CN104190389A - Thermal regeneration method and device of activated carbon - Google Patents
Thermal regeneration method and device of activated carbon Download PDFInfo
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- CN104190389A CN104190389A CN201410427474.4A CN201410427474A CN104190389A CN 104190389 A CN104190389 A CN 104190389A CN 201410427474 A CN201410427474 A CN 201410427474A CN 104190389 A CN104190389 A CN 104190389A
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Abstract
The invention provides a thermal regeneration method of activated carbon. The method comprises the steps of (1) transferring activated carbon which adsorbs pollutants including sulfur oxide, nitrogen oxide and dioxin in an adsorption tower of a dry process desulphurization and denitration device into an activated carbon analysis tower from the bottom of the adsorption tower, wherein the desulphurization and denitration device comprises the activated carbon adsorption tower and the activated carbon analysis tower; and (2) carrying out heat exchange on the activated carbon and heating gas in the analysis tower to enable the activated carbon to be heated up to the activated carbon regeneration temperature T1 to enable the activated carbon to be analyzed and regenerated at the temperature T1, wherein the heating gas is high temperature flue gas G1 coming from one or two bellows at the tail of a sintering machine, or hot air G2 formed by indirect heat exchange between air with room temperature and the high temperature flue gas G1 coming from the one or two bellows at the tail of the sintering machine. The invention also provides a regeneration device of activated carbon.
Description
Technical field
The present invention relates to hot renovation process and the device thereof of active carbon in the dry desulfurization that comprises activated carbon adsorber and Analytic Tower, denitrification apparatus and technique, more particularly, relate to and utilize the high-temperature flue gas of sintering machine to the charcoal absorption desulfurization (SO from flue gas or waste gas (the especially sinter fume of the sintering machine of steel and iron industry)
2), denitration (NO
x) active carbon in technique carries out the method for heat regeneration, belongs to environmental protection and energy saving field, i.e. the process field of sinter fume.
Background technology
For industrial smoke, especially for the sintering device flue gas of steel and iron industry, adopt and comprise that desulphurization and denitration device and the technique of activated carbon adsorber and Analytic Tower (or regenerator) are more satisfactory.Activated carbon desulfurization have desulfurization degree high, can realize denitration, Tuo bioxin, dedusting simultaneously, do not produce the advantages such as waste water and dregs, be extremely promising flue gas purifying method.Active carbon can at high temperature be regenerated, in temperature during higher than 350 DEG C, be adsorbed on the pollutant generation fast resolvings such as oxysulfide on active carbon, nitrogen oxide, dioxin or decomposition (sulfur dioxide is resolved, nitrogen oxide He bioxin be decomposed).And along with the rising of temperature, the reproduction speed of active carbon is further accelerated, recovery time shortens, preferably in general control Analytic Tower, regenerating active carbon temperature approximates 400 DEG C, therefore, desirable resolution temperature (or regeneration temperature) be for example 390-430 DEG C of scope, more preferably 400-420 DEG C of scope.
As shown in Figure 1, the Analytic Tower (or regenerator) that available technology adopting structure is similar to shell and tube heat exchanger carries out parsing, the regeneration of active carbon, active carbon enters from the top of tower, arrive the bottom of tower via tube side, and enter from a side for the heated air of heat activated charcoal, via shell side, from opposite side output, wherein active carbon and heated air are carried out heat exchange and are heated to regeneration temperature.For active carbon in Analytic Tower being heated up and remaining on 400 DEG C of left and right, general burning blast furnace gas or the coke-stove gas Heating Cyclic hot blast of adopting, the hot blast temperature that makes to enter Analytic Tower is 400-450 DEG C, in Analytic Tower, hot blast and active carbon carry out heat exchange, active carbon temperature rise to 400 DEG C left and right, heated air temperature is down to 300 DEG C of left and right.
On the other hand, in the sintering machine of steel and iron industry, the heat of flue gas or waste gas is not used appropriately, and the efficiency of utilization is lower, and economic worth is not high.Flue-gas temperature in two bellows of sintering machine afterbody is generally 380～450 DEG C, preferred 420-450 DEG C, if be not used, and discharge after can mixing with lower temperature flue gas in the anterior bellows of sintering machine, 90～180 DEG C of exhaust temperatures.
Utilize blast furnace gas or coke-stove gas that hot blast is heated to approximately 400 DEG C (temperature difference of approximately 100 DEG C) from 300 DEG C and need to consume a large amount of energy medium, if can use other useless high-temperature gases to replace blast furnace gas or coke-stove gas as heat medium, can realize used heat utilization, save the energy simultaneously.
Summary of the invention
At the dry desulfurization that comprises activated carbon adsorber and Analytic Tower of the present invention, in denitrification apparatus and technique, in adsorption tower, from sinter fume, adsorb and comprised oxysulfide, nitrogen oxide and dioxin are transferred in the thermal treatment zone of active carbon Analytic Tower at the active carbon of interior pollutant, active carbon and heated air G in the thermal treatment zone of Analytic Tower (as the hot-air of 400-500 DEG C or hot blast G2 or high-temperature flue gas G1) carry out indirect heat exchange and are heated (or intensification) to for example temperature of 390-480 DEG C of scope, active carbon is resolved conventionally at this temperature, regeneration.Wherein Analytic Tower (or regenerator) has the thermal treatment zone on top and the cooling zone of optional bottom.Conventionally, the described thermal treatment zone has shell pipe type heat exchanger structure.Equally, described cooling zone also has shell pipe type heat exchanger structure.Active carbon is respectively via the tube side of the tube side of the thermal treatment zone and optional cooling zone, and heated air or high-temperature flue gas in the thermal treatment zone via shell side, cooling air in cooling zone via shell side.
Present inventor surprisingly finds, flue gas in two bellows of afterbody of the sintering machine of steel and iron industry or waste gas 380～450 DEG C, preferably 420-450 DEG C of temperature mated with parsing, regeneration temperature in active carbon Analytic Tower very much, that is to say, sintering machine afterbody high-temperature flue gas is suitable as thermal source and heats the active carbon in Analytic Tower (or regenerator) very much.
According to the first embodiment of the present invention, provide a kind of hot renovation process of active carbon, the method comprises:
1) active carbon that has adsorbed the pollutant including oxysulfide, nitrogen oxide and dioxin in the activated carbon adsorber of desulphurization and denitration device from flue gas or sinter fume is transferred to the thermal treatment zone of active carbon Analytic Tower from the bottom of adsorption tower, wherein desulphurization and denitration device comprises activated carbon adsorber and Analytic Tower; With
2) in the thermal treatment zone of Analytic Tower, active carbon carries out indirect heat exchange and is heated or is warming up to regenerating active carbon temperature (or active carbon resolution temperature) T1 with the heated air in the input thermal treatment zone, causes active carbon to resolve, regenerate at this T1 temperature;
It is characterized in that, the heated air in the input thermal treatment zone is: (a) for example, from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C); (b) in heat exchanger, carry out the indirect heat exchange hot-air G2 (for example 410～445 DEG C) that institute forms or heats up afterwards by normal temperature air and for example, from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C); Or (c) between heat exchanger and the thermal treatment zone of Analytic Tower circulation (preferably adopting closed circulation or closed circulation) and in heat exchanger with for example, having carried out from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C) after indirect heat exchange the hot-air G2 (for example 410～445 DEG C) heating up.
