology of raw gas after coke oven collecting main of the present invention, after its coke oven collecting main raw gas directly cooling and tar ammonia tripping device include taper tower tray 1, raw gas outlet 2, the cooling tar separation tower 3 of raw gas, 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 aqua ammonia pump 15, tar press pump 16, cyclic ammonia water pump 17, aqueous ammonia pump of high pressure 18 and raw gas entrance 19 form.the cooling tar separation tower 3 of raw gas is main components of the present invention, upper end at the cooling tar separation tower 3 of raw gas, be provided with raw gas outlet 2, side top at the cooling tar separation tower 3 of raw gas, be provided with raw gas entrance 19, side bottom at the cooling tar separation tower 3 of raw gas, be provided with aqueous ammonia pump of high pressure 18 and cyclic ammonia water pump 17, lower end at the cooling tar separation tower 3 of raw gas, be provided with the tar press pump 16 that pipeline connects, another side bottom at the cooling tar separation tower 3 of raw gas, connect by pipeline, be provided with ammoniacal liquor regulating tank 4, one side of ammoniacal liquor regulating tank 4 is provided with liquidometer 6.In the cooling tar separation tower 3 of raw gas, be provided with taper tower tray 1.In ammoniacal liquor regulating tank 4 one sides, be provided with the plate-type heat exchanger 14 that is connected to the cooling tar separation tower 3 of raw gas by pipeline and cooling aqua ammonia pump 15, the other end of plate-type heat exchanger 14 is connected to top one side of the cooling tar separation tower 3 of raw gas by pipeline.In the bottom of the cooling tar separation tower 3 of raw gas, be connected to whizzer 5 by pipeline and tar pump A13.At the middle part of the cooling tar separation tower 3 of raw gas, be connected to Lower tank 12 by pipeline and submerged pump 11.Whizzer 5 is connected to remained ammonia groove 7 by one road pipeline, is connected to tar groove 9 by another road pipeline, the rear connection tar of tar groove 9 pump B10; Connect remained ammonia pump 8 after remained ammonia groove 7.The direct cooling and tar ammonia separating technology of raw gas after coke oven collecting main of the present invention, main flow process are that the raw gas in effuser enters that raw gas is cooling, the raw gas outlet 2 of gas part through being distributed on taper tower tray 1 enters water cooling tower behind the middle part of tar separation tower; Liquid portion enters the tar ammonia tripping device.The flushing liquor that spraying cooling produces directly enters the tar ammonia tripping device by taper tower tray 1.The space outerpace of taper tower tray 1 is the passage that raw gas enters refrigerating unit.The low temperature ammoniacal liquor of the cooling use of raw gas is entered low temperature ammoniacal liquor regulating tank after the low temperature aqua ammonia pump is cooling by interchanger by ammoniacal liquor regulating tank 4, a plurality of overflow ports that are connected 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 enter low temperature ammoniacal liquor regulating tank from the many places, top.The ammoniacal liquor that enters low temperature ammoniacal liquor regulating tank is connected with each water distributor, and water distributor is connected with insufflation showerhead.Low temperature ammoniacal liquor regulating tank partly is looped around cooling spray and spills on tower.The very little 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, total sprinkling amount of cooling ammoniacal liquor is controlled between 10～20 m3/m2h, the flow that one-level is sprayed more greatly, the amount that secondary sprays is less, the distance that one-level spray and secondary spray should be controlled between 1.5～2m.The one-level spray is mutually vertical 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 of water-distribution nozzle use that resistance is less should not 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 24 ℃ of left and right; Winter, cooled coal gas was controlled at 22 ℃ of left and right, changes according to different processing requirement low temperature ammoniacal liquor and gas temperature owing to not needing low-temperature circulating water low temperature ammoniacal liquor can be controlled at 20～22 ℃.Cooled coal gas enters electrical tar precipitator by tower top, further removes tar removing and ammoniacal liquor in electrical tar precipitator.Spray phlegma taper tower tray is to be deep into below the liquid level of tar ammonia tripping device as the bottom that is connected with the outer wall of the cooling tar separator of raw gas, a funnel top.The lower ending opening of spray phlegma 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, be equipped with conical blast cap above the raw gas outlet.The cross-sectional area sum of raw gas outlet herein 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 affect phlegma normally enters the tar ammonia tripping device and stop up raw gas and export and just need not manage it.Regular switched system steams for a long time the tar that tower will condense on tower tray and all melts.The inside of tar ammonia tripping device is to be inverted a cone to be called the 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 taper the lay down top of plate is connected with the outer wall of tar ammonia tripping device, and the bottom is goed deep into about the inner 50cm of cone.The