CN107551756A

CN107551756A - Prevent the flue gas desulfurization and denitration method and device of corrosion

Info

Publication number: CN107551756A
Application number: CN201610507677.3A
Authority: CN
Inventors: 刘昌齐; 彭建宏; 魏进超; 叶恒棣; 李勇
Original assignee: Smelting Vast Of Heaven Energy-Conserving And Environment-Protective Technology Co Ltd In Hunan; Zhongye Changtian International Engineering Co Ltd
Current assignee: Smelting Vast Of Heaven Energy-Conserving And Environment-Protective Technology Co Ltd In Hunan; Zhongye Changtian International Engineering Co Ltd
Priority date: 2016-06-30
Filing date: 2016-06-30
Publication date: 2018-01-09
Also published as: WO2018000888A1

Abstract

A kind of flue gas desulfurization and denitrification device, preheated for the sour gas conveyance conduit of active carbon desorption tower by using hot gas and sour gas conveyance conduit is purged after parsing operation terminates, prevent the corrosive pipeline.Also provide a kind of flue gas desulfurization and denitrification device in addition, described device includes primary adsorption tower (T1) and activated carbon Analytic Tower (T3), wherein discharge chamber (a of primary adsorption tower (T1), b) it is divided into top discharge chamber (a) and bottom discharge chamber (b), the second flue (L2) for being wherein used for the pure flue gas of output from top discharge chamber (a) is communicated to blowdown stack, it is that the first flue (L1) merges or converged to return to the upstream of inlet plenum (3) and former flue gas conveying flue with the 3rd flue (L3) for the output flue gas from bottom discharge chamber (b).

Description

Prevent the flue gas desulfurization and denitration method and device of corrosion

Technical field

The present invention relates to the flue gas desulfurization and denitrification device and flue gas desulfurization and denitration method using activated carbon.More specifically, it is of the invention It is related to a kind of flue gas desulfurization and denitrification device, wherein by using hot gas for the sour gas conveyance conduit of active carbon desorption tower Preheated and sour gas conveyance conduit is purged after parsing operation terminates, prevent the corrosive pipeline, these category In fume treatment field.

Background technology

Activated carbon method processing flue gas technology has had more than 50 years research applicating history, and the technical research and application of early stage are main to concentrate In states such as Germany, Japan, the U.S..The BF companies of Germany begin to have developed Reinluft in nineteen fifty-seven (present DMT companies) Method desulfurization technology, Japanese then begun one's study active carbon desulfurization in the mid-1960s, German LURGI has also carried out water earlier Wash the research of regenerated carbon flue gas desulfurization technique.As the development of activated carbon method flue gas desulfurization technique abroad is with ripe, generation Some are more representational such as the BF methods, Reinluft methods, Lurgi methods of Germany；The day legislation of Japan, Sumitomo method；It is beautiful The Westraco methods of state.

For industrial smoke, the especially sintering device flue gas of steel and iron industry, using de- including activated carbon adsorber and Analytic Tower Sulphur, denitrification apparatus and technique are more satisfactory.In the desulphurization and denitration including activated carbon adsorber and Analytic Tower (or regenerator) In device, activated carbon adsorber is used to include from sintering flue gas or waste gas (the especially sintering flue gas of the sintering machine of steel and iron industry) absorption Pollutant including oxysulfide, nitrogen oxides, dust and dioxin, and Analytic Tower is used for the hot recycling of activated carbon.

Activated carbon desulfurization has that desulfurization degree is high, can realize denitration simultaneously, Tuo bioxin, dedusting, not produce waste water and dregs etc. excellent Point, it is extremely promising flue gas purifying method.Activated carbon can regenerate at high temperature, when temperature is higher than 350 DEG C, adsorb (sulfur dioxide is resolved, nitrogen for the pollutants such as oxysulfide, nitrogen oxides, dioxin on activated carbon generation fast resolving or decomposition Oxide is He bioxin is decomposed).And with the rise of temperature, the reproduction speed of activated carbon is further speeded up, recovery time contracting Short, preferably regenerating active carbon temperature is approximately equal to 430 DEG C in general control Analytic Tower, therefore, preferable resolution temperature (or again Raw temperature) it is for example in 390-450 DEG C of scope, more preferably in 400-440 DEG C of scope.