More than in (c) situation, for the air (or hot blast) circulating between heat exchanger and the thermal treatment zone of Analytic Tower, it is from the heated air outlet output of the thermal treatment zone, again turns back to the heated air import of the thermal treatment zone by carry out indirect heat exchange in heat exchanger after heating up.That is to say, heated air be by that indirect heat exchange is lowered the temperature by carrying out in the thermal treatment zone of Analytic Tower with active carbon, from the heated air of the thermal treatment zone of Analytic Tower export the air (or hot blast) flowing out be transported to heat exchanger with the hot-air G2 that carries out from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine again heating up and forming after indirect heat exchange.In this case, circulate between heat exchanger and the thermal treatment zone of Analytic Tower as the hot-air of heated air., in the thermal treatment zone of Analytic Tower, carried out indirect heat exchange lowers the temperature with active carbon, export the cooling air or the cooling hot blast G2 (280-350 DEG C that flow out from the heated air of the thermal treatment zone of Analytic Tower, approximately 320 DEG C) be conventionally transported in heat exchanger and for example, from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C) and carry out again heating up after indirect heat exchange, become the hot-air G2 (for example 410～445 DEG C) of high temperature, the latter be transported to Analytic Tower the thermal treatment zone heated air import and enter into the thermal treatment zone, make to circulate between heat exchanger and the thermal treatment zone of Analytic Tower as the hot-air G2 of heated air.
For example, if sintering machine afterbody flue-gas temperature is suitable, adopt above (a) scheme, if sintering machine afterbody flue-gas temperature is too high, convert some cold wind or employing scheme (b).
Such scheme (c) is optimum embodiment of the present invention.Heat utilization most effective, operate the simplest, the easily operation of control system, and environmental protection more.Compared with mode (b), energy-conservation highly significant, recirculated hot air only need be warmed up to a little suitable temperature and just can return in the thermal treatment zone and recycle.
Here said " one or two bellows of afterbody " refer to last of afterbody or last of afterbody and the penultimate bellows at sintering machine.The temperature of one or two bellows of sintering machine afterbody is the highest often.The particularly important is SO in the flue gas extracting in one or two bellows of sintering machine afterbody
2concentration obviously reduces.Meanwhile, the temperature of the flue gas extracting from one or two bellows of sintering machine afterbody, usually above 400 DEG C, may be low to moderate 390 DEG C or even 380 DEG C winter, and therefore, after being introduced in adsorption tower, it is also little for the corrosiveness of adsorption tower.Because higher than 380 DEG C in the situation that the water of vapor form cannot with SO
2form sulfurous acid, or cannot with SO
2and O
2both react formation sulfuric acid.
In general, regenerating active carbon temperature T 1 is at 390-500 DEG C, preferably 400-470 DEG C, and more preferably 405-450 DEG C, more preferably at 410-440 DEG C, the more preferably scope of 410-430 DEG C.
Generally, the flue gas G1 or the hot-air G2 that are transfused in the thermal treatment zone as heated air have 380～500 DEG C, and preferably 390～480 DEG C, more preferably 400-470 DEG C, more preferably 410-460 DEG C, the preferably temperature of 420-450 DEG C, as 430 DEG C or 440 DEG C.
Conventionally, high-temperature flue gas G1 or hot-air G2 its temperature after for active carbon Analytic Tower heat activated charcoal can reduce, for example, be reduced to temperature T 2 (be generally 280-350 DEG C, be preferably 290-330 DEG C, 300 DEG C according to appointment, 310 DEG C or 320 DEG C).Preferably, the flue gas (or being called the flue gas after flue gas or the heat exchange after cooling) of lower the temperature (having temperature T 2) returns in the flue collector of sintering machine with active carbon heat exchange.And active carbon is heated to 415 DEG C of left and right in Analytic Tower
Preferably, when input the thermal treatment zone in before heated air (for example G1, as shown in Figure 2; Or G2, temperature as shown in Figure 3) during lower than regenerating active carbon temperature T 1, utilized other heating source to heat the high-temperature flue gas G1 as heated air or hot-air G2 before heated air enters into Analytic Tower; Preferably, high-temperature flue gas G1 or hot-air G2 are heated, make its temperature be increased to high 5-40 DEG C of specific activity charcoal regeneration temperature T1, preferred high 7-30 DEG C, more preferably 8-20 DEG C, the more preferably temperature of 10-15 DEG C.For example, when the temperature of the high-temperature flue gas G1 in one or two bellows of the afterbody from sintering machine is during lower than regenerating active carbon temperature (or active carbon resolution temperature) T1, enter into before Analytic Tower (its thermal treatment zone) and utilize other heating source to heat high-temperature flue gas G1 at this flue gas G1, make its temperature be increased to high 5-40 DEG C of specific activity charcoal regeneration temperature T1, preferred high 7-30 DEG C, more preferably 8-20 DEG C, the more preferably temperature of 10-15 DEG C.Preferably, heating source is heating furnace, and for example burn blast furnace gas or coke-stove gas of this heating furnace for example, heats heated air (G1 or G2).
When in the operation at Analytic Tower with heating furnace come in advance to heated air (for example G1, as shown in Figure 2, or G2, while intensification as shown in Figure 3), in the case of combustion air being input to the air inlet of the combustion chamber in heating furnace by combustion fan, blast furnace gas or coke-stove gas (optionally flow through an other heat exchanger is preheated after) are transfused in the combustion chamber of heating furnace and burn, then: the high-temp waste gas of (I) discharging from combustion chamber or high-temperature hot-air (Ga) (for example have 1100-1900 DEG C, preferably 1300-1600 DEG C) equalizing section flowing through heating furnace afterbody (or is called mixing, buffering area) and flow out with from heat exchanger (14) after the hot blast G2 in this region of input mix or mix and be conditioned temperature (for example, to 400-460 DEG C with the high-temperature flue gas G1 in one or two bellows of afterbody from sintering machine, preferably 400-450 DEG C, more preferably 410-430 DEG C), thereby become and there is for example 400-460 DEG C (preferably 400-450 DEG C, more preferably 410-430 DEG C) hot blast (Gb), then, this hot blast Gb is transported to the hot-wind inlet of the thermal treatment zone of Analytic Tower via pipeline as heated air, or
(II) high-temp waste gas of discharging from combustion chamber or high-temperature hot-air (Ga) (for example have 1100-1900 DEG C, preferably 1300-1600 DEG C) flow through temperature regulated zone of heating furnace afterbody and with (II) with from heat exchanger (14), flow out after input this region hot blast G2 carry out indirect heat exchange in case the temperature of this hot blast G2 that further raises (for example, to 400-460 DEG C, preferably 400-450 DEG C, more preferably 410-430 DEG C), then, this hot blast G2 heating up is transported to the hot-wind inlet of the thermal treatment zone of Analytic Tower via pipeline as heated air.