taper plate of laying down is connected with inner cone near the raw gas import, rest part both at a distance of the 30cm left and right.The bottom of spray phlegma taper tower tray is also lower than the about 5～10cm left and right of the height of cone.Raw gas enters the liquid portion of rear generation and sprays phlegma and just directly enters inner cone like this, and tar arrives the bottom of inner cone through precipitation, and ammoniacal liquor will arrive outer cone through the plate of laying down above through inner cone.Be equipped with snakelike steam coils in the inner cone bottom of tar ammonia tripping device and 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 is in 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 again with coke tar refuse.Solid matter is pulverized in press pump, and tar presses the amount of pulp pump very little generally in the 3-5m3/h left and right.The ammoniacal liquor regulating tank in addition that is connected with tar ammonia tripping device outer cone, the bottom of ammoniacal liquor regulating tank, middle part and top are connected with tar ammonia tripping device outer cone respectively.The ammoniacal liquor that produces when system is unstable can come with the ammoniacal liquor regulating tank adjusting of short period of time more or less the time.Need to replenish ammoniacal liquor to another system by the ammoniacal liquor regulating tank when switched system.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.Need to open bottom valve and replenish ammoniacal liquor to outer cone when liquid level is very low.Can be to another system's discharging ammoniacal liquor when liquid level is very high.The ammoniacal liquor that is used for cooling 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 enters dish piece type three-phase centrifuge by the tar pump, realizes separating of tar, coke tar refuse and ammoniacal liquor in dish piece type three-phase centrifuge.The output that the amount that enters the tar ammonia mixture of three-phase centrifuge equals the amount of remained ammonia and tar is added the amount of coke tar refuse.Control the amount of the tar ammonia mixture that enters 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 yield.Raw gas is cooling, to be two be parallel running to the tar separation tower, 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 effuser～-10pa between, the fluctuation be controlled at ± the 10pa scope in, change according to the technique different pressures.Unknown cause pressure should not be controlled and chilling spray tower internal resistance timely switched system when little within effuser occurring, timely switched system when in definite taper tower tray, hydrops is serious.Normal circumstances should be switched primary system every month and normally move with the assurance system.Spraying cooling liquid enters the tar ammonia tripping device can not produce large variation to the temperature of cyclic ammonia water.If the temperature of the heat cyclic ammonia water that the transmission of the large steam sinuous coil of the amount of spraying cooling liquid comes has regulating effect, the temperature of cyclic ammonia water is controlled at 70 ℃ of left and right.The waste water that other regional phlegma, ammoniacal liquor, tar and being difficult for is transported to sewage disposal enters Lower tank, is transported to the top of tar ammonia tripping device through submerged pump.After coke oven collecting main of the present invention, the direct cooling and tar ammonia separating technology of raw gas, say good stability on the whole, and reliability is high.Original technology raw gas carries out gas-liquid in transverse pipe initial cooler indirectly cooling, and water coolant passes through the cooling raw gas of conduction at pipe interior.The present invention uses directly cooling method of gas-liquid, directly raw gas is carried out spraying cooling after ammoniacal liquor is cooling through interchanger.Raw gas is cooling not only cooling raw gas directly, and the effect that purifies coal gas is arranged, and the tar naphthalene ammonia hydrogen sulfide prussic acid in coal gas all reduces in a large number.The advantages such as direct cooling cooling efficiency is high, and the gas pressure loss is little, and the capital construction cost is little.After prior art was all generally the raw gas process gas-liquid separator of coke oven, it is in primary cooler, that raw gas is cooling that gas partly enters out transverse pipe initial cooler.Liquid portion enters tar ammonia water separator and realizes that tar ammonia separates after the tar slag scraper.And technology of the present invention is: raw gas enters the refrigerated separation tower and realizes that at first tar ammonia separates, and raw gas enters the top cooling sprayer of tower, and raw gas is cooling, and spray liquid enters the bottom tar ammonia tripping device of tower and realizes that tar ammonia separates.Raw gas enters the refrigerated separation tower and has realized that namely cooling effect has realized again the purpose of tar ammonia initial gross separation.The ammoniacal liquor that cooling ammoniacal liquor separates from the tar ammonia tripping device.Raw gas of the present invention is cooling, knockout tower all replaces the effect of the equipment such as gas-liquid separator, tar slag scraper, tar ammonia water separator, transverse pipe initial cooler.The simple convenient operation of technique.