Traditional active carbon desulfurization technique is as shown in fig. 1.Flue gas introduces adsorption tower by booster fan, and ammonia is sprayed into entering tower mouth With the mixed gas of air, to improve NO_XRemoval efficiency, flue gas after purification, which enters, sinters main smoke stack emission.Activated carbon by Tower top is added in adsorption tower, and is moved down in the presence of gravity and bottom of towe drawing mechanism.Analytic Tower come out activated carbon by Activated carbon conveyer is delivered to adsorption tower, and the activated carbon after adsorption tower absorption pollutant saturation is discharged by bottom, the activated carbon of discharge Analytic Tower is delivered to by activated carbon conveyer, carries out regenerating active carbon.

Activated carbon flue gases purification have can simultaneous SO_2 and NO removal, realize by-product resource, adsorbent can be recycled, The features such as denitrification efficiency is high, right and wrong are often with promising desulfurization and denitrification integral technology.Including activated carbon adsorber In the desulphurization and denitration device of Analytic Tower (or regenerator), activated carbon adsorber is used for from sintering flue gas or waste gas (especially steel work The sintering flue gas of the sintering machine of industry) pollutant of the absorption including oxysulfide, nitrogen oxides and dioxin, and Analytic Tower is used for The hot recycling of activated carbon.

Activated carbon method flue gases purification has the function of simultaneous SO_2 and NO removal, and the main equipment that this technique includes has adsorption tower, again Raw tower and activated carbon conveying device.Relative to NO_xFor, SO₂Easily remove, next group of adsorption tower of normal condition can obtain To up to 90% desulfurization degree, but denitration rate is relatively low.

Generally, there is activated carbon method flue gases purification high desulphurization denitration rate, the utilization of accessory substance resourcebility, activated carbon to be recycled The features such as use, the principle of its desulphurization denitration are as follows：

In adsorption tower, a part of SO in flue gas₂It is tightly held by activated carbon, still, the SO of another part₂, i.e., in activated carbon Surface SO₂Oxidized absorption forms sulfuric acid, its reaction equation：

2SO₂+O₂+2H₂O→2H₂SO₄

If spraying into a small amount of ammonia in flue gas or in adsorption tower, SO can be accelerated₂Absorption, its reaction equation：

NH₃+H₂SO₄→NH₄HSO₄

But in order to reach the effect of denitration while desulfurization, more ammonia can be typically sprayed at adsorption tower smoke inlet, The ammonia needed for desulfurization should be met, while meet the ammonia needed for denitration.Denitration reaction formula is：

4NO+O₂+4NH₃→4N₂+6H₂O

At the same time following side reaction in adsorption tower also be present：

2NH₃+H₂SO₄→(NH₄)₂SO₄。

Typically, SO₂With NH₃Reaction rate than NO and NH₃Reaction rate faster.In addition, the SO in flue gas₃、HF、 It can also be reacted with HCl with NH3.

The effect of Analytic Tower is by the SO of charcoal absorption₂Discharge, while the temperature more than 400 DEG C and certain stop , bioxin decomposable asymmetric choice net more than 80% under time, activated carbon recycles again after cooling down, sieving.The SO discharged₂It can make Sulfuric acid etc., the communicated device of activated carbon after parsing are sent to adsorption tower and are re-used to adsorb SO₂And NO_XDeng.

The NO in adsorption tower and Analytic Tower_XThe reaction such as SCR, SNCR occurs with ammonia, so as to remove NO_X.Dust is passing through suction It is tightly held by activated carbon during attached tower, the vibratory sieve in Analytic Tower bottom is separated, and sends to ash silo under sieving for active carbon powder, then Blast furnace can be sent to or sintering uses as fuel.

Gas cleaning is carried out using activated carbon method, in order to improve clean-up effect, flue gas can be made to pass through multilayer active carbon bed.Multilayer Active carbon bed arrangement is broadly divided into up-down structure and front-end geometry, as shown in Figure 2.Active carbon bed is integral in tower, Activated carbon is uniformly moved down using gravity.Along the flow direction of flue gas, first with the charcoal absorption of smoke contacts in flue gas more Multi-pollutant, discharged together with later active charcoal, the unadsorbed saturation of later active charcoal can be caused just to discharge in tower or above active Gas cleaning effect is not played in charcoal adsorption saturation still in tower.