Conventionally by cooling blower, normal temperature air (as cooling air or cooling-air) is passed into the cooling zone of Analytic Tower from the cold air inlet of Analytic Tower cooling zone, carry out indirect heat exchange with the active carbon moving down to coolingly there is the active carbon that pyrolysis is analysed in cooling zone, and in cooling zone, carry out heat exchange with active carbon and the cooling air that heats up from the cooling air outlet output of the cooling zone of Analytic Tower, become the cooling air (for example 90-120 DEG C, 100 DEG C according to appointment) of intensification.The cooling air (about 90-120 DEG C, as 100 DEG C) of preferably, discharging from the refrigerating gas outlet of the cooling zone of Analytic Tower substitutes above-described normal temperature air.
More preferably, cooling air ((the about 90-120 DEG C that the cooling air outlet of the cooling zone from Analytic Tower is discharged, as 100 DEG C)) guide to and the air inlet of the matching used combustion fan of heating furnace, sent into the air inlet of the combustion chamber of heating furnace by combustion fan.Therefore, the waste heat of outer row's cold wind (for example 90-120 DEG C, 100 DEG C according to appointment) of the outer thermal wind exhausting of the thermal treatment zone (280-350 DEG C, approximately 320 DEG C) and cooling zone is all utilized.
Preferably, in Analytic Tower or heat exchanger, experience high-temperature flue gas after heat exchange and be back to the flue collector of sintering machine.For example turn back to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
Analytic Tower of the present invention is regenerator or the Analytic Tower for the desulphurization and denitration device of the exhaust-gas treatment of steel and iron industry, conventionally has 15-45 rice, preferably 20-40 rice, the more preferably tower height of 25-35 rice.In addition, Analytic Tower or its main part have 6-100 rice
2, preferred 8-50 rice
2, more preferably 10-30 rice
2, further preferably 15-20 rice
2body cross-section long-pending.And (desulphurization and denitration) adsorption tower in desulfuring and denitrifying apparatus has larger size conventionally, the tower height of for example adsorption tower is 20-60, preferably 22-50, more preferably 25-45 rice.
For sintering machine in steel and iron industry, its total length is generally 20-120 rice, preferably 40-100 rice, more preferably 60-80 rice.
Second embodiment according to the present invention, based on above-mentioned first embodiment, also provides the desulphurization and denitration method of sinter fume, and the method comprises:
1), sinter fume is transported in a kind of activated carbon adsorber of desulphurization and denitration device that comprises activated carbon adsorber and Analytic Tower, contact with the active carbon of the top input from adsorption tower, make pollutant including oxysulfide, nitrogen oxide and dioxin by charcoal absorption; With
2) active carbon that has adsorbed the pollutant including oxysulfide, nitrogen oxide and dioxin is transferred to the thermal treatment zone of active carbon Analytic Tower from the bottom of adsorption tower; With
3) in the thermal treatment zone of Analytic Tower, active carbon carries out indirect heat exchange and is heated or is warming up to regenerating active carbon temperature T 1 with the heated air in the input thermal treatment zone, causes active carbon to resolve, regenerate at this T1 temperature;
It is characterized in that, the heated air in the input thermal treatment zone is: (a) for example, from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C); (b) in heat exchanger, carry out the indirect heat exchange hot-air G2 (for example 410～445 DEG C) that institute forms or heats up afterwards by normal temperature air and for example, from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C); Or (c) between heat exchanger and the thermal treatment zone of Analytic Tower circulation (preferably adopting closed circulation or closed circulation) and in heat exchanger with for example, having carried out from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine (420～450 DEG C) after indirect heat exchange the hot-air G2 (for example 410～445 DEG C) heating up.
In general the active carbon that, has adsorbed pollutant in above step (2) is transferred to the thermal treatment zone of a kind of active carbon Analytic Tower with the thermal treatment zone on top and the cooling zone of bottom from the bottom of adsorption tower.
In the thermal treatment zone of Analytic Tower, active carbon and heated air are carried out heat exchange and are heated (or intensification) to the temperature of for example 390-450 DEG C (as 430 DEG C) scope, and active carbon is conventionally resolved, regenerated at this temperature.
In the present invention, according to the control of sintering end point, the temperature peak of flue gas G1 generally appears at some in two bellows of afterbody in sintering machine wind box.Flue-gas temperature in two bellows of sintering machine afterbody is generally 380～450 DEG C, if be not used, and discharge after can mixing with lower temperature flue gas in the anterior bellows of sintering machine, 90～180 DEG C of exhaust temperatures.
Flue-gas temperature difference in two bellows of sintering machine afterbody, selects flue gas (high-temperature flue gas) that temperature is higher as heating activated carbon medium in Analytic Tower, and the flue gas that temperature is lower is closed the baffle door on its pipeline.High-temperature flue gas by blower fan, in heating furnace causes Analytic Tower indirect tower active carbon, the high-temperature flue gas after heat exchange is back to sintering flue collector.
Judge whether to utilize heating furnace to heat high-temperature flue gas according to the temperature at Analytic Tower smoke inlet place.If Analytic Tower entrance flue gas temperature is higher than the flue gas of 400 DEG C, without the flue gas of heating that heating furnace is lighted a fire, high-temperature flue gas can directly enter Analytic Tower heat activated charcoal; If Analytic Tower entrance flue gas temperature, lower than the flue gas of 400 DEG C, needs heating furnace to light a fire, burning blast furnace gas or coke-stove gas heat high-temperature flue gas, make it be warming up to 400 DEG C of left and right, the amplitude that now flue-gas temperature raises is 10～40 DEG C (having considered the heat loss of high-temperature flue gas transfer pipeline), far below the temperature difference compensation of 100 DEG C.
Third embodiment according to the present invention, provides a kind of active carbon resolver or a kind of active carbon resolver for said method, and it comprises:
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the flue gas blower fan (7) of the hot flue gas of conveying of (gas circuit) upstream of heating furnace (4);
Combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Second pipeline (L2) of supplied flue gases, wherein flue gas blower fan (7) is positioned between the leading portion and back segment of this second pipeline (L2), the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), be communicated on first pipeline (L1) of heating furnace (4) afterbody downstream the downstream of the 3rd optional valve (V3) (or) via optional the second valve (V2) with the second branch road (L10),
Air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4);
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4); With
The 3rd pipeline (L3), for from the thermal treatment zone heated air outlet of (2) discharge heated air, its one end is connected to the heated air outlet of the thermal treatment zone (2).