Claims (1)
1. the direct cooling and tar ammonia separating technology of raw gas after coke oven collecting main, it is characterized in that the upper end at the cooling tar separation tower of raw gas (3), be provided with raw gas outlet (2), side top at the cooling tar separation tower of raw gas (3), be provided with raw gas entrance (19), side bottom at the cooling tar separation tower of raw gas (3), be provided with aqueous ammonia pump of high pressure (18) and cyclic ammonia water pump (17), lower end at the cooling tar separation tower of raw gas (3), be provided with the tar press pump (16) that pipeline connects, another side bottom at the cooling tar separation tower of raw gas (3), connect by pipeline, be provided with ammoniacal liquor regulating tank (4), one side of ammoniacal liquor regulating tank (4) is provided with liquidometer (6), in the cooling tar separation tower of raw gas (3), be provided with taper tower tray (1), in ammoniacal liquor regulating tank (4) one sides, be provided with the plate-type heat exchanger (14) that is connected to the cooling tar separation tower of raw gas (3) by pipeline and cooling aqua ammonia pump (15), the other end of plate-type heat exchanger (14) is connected to top one side of the cooling tar separation tower of raw gas (3) by pipeline, in the bottom of the cooling tar separation tower of raw gas (3), by pipeline and tar pump A(13) be connected to whizzer (5), spray phlegma taper tower tray is to be deep into below the liquid level of tar ammonia tripping device as the bottom that is connected with the outer wall of the cooling tar separator of raw gas, a funnel top, the lower ending opening of spray phlegma taper tower tray is provided with a plurality of raw gas outlets on the taper tower tray between 1.0～1.5 meters, be equipped with conical blast cap above the raw gas outlet, the cross-sectional area sum of raw gas outlet herein is near the cross-sectional area of raw gas import, the diameter of raw gas outlet is between 40～60cm, and the height of raw gas outlet is between 30～50cm, 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 °, the inside of tar ammonia tripping device is to be inverted a cone to be called the 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 taper the lay down top of plate is connected with the outer wall of tar ammonia tripping device, and cone inside 50cm is goed deep in the bottom, the taper plate of laying down is connected with inner cone near the raw gas import, rest part both at a distance of 30cm, the bottom of spray phlegma taper tower tray is also lower than the height 5～10cm of cone, raw gas enters the liquid portion of rear generation and sprays phlegma and just directly enters inner cone like this, and tar arrives the bottom of inner cone through precipitation, and ammoniacal liquor will arrive outer cone through the plate of laying down above through inner cone, be equipped with snakelike steam coils in the inner cone bottom of tar ammonia tripping device and 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 is at 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110196443 CN102277203B (en) | 2011-07-14 | 2011-07-14 | New technology for directly cooling waste gas behind coke oven gas header and separating tar and ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110196443 CN102277203B (en) | 2011-07-14 | 2011-07-14 | New technology for directly cooling waste gas behind coke oven gas header and separating tar and ammonia |
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| CN103060016B (en) * | 2013-01-18 | 2014-03-19 | 内蒙古乌拉山化肥有限责任公司 | Method for removing tar in process of producing synthetic ammonia by oxygen-enriched gas-producing and gas-making furnace |
| CN105381648A (en) * | 2015-12-19 | 2016-03-09 | 太原重工股份有限公司 | Tar ammonia separation system and tar ammonia separation method |
| CN105623745A (en) * | 2016-01-25 | 2016-06-01 | 神木县三江煤化工有限责任公司 | Raw coal gas purification circulating device and method |
| CN106281475A (en) * | 2016-09-09 | 2017-01-04 | 新疆广汇中化能源技术开发有限公司 | Raw coke oven gas dust arrester |
| CN108168642A (en) * | 2018-01-31 | 2018-06-15 | 锦州中科制管有限公司 | A kind of aperture measurement of gas flow device and its measuring method |
| CN109630430A (en) * | 2018-12-04 | 2019-04-16 | 山西焦化股份有限公司 | A kind of devices and methods therefor extending aqueous ammonia pump of high pressure service life |
| CN110903863A (en) * | 2019-12-23 | 2020-03-24 | 中冶焦耐(大连)工程技术有限公司 | Primary cooling process and device adopting circulating ammonia water for refrigeration |
| CN112850945A (en) * | 2020-12-25 | 2021-05-28 | 上海泽玛克敏达机械设备有限公司 | Dust-containing phenol water separation process and separation method |
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| DE2436577C3 (en) * | 1974-07-30 | 1980-08-28 | Verfahrenstechnik Dr.-Ing. Kurt Baum, 4300 Essen | Device for the separation of the termebels remaining in the coke oven gas after it has been cooled and condensed |
| GB1497107A (en) * | 1975-10-13 | 1978-01-05 | Uniroyal Ltd | Expansion joints and dredging sleeves |
| CN2540398Y (en) * | 2002-04-29 | 2003-03-19 | 辽宁华荣冶金石化设备有限公司 | Cylindrical spray saturator |
| CN101029246A (en) * | 2006-03-02 | 2007-09-05 | 攀枝花新钢钒股份有限公司 | Method for separating tar from ammonia water by cooling coal oven dithio-gas |
| CN101037602B (en) * | 2007-04-20 | 2011-05-25 | 武汉钢铁(集团)公司 | Gas transverse pipe initial cooler for coking oven |
| CN102120937A (en) * | 2010-01-07 | 2011-07-13 | 上海宝钢化工有限公司 | Purification method of coke oven gas matched with vacuum carbonate desulphurization |
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