Steel industry is promotes China's industrialization, the development of urbanization to be made that significant contribution, but China's steel and iron industry is environmentally friendly simultaneously Horizontal low, specific yield pollutant discharge amount is higher, seriously restricts the raising of steel industry whole competitiveness.Polluted for control Thing discharges, and State Ministry of Environmental Protection formulates《Steel sintering, pelletizing industrial air pollution thing discharge standard》, it is indicated that from 2015 1 The moon 1, existing steel enterprise sintering, pelletizing perform following Air Pollutant Emission limit value：SO₂ 200mg/m³、NOx 300 mg/m³, dioxins 0.5ng-TEG/m³.It can be seen that steel industry air contaminant treatment is lifted by original dedusting, desulfurization For SO₂The multi-pollutant Collaborative Control such as-NOx- dioxin.At present, state's inner desulfurization technology tends to be ripe, and denitration takes off bioxin and still located In the starting stage.Domestic Shanghai Ke Liu companies use activated coke technology, its structure type in coal-burning boiler and nonferrous smelting industry It is consistent with principle with Sumitomo.

Activated carbon (Jiao) method sintering gas purifying technology is a kind of dry method flue gas treatment technology of resourcebility, has water saving, takes off Sulphur, denitration, Tuo bioxin, removing heavy-metal, dedusting and remove other micro harmful smoke components (such as HCl, HF, SO3) Function, while the Sulphur ressource that the recyclable country is in short supply (high concentration SO 2 can prepare concentrated sulfuric acid etc.).

Fig. 2 shows the absorbent charcoal adsorber of SUMITOMO CHEMICAL company：Active carbon bed is divided into three rooms, each room activated carbon in tower Uniformly moved down using gravity, it is more in flue gas first with the cup charcoal absorption of smoke contacts along the flow direction of flue gas Pollutant, the activated carbon of middle rear chamber adsorb the pollutant in flue gas successively, thus control turn of the discharge valve of active carbon bed bottom Speed come control activated carbon from the velocity of discharge, so as to reach gas cleaning effect.

Fig. 3 shows the absorbent charcoal adsorber of Shanghai Ke Liu companies：Active carbon bed is integral in tower, multistage active-carbon bed Layer arrangement is broadly divided into up-down structure, and activated carbon is uniformly moved down using gravity.Along the flow direction of flue gas, connect first with flue gas More multi-pollutant in tactile charcoal absorption flue gas, is discharged together with later active charcoal, and later active charcoal can be caused unadsorbed full With just in discharge tower or above charcoal absorption is saturated and does not play gas cleaning effect still in tower.

The concentration for being entered oxious component of the adsorption tower after the purification of adsorption tower in flue gas due to former flue gas is gradually increased from top to bottom Add, existing process and device need whole flue gases entering next stage adsorption tower, not only increase investment and operating cost, also increase Add extras maintenance workload.

For investment reduction and operating cost, more reasonably active carbon purifying technique and device need to be used.

The content of the invention

For disadvantages described above and problem, present inventor has found after further investigation, from the active carbon bed of adsorption tower In, top enter discharge chamber in flue gas (abbreviation upper strata flue gas) in pollutant concentration it is very low (ppm levels), often reach Emission request or discharge standard, or the flue gas of the part are individually handled in addition.

The present invention requires increasingly tighter environmental requirement for gas cleaning, and flue gas is purified, to reach requirements at the higher level, must Two stage treatment must be carried out to whole flue gases.This technology is that basis exhaust gas components after smoke eliminator coagulation have from top to bottom Evil composition be stepped up (activated carbon (Jiao) due to entering purifier top is the activated carbon (Jiao) after Analytic Tower activates, As activated carbon (Jiao) moves from top to bottom, the increase of the oxious component in activated carbon (Jiao) absorption flue gas, its adsorption capacity Also weaker, thus it is also higher to give off the concentration of the oxious component of flue gas for it), so as to extract the exceeded portion of wherein oxious component Divide flue gas to enter secondary smoke purifier or turn again to primary adsorption tower, a part for emission request is met after coagulation Flue gas is then directly discharged into air by chimney.

Adsorption tower discharge chamber is divided into two layers or multilayer up and down by the technique and device of the present invention, according to the harmful components of discharge Concentration regulation so