Preferably, the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, be connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
According to the 4th embodiment of the present invention, a kind of active carbon resolver or a kind of active carbon resolver for said method are provided, it comprises:
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the heat exchanger (14) (for example shell and tube exchanger) of (gas circuit) upstream of heating furnace (4);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Carry second pipeline (L2) of hot flue gas, the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is connected to the import of the exhaust gases passes of heat exchanger (14);
For discharging the 3rd pipeline (L3) of flue gas, its one end is connected to the outlet of the exhaust gases passes of heat exchanger (14);
For exporting the 4th pipeline (L4) of hot blast, its front end is connected with the heated air outlet of the thermal treatment zone (2), and its rear end is communicated to the hot blast of heat exchanger (14) or the import of air duct via optional the 4th valve (V4);
For delivery of the 6th pipeline (L6) of hot blast, its front end is communicated to the import of air or the circulating air passage of heat exchanger (14), and its rear end is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), and the second branch road (L10) is communicated on first pipeline (L1) in the downstream of the 3rd optional valve (V3) via optional the second valve (V2);
Flue gas blower fan (7), it is positioned between the leading portion and back segment of this second pipeline (L2);
Optional combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
Optional air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4); With
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4).
Preferably, a circulating fan (17) is installed in pipeline L6.
In addition, said apparatus further comprises: for the 5th pipeline (L5) of input air, it is communicated to the import of air or the circulating air passage of heat exchanger (14) via optional the 5th valve (V5).
Preferably, the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, be connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
For design and the absorbing process thereof of flue gas (or waste gas) adsorption tower, in prior art, there are a lot of documents to disclose, referring to for example US5932179, JP2004209332A, and JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A.The application is no longer described in detail.
In the present invention, there is no special requirement for Analytic Tower, the Analytic Tower of prior art all can be used in the present invention.Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type (or package type), wherein active carbon is inputted from tower top, flow through the downwards tube side of the thermal treatment zone, top, then arrive a cushion space between the thermal treatment zone, top and cooling zone, bottom, then the flow through tube side of cooling zone, bottom, then at the bottom of arriving tower, the flow through shell side of the thermal treatment zone of heated air (or high-temperature flue gas), heated air (or high-temperature flue gas, 400-450 DEG C) enter from a side of the thermal treatment zone of Analytic Tower, carry out indirect heat exchange and lower the temperature with the active carbon of the thermal treatment zone tube side of flowing through, then from the opposite side output of the thermal treatment zone of tower.Cooling air enters from a side of the cooling zone of Analytic Tower, carries out indirect heat exchange with the active carbon of resolving, regenerating of the cooling zone tube side of flowing through.After indirect heat exchange, cooling air is warming up to 90-130 DEG C (100 DEG C according to appointment).
For design and the regeneration method of active carbon of active carbon Analytic Tower, in prior art, there are a lot of documents to disclose, JP3217627B2 (JPH08155299A) discloses a kind of regenerator (being desorber), it adopts double seal valve, logical noble gas sealing, screening, water-cooled (referring to the Fig. 3 in this patent).JP3485453B2 (JPH11104457A) discloses regenerator (referring to Figure 23 and 24), can adopt preheating section, double seal valve, logical noble gas, the cooling or water-cooled of air.JPS59142824A discloses gas from cooling section for preheating active carbon.Chinese patent application 201210050541.6 (Shanghai Ke Liu company) discloses the scheme of the energy recycling of regenerator, has wherein used drier 2.JPS4918355B discloses employing blast furnace gas (blast furnace gas) and has carried out regenerated carbon.JPH08323144A discloses the regenerator of employing fuel (heavy oil or light oil), uses air-heating furnace (referring to Fig. 2 of this patent, 11-hot-blast stove, 12-fuel supply system).China's utility model 201320075942.7 relates to heater and possesses the emission-control equipment of this heater (coal-fired, air heat), referring to the Fig. 2 in this utility model patent.
" optional " represents to be with or without in this application.Analytic Tower and regenerator are used interchangeably.Regeneration is used interchangeably with parsing.In addition, resolving with desorb is identical concept.
Advantage of the present invention or useful technique effect
1,380～450 DEG C of the flue gas in two bellows of afterbody of the sintering machine of steel and iron industry or waste gas, preferably 420-450 DEG C of temperature for example, mated with parsing, regeneration temperature (390-430 DEG C) in active carbon Analytic Tower very much, therefore, sintering machine afterbody high-temperature flue gas is suitable as thermal source and heats the active carbon in Analytic Tower (or regenerator) very much.In the time that EGT is slightly high, can directly use, therefore, technological operation and control seem very convenient.Even if or EGT is slightly lower than needed regeneration temperature, only needs the temperature of little heat rising waste gas to use.
2, the contained used heat of waste gas is used, and causes having saved the energy.
3, compared with the regeneration technology of prior art, reduce the use of the energy, reduce significantly the cost of technique.
4, for the supply of regeneration thermal source, as large-scale gas furnace, reduce equipment investment and operation, maintenance cost without the larger heat generator of construction scale.
Brief description of the drawings
Fig. 1 is the regeneration technology schematic flow sheet of the regenerator of prior art.
Fig. 2 is the regeneration technology of regenerator of the present invention or Analytic Tower or resolves process flow diagram.
Fig. 3 is the regenerator of employing heat exchanger of the present invention or the regeneration technology of Analytic Tower or resolves process flow diagram.
Reference numeral: 1, Analytic Tower; 2, the thermal treatment zone; 3, sintering machine; 4, heating furnace; The heated air of 5, arranging from the thermal treatment zone is as the flue gas of heating use; 6, flue gas pre-processing device (deduster); 7, flue gas blower fan; 8, valve; 9, cooling zone; 10, bellows; 11, combustion fan; 12, air stream; 13, coal gas basin or gaspipe line; 14, heat exchanger; 15: active carbon to be regenerated; 16: the active carbon of regeneration; 17: circulating fan; L1-L11: pipeline; V1-V6: valve.
Fig. 4 is the schematic diagram of the desulfuring and denitrifying apparatus that comprises adsorption tower and Analytic Tower of the present invention.
Wherein 20: reaction tower (being adsorption tower); 201: active carbon bed; 202: former flue gas; 203: clean flue gas; 204: active carbon entrance; 205: active carbon outlet; 206: ammonia; 207: ammonia valve; 30: active carbon feed bin; 40: vibratory sieve; 401: dust; 501,502: active carbon conveying mechanism; A: inlet plenum; B: discharge chamber.
Fig. 5 is the multistage spray another kind of reaction tower of ammonia or the schematic diagram of adsorption tower (20) with three active carbon beds (201a, 201b, 201c) of the present invention.
Wherein, 20: reaction tower (being adsorption tower); 201a, 201b, 201c: active carbon bed; 202: former flue gas; 203: clean flue gas; 204: active carbon entrance; 204a: active carbon material feeding valve; 205: active carbon outlet; 205b: active carbon blowdown valve; 206: ammonia; 206a: air or hot-air; 207: ammonia valve (V1, V2, V3); 208: spray ammonia pipe array; A: inlet plenum; B: discharge chamber.
Fig. 6 is the another kind of reaction tower of double tower type or the schematic diagram of adsorption tower (20) (being many beds of multitower type) that each tower of the present invention has 5 active carbon beds (a, b, c, d, e) separately.
Fig. 7 is the schematic diagram of another kind of many beds of multitower type reaction tower of the present invention or adsorption tower (20).Wherein the tower body of activated carbon adsorber has the multiple field chamber structure (many beds) being parallel to each other in vertical direction, that is, and and left side discharge chamber B-bed c-bed b-bed a-A inlet plenum-bed a-bed b-bed c-right side discharge chamber B.
Fig. 8 is the air inlet of reaction tower (or adsorption tower) and gas outlet at the design diagram of homonymy (top view) not.
Fig. 9 is the air inlet of reaction tower (or adsorption tower) and the gas outlet design diagram (top view) in the same side.
Concrete embodiment
In order to be illustrated more clearly in the present invention, below in embodiment referring to figs. 2 and 3 describing device of the present invention and various technique.
Referring to Fig. 2 or Fig. 3, the active carbon resolver using is in an embodiment as described below:
A kind of active carbon resolver, it comprises:
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the flue gas blower fan (7) of the hot flue gas of conveying of (gas circuit) upstream of heating furnace (4);
Combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Second pipeline (L2) of supplied flue gases, wherein flue gas blower fan (7) is positioned between the leading portion and back segment of this second pipeline (L2), the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), be communicated to via optional the second valve (V2) on first pipeline (L1) in downstream at heating furnace (4) the afterbody downstream of the 3rd valve (V3) (or) with the second branch road (L10),
Air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4);
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4); With
The 3rd pipeline (L3), for from the thermal treatment zone heated air outlet of (2) discharge heated air, its one end is connected to the heated air outlet of the thermal treatment zone (2).
Preferably, the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, be connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
In addition, can use another active carbon resolver, it comprises:
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the heat exchanger (14) (for example shell and tube exchanger) of (gas circuit) upstream of heating furnace (4);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Carry second pipeline (L2) of hot flue gas, the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is connected to the import of the exhaust gases passes of heat exchanger (14);
For discharging the 3rd pipeline (L3) of flue gas, its one end is connected to the outlet of the exhaust gases passes of heat exchanger (14);
For exporting the 4th pipeline (L4) of hot blast, its front end is connected with the heated air outlet of the thermal treatment zone (2), and its rear end is communicated to the hot blast of heat exchanger (14) or the import of air duct via optional the 4th valve (V4);
For delivery of the 6th pipeline (L6) of hot blast, its front end is communicated to the import of air or the circulating air passage of heat exchanger (14), and its rear end is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), be communicated to via optional the second valve (V2) on first pipeline (L1) in downstream at heating furnace (4) the afterbody downstream of the 3rd optional valve (V3) (or) with the second branch road (L10),
Flue gas blower fan (7), it is positioned between the leading portion and back segment of this second pipeline (L2);
Optional combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
Optional air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4); With
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4).
Preferably, a circulating fan (17) is installed in pipeline L6.
In addition, as another scheme, said apparatus also comprises: for the 5th pipeline (L5) of input air, it is communicated to the import of air or the circulating air passage of heat exchanger (14) via optional the 5th valve (V5).
Preferably, the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, be connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
Embodiment 1
As shown in Figure 4, desulphurization and denitration device comprises activated carbon adsorber (20) (30 meters of tower heights, cross-sectional area 120m
2) and Analytic Tower (25 meters of tower heights, cross-sectional area 16m as shown in Figure 2,
2).The tower body (referring to Fig. 7) of activated carbon adsorber has the multiple field chamber structure being parallel to each other in vertical direction,, left side c ← desulphurization and denitration chamber, discharge chamber B ← denitration chamber b ← desulfurization chamber a ← inlet plenum A → desulfurization chamber a → desulphurization and denitration chamber b → denitration chamber c → right side discharge chamber B, wherein flue gas inlet plenum A from the inside along left and right direction essentially horizontally outward flow (to B discharge chamber).In order to draw conveniently, the reaction tower (or adsorption tower) in Fig. 4 is depicted single tower reaction tower as, but in fact replaces the adsorption tower in Fig. 4 by the reaction tower (or adsorption tower) of Fig. 7 in the present embodiment 1.
Analytic Tower has the thermal treatment zone (2) on top and the cooling zone (9) of bottom.
Pending sinter fume is transported in a kind of activated carbon adsorber of desulphurization and denitration device that comprises activated carbon adsorber and Analytic Tower, contact with the active carbon of the top input from adsorption tower, make pollutant including oxysulfide, nitrogen oxide and dioxin by charcoal absorption, the active carbon that has adsorbed pollutant is transferred to the thermal treatment zone (2) of a kind of active carbon Analytic Tower with the thermal treatment zone (2) on top and the cooling zone (9) of bottom from the bottom of adsorption tower.
In the thermal treatment zone (2) of Analytic Tower (or regenerator), active carbon and heated air are carried out indirect heat exchange and are heated or are warming up to regenerating active carbon temperature or active carbon resolution temperature T1=410 DEG C, cause active carbon to resolve, regenerate at 410 DEG C of temperature;
Wherein, heated air is from the high-temperature flue gas G1 (=446 DEG C) in last bellows of afterbody of sintering machine:
446 DEG C of flue-gas temperatures in last bellows of sintering machine afterbody, air quantity 28000Nm
3/ h; 420 DEG C of flue-gas temperatures in penultimate bellows, air quantity 30000Nm
3/ h.Select high-temperature flue gas in last bellows of sintering machine afterbody to resolve thermal source as active carbon, as above-mentioned heated air.The ability that Analytic Tower is processed active carbon is 5t/h, by the adjusting of blower fan and valve, makes the interior high-temperature flue gas of last bellows of sintering machine afterbody with 16000Nm
3the flow of/h enters Analytic Tower, and due to the heat radiation on flue gas delivery pipe road, Analytic Tower porch flue-gas temperature is about 420 DEG C, meets and resolves requirement, now in heating furnace, heats flue gas without burning blast furnace gas or coke-stove gas.After high-temperature flue gas heat activated charcoal, temperature is down to approximately 300 DEG C, returns to (or upstream) before the main exhauster of sintering of sintering flue collector but in the former downstream of getting flue gas mouth of afterbody bellows.In Analytic Tower, active carbon is heated to 415 DEG C of left and right.
Comparative example 1
Repeat embodiment 1, but take coke-stove gas to burn 16000Nm
3the hot-air of/h raises approximately 120 DEG C (from 300 DEG C to 420 DEG C), approximately needs coke-stove gas 140Nm
3/ h.
Comparative example 2
Repeat comparative example 1, but take blast furnace gas combustion, need the about 800Nm of blast furnace gas
3/ h.
Embodiment 2
Technological process as shown in Figure 3.Repeat embodiment 1, the heated air being just transfused in the thermal treatment zone of Analytic Tower is by normal temperature air and the hot-air G2 (=440 DEG C) that carries out in a heat exchanger (14) from the high-temperature flue gas G1 (=446 DEG C) in last bellows of afterbody of sintering machine forming after indirect heat exchange.
Embodiment 3
Technological process as shown in Figure 3.Repeat embodiment 1, be just transfused to heated air in the thermal treatment zone of Analytic Tower and be between heat exchanger (14) and the thermal treatment zone of Analytic Tower closed circulation or semiclosed circulation and in heat exchanger (14) and from the high-temperature flue gas G1 (temperature is between 420～450 DEG C) in one or two bellows of afterbody of sintering machine, carried out indirect heat exchange after and the hot-air G2 (temperature is between 410～445 DEG C) of intensification.
Embodiment 4
Process unit is in the same manner as in Example 1.
386 DEG C of flue-gas temperatures in last bellows of sintering machine afterbody, air quantity 62000Nm
3/ h; 410 DEG C of flue-gas temperatures in penultimate bellows, air quantity 58000Nm
3/ h.Select high-temperature flue gas in sintering machine afterbody penultimate bellows to resolve thermal source as active carbon.The ability that Analytic Tower is processed active carbon is 15t/h, by the adjusting of blower fan and valve, makes the interior high-temperature flue gas of sintering machine afterbody penultimate bellows with 45000Nm
3the flow of/h enters Analytic Tower, due to the heat radiation on flue gas delivery pipe road, Analytic Tower porch flue-gas temperature is about 390 DEG C, now by high-temp waste gas (or the hot blast producing at heating furnace internal combustion burning blast-furnace gas or coke-stove gas, for blast furnace gas approximately 1100 DEG C, for coke-stove gas approximately 1900 DEG C) mix with the flue gas of 390 DEG C and make flue gas heat up, make Analytic Tower porch flue-gas temperature be about 410 DEG C, the about 100Nm of required coke-stove gas heats up
3/ h (if use blast furnace gas, needs the about 500Nm of blast furnace gas
3/ h).After high-temperature flue gas heat activated charcoal, temperature is down to approximately 300 DEG C, returns to before the main exhauster of sintering of sintering flue collector (or upstream) but in former downstream of getting flue gas mouth.In Analytic Tower, active carbon is heated to 405 DEG C of left and right.
Comparative example 3
Repeat embodiment 4, but take coke-stove gas to burn 45000Nm
3the hot-air of/h raises approximately 110 DEG C (from 300 DEG C to 410 DEG C), approximately needs coke-stove gas 380Nm
3/ h.
Comparative example 4
Repeat comparative example 3, but take blast furnace gas combustion heat supply, need the about 2200Nm of blast furnace gas
3/ h.
Embodiment 5
Repeat embodiment 4, just between heat exchanger (14) and the thermal treatment zone of Analytic Tower closed circulation or semiclosed circulation and in heat exchanger (14) and from the high-temperature flue gas G1 (temperature is between 380～400 DEG C) in one or two bellows of afterbody of sintering machine, carried out indirect heat exchange after and the hot-air G2 (approximately 390 DEG C of temperature) of intensification, after flowing out from heat exchanger, further with by high-temp waste gas (or the hot blast producing at heating furnace internal combustion burning blast-furnace gas or coke-stove gas, for blast furnace gas approximately 1100 DEG C, for coke-stove gas approximately 1900 DEG C) in the temperature regulated zone of heating furnace afterbody, carry out indirect heat exchange and be warming up to approximately 450 DEG C, become the hot blast G2 of 450 DEG C, then input the latter as heated air in the thermal treatment zone of Analytic Tower.
Embodiment 6
Repeat embodiment 5.In addition, by cooling blower, normal temperature air (as cooling air or cooling-air) is passed into the cooling zone of Analytic Tower from the cold air inlet of Analytic Tower cooling zone, carry out indirect heat exchange with the active carbon moving down to coolingly there is the active carbon that pyrolysis is analysed in cooling zone, and in cooling zone, carry out heat exchange with active carbon and the cooling air that heats up from the cooling air outlet output of the cooling zone of Analytic Tower, become the cooling air (for example 90-120 DEG C, 100 DEG C according to appointment) of intensification.The cooling air (about 90-120 DEG C, as 100 DEG C) that the cooling air outlet of the cooling zone from Analytic Tower is discharged guides to the air inlet of the combustion fan of heating furnace, is sent into the air inlet of the combustion chamber of heating furnace by combustion fan.Compared with embodiment 5, save the about 6.5vol% of coal gas.
Claims (16)
1. a hot renovation process for active carbon, the method comprises:
1) active carbon that has adsorbed the pollutant including oxysulfide, nitrogen oxide and dioxin in the activated carbon adsorber of desulphurization and denitration device from flue gas or sinter fume is transferred to the thermal treatment zone of active carbon Analytic Tower from the bottom of adsorption tower, wherein desulphurization and denitration device comprises activated carbon adsorber and Analytic Tower; With
2) in the thermal treatment zone of Analytic Tower, active carbon carries out indirect heat exchange and is heated or is warming up to regenerating active carbon temperature T 1 with the heated air in the input thermal treatment zone, cause active carbon to resolve, regenerate at this T1 temperature, the heated air of lowering the temperature with active carbon heat exchange is discharged from the heated air outlet of the thermal treatment zone simultaneously;
It is characterized in that, the heated air in the input thermal treatment zone is: (a) from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine; (b) by normal temperature air and the hot-air G2 that carries out in heat exchanger (14) from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine forming after indirect heat exchange; Or (c) between heat exchanger and the thermal treatment zone of Analytic Tower, circulate and in heat exchanger (14) with having carried out from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine after indirect heat exchange the hot-air G2 heating up.
2. the desulphurization and denitration method of sinter fume, the method comprises:
1) sinter fume is transported in a kind of activated carbon adsorber of desulphurization and denitration device that comprises activated carbon adsorber and Analytic Tower, contact with the active carbon of the top input from adsorption tower, make pollutant including oxysulfide, nitrogen oxide and dioxin by charcoal absorption; With
2) active carbon that has adsorbed the pollutant including oxysulfide, nitrogen oxide and dioxin is transferred to the thermal treatment zone of active carbon Analytic Tower from the bottom of adsorption tower; With
3) in the thermal treatment zone of Analytic Tower, active carbon and heated air are carried out indirect heat exchange and are heated or are warming up to regenerating active carbon temperature T 1, cause active carbon to resolve, regenerate at this T1 temperature, the heated air of lowering the temperature with active carbon heat exchange is discharged from the heated air outlet of the thermal treatment zone simultaneously;
It is characterized in that, the heated air in the input thermal treatment zone is: (a) from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine; (b) by normal temperature air and the hot-air G2 that carries out in heat exchanger (14) from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine forming after indirect heat exchange; Or (c) between heat exchanger and the thermal treatment zone of Analytic Tower, circulate and in heat exchanger (14) with having carried out from the high-temperature flue gas G1 in one or two bellows of afterbody of sintering machine after indirect heat exchange the hot-air G2 heating up.
3. according to the method for claim 1 or 2, wherein regenerating active carbon temperature T 1 is at 390-500 DEG C, preferably 400-470 DEG C, and more preferably 405-450 DEG C, more preferably at 410-440 DEG C, the more preferably scope of 410-430 DEG C.
4. according to the method for claim 1 or 2, the flue gas G1 or the hot-air G2 that are wherein transfused in the thermal treatment zone as heated air have 380～500 DEG C, and preferably 390～480 DEG C, more preferably 400-470 DEG C, more preferably 410-460 DEG C, the further temperature of preferred 420-450 DEG C.
5. according to any one method in claim 1-4, the flue gas G1 wherein lowering the temperature with active carbon heat exchange and discharge from the heated air outlet of the thermal treatment zone or the temperature T 2 of hot-air G2 are at 270-350 DEG C, the preferably scope of 290-330 DEG C, 300 DEG C according to appointment, 310 DEG C or 320 DEG C.
6. according to the method for claim 5, wherein in Analytic Tower or heat exchanger, experience the flue collector that high-temperature flue gas after heat exchange is back to sintering machine, preferably, turn back to the main exhauster of sintering of flue collector of sintering machine before or upstream but in the former downstream of getting flue gas mouth of above-mentioned bellows.
7. according to any one method in claim 1-6, wherein, the temperature of heated air before in the input thermal treatment zone during lower than regenerating active carbon temperature T 1, utilized other heating source to heat the high-temperature flue gas G1 as heated air or hot-air G2 before heated air enters into Analytic Tower; Preferably, high-temperature flue gas G1 or hot-air G2 are heated, make its temperature be increased to high 5-40 DEG C of specific activity charcoal regeneration temperature T1, preferred high 7-30 DEG C, more preferably 8-20 DEG C, the more preferably temperature of 10-15 DEG C.
8. according to the method for claim 7, wherein heating source is heating furnace, and this heating furnace burning blast furnace gas or coke-stove gas heat the high-temperature flue gas G1 as heated air or hot-air G2.
9. method according to claim 8, wherein in the case of combustion air being input to the air inlet of the combustion chamber in heating furnace by combustion fan, blast furnace gas or coke-stove gas are transfused in the combustion chamber of heating furnace and burn, then: the high-temp waste gas of (I) discharging from combustion chamber or high-temperature hot-air (Ga) flow through temperature regulated zone of heating furnace afterbody and flow out with from heat exchanger (14) after the hot blast G2 in this region of input mix or mix with the high-temperature flue gas G1 in one or two bellows of afterbody from sintering machine and be conditioned temperature, thereby become the hot blast (Gb) with 400-500 DEG C, then, this hot blast Gb is transported to the hot-wind inlet of the thermal treatment zone of Analytic Tower via pipeline as heated air, or
(II) high-temp waste gas of discharging from combustion chamber or high-temperature hot-air (Ga) flow through temperature regulated zone of heating furnace afterbody and with (II) with from heat exchanger (14), flow out after input this region hot blast G2 further carry out indirect heat exchange in case the temperature of this hot blast G2 that further raises to 400-500 DEG C, then, this hot blast G2 of intensification is transported to the hot-wind inlet of the thermal treatment zone of Analytic Tower via pipeline as heated air.
10. according to any one method in claim 1-9, wherein Analytic Tower is the vertical Analytic Tower of shell pipe type, and/or
Wherein Analytic Tower has 15-45 rice, preferably 20-40 rice, the more preferably tower height of 25-35 rice.
11. according to the method described in claim 9 or 10, wherein desorber has the thermal treatment zone on top and the cooling zone of bottom, the cooling air that the cooling air outlet of the cooling zone from Analytic Tower is discharged guides to the air inlet with the matching used combustion fan of heating furnace, is sent into the air inlet of the combustion chamber of heating furnace by combustion fan.
12. 1 kinds of active carbon resolvers or for a kind of active carbon resolver in any one method of above claim 1-11, it comprises:
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the flue gas blower fan (7) of the hot flue gas of conveying of (gas circuit) upstream of heating furnace (4);
Combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Second pipeline (L2) of supplied flue gases, wherein flue gas blower fan (7) is positioned between the leading portion and back segment of this second pipeline (L2), the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), be communicated to via optional the second valve (V2) on first pipeline (L1) in downstream at heating furnace (4) the afterbody downstream of the 3rd valve (V3) (or) with the second branch road (L10),
Air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4);
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4); With
The 3rd pipeline (L3), for from the thermal treatment zone heated air outlet of (2) discharge heated air, its one end is connected to the heated air outlet of the thermal treatment zone (2).
13. according to the device of claim 12, and wherein the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, the other end of the 3rd pipeline (L3) is connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
14. 1 kinds of active carbon resolvers or for a kind of active carbon resolver in any one method of above claim 1-11, it comprises
Active carbon Analytic Tower (1), this Analytic Tower (1) has: the thermal treatment zone (2) on top and the cooling zone (9) of bottom, be positioned at tower top for inputting the outlet of active carbon of output at the bottom for the treatment of the import of regenerated carbon and being positioned at tower regeneration;
Be positioned at the heating furnace (4) of (gas circuit) upstream of Analytic Tower (1);
Be positioned at the heat exchanger (14) (for example shell and tube exchanger) of (gas circuit) upstream of heating furnace (4);
For first pipeline (L1) of the thermal treatment zone (2) input heated air, its front end is connected to the tail end air outlet of heating furnace (4) and its end and is connected to the heated air import of the thermal treatment zone (2) via optional the 3rd valve (V3);
Carry second pipeline (L2) of hot flue gas, the front end of the leading portion of this second pipeline (L2) is connected to sintering machine (3) one or two bellows of afterbody (10), and the rear end of the back segment of the second pipeline (L2) is connected to the import of the exhaust gases passes of heat exchanger (14);
For discharging the 3rd pipeline (L3) of flue gas, its one end is connected to the outlet of the exhaust gases passes of heat exchanger (14);
For exporting the 4th pipeline (L4) of hot blast, its front end is connected with the heated air outlet of the thermal treatment zone (2), and its rear end is communicated to the hot blast of heat exchanger (14) or the import of air duct via optional the 4th valve (V4);
For delivery of the 6th pipeline (L6) of hot blast, its front end is communicated to the import of air or the circulating air passage of heat exchanger (14), and its rear end is divided into the first branch road (L9) and the second branch road (L10), wherein the first branch road (L9) is communicated to the equalizing section (being mixed zone or heat transfer zone) of heating furnace (4) afterbody via optional the first valve (V1), be communicated to via optional the second valve (V2) on first pipeline (L1) in downstream at heating furnace (4) the afterbody downstream of the 3rd optional valve (V3) (or) with the second branch road (L10),
Flue gas blower fan (7), it is positioned between the leading portion and back segment of this second pipeline (L2);
Optional combustion fan (11), it carries air to arrive the air inlet of heating furnace (4) via the 7th pipeline (L7);
Optional air delivery pipe road (L7), its front end is connected to the air outlet of combustion fan (11), and its rear end is connected to the air inlet of the combustion chamber of heating furnace (4); With
Gas conveying tube road (L8), its front end is connected to gaspipe line or coal gas basin (13), and its rear end is connected to the fuel inlet of the combustion chamber of heating furnace (4).
15. according to the device of claim 14, wherein said device also comprises: for the 5th pipeline (L5) of input air, it is communicated to the import of air or the circulating air passage of heat exchanger (14) via optional the 5th valve (V5).
16. according to the device of claims 14 or 15, and wherein the other end of the 3rd pipeline (L3) is connected to the flue collector of sintering machine; More preferably, the other end of the 3rd pipeline (L3) is connected to (or upstream) before the main exhauster of sintering of flue collector of sintering machine but in the former downstream of getting flue gas mouth of above-mentioned bellows.
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105056919A (en) * | 2015-07-24 | 2015-11-18 | 中冶华天工程技术有限公司 | Vertical oval charge pipe activated charcoal/coke regeneration integrated tower |
| CN105056920A (en) * | 2015-07-24 | 2015-11-18 | 中冶华天工程技术有限公司 | Embedded smoke pipe heating-cooling active carbon/coke regeneration integrated tower |
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| CN110743519A (en) * | 2019-11-11 | 2020-02-04 | 中国科学院山西煤炭化学研究所 | Desulfurization and denitrification activated carbon/carbon-based catalyst regeneration equipment and method |
| CN112403436A (en) * | 2019-09-04 | 2021-02-26 | 中冶长天国际工程有限责任公司 | Method and system for preparing desulfurization and denitrification active carbon by using active carbon powder |
| CN112705008A (en) * | 2019-10-25 | 2021-04-27 | 中冶长天国际工程有限责任公司 | Control method and device for hot air fan of analytical tower |
| CN112705005A (en) * | 2019-10-25 | 2021-04-27 | 中冶长天国际工程有限责任公司 | Method and device for obtaining pollution adsorption coefficient of activated carbon |
| CN112755987A (en) * | 2020-12-29 | 2021-05-07 | 江苏核电有限公司 | Device for on-line vacuum drying and regeneration of activated carbon of nuclear power unit detention bed |
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| CN105056920A (en) * | 2015-07-24 | 2015-11-18 | 中冶华天工程技术有限公司 | Embedded smoke pipe heating-cooling active carbon/coke regeneration integrated tower |
| CN105056918A (en) * | 2015-07-24 | 2015-11-18 | 中冶华天工程技术有限公司 | Energy-saving environment-friendly type active coke regeneration system and method thereof |
| CN105056919B (en) * | 2015-07-24 | 2018-02-13 | 中冶华天工程技术有限公司 | Vertical elliptical expects pipe activated carbon/Jiao regenerates integrated tower |
| CN105056920B (en) * | 2015-07-24 | 2018-02-13 | 中冶华天工程技术有限公司 | Buried smoke pipe heating cooling activated carbon/Jiao regenerates integrated tower |
| CN105056919A (en) * | 2015-07-24 | 2015-11-18 | 中冶华天工程技术有限公司 | Vertical oval charge pipe activated charcoal/coke regeneration integrated tower |
| CN108007217A (en) * | 2017-05-08 | 2018-05-08 | 中冶长天国际工程有限责任公司 | The activated carbon air-transport system and carrying method of UTILIZATION OF VESIDUAL HEAT IN |
| CN108007217B (en) * | 2017-05-08 | 2023-06-23 | 中冶长天国际工程有限责任公司 | Pneumatic conveying system and method for activated carbon by utilizing waste heat |
| CN109012168A (en) * | 2018-09-28 | 2018-12-18 | 国电环境保护研究院有限公司 | A kind of sealing and circulating regenerative feed heating system of desulfuring and denitrifying apparatus |
| CN109012168B (en) * | 2018-09-28 | 2023-12-19 | 国电环境保护研究院有限公司 | Closed circulation regeneration heating system of desulfurization and denitrification device |
| CN109675403A (en) * | 2019-03-11 | 2019-04-26 | 杨松 | A kind of improvement VOCs waste-gas adsorbant circular regeneration technique |
| CN112403436B (en) * | 2019-09-04 | 2022-12-06 | 中冶长天国际工程有限责任公司 | Method and system for preparing desulfurization and denitrification active carbon by using active carbon powder |
| CN112403436A (en) * | 2019-09-04 | 2021-02-26 | 中冶长天国际工程有限责任公司 | Method and system for preparing desulfurization and denitrification active carbon by using active carbon powder |
| CN110624526A (en) * | 2019-09-24 | 2019-12-31 | 常州大学 | Adsorbent regenerating unit based on hot gas desorption method |
| CN110624526B (en) * | 2019-09-24 | 2022-04-26 | 常州大学 | Adsorbent regenerating unit based on hot gas desorption method |
| CN112705008B (en) * | 2019-10-25 | 2022-06-07 | 中冶长天国际工程有限责任公司 | Control method and device for hot air fan of analytical tower |
| CN112705005A (en) * | 2019-10-25 | 2021-04-27 | 中冶长天国际工程有限责任公司 | Method and device for obtaining pollution adsorption coefficient of activated carbon |
| CN112705008A (en) * | 2019-10-25 | 2021-04-27 | 中冶长天国际工程有限责任公司 | Control method and device for hot air fan of analytical tower |
| CN110743519A (en) * | 2019-11-11 | 2020-02-04 | 中国科学院山西煤炭化学研究所 | Desulfurization and denitrification activated carbon/carbon-based catalyst regeneration equipment and method |
| CN112755987A (en) * | 2020-12-29 | 2021-05-07 | 江苏核电有限公司 | Device for on-line vacuum drying and regeneration of activated carbon of nuclear power unit detention bed |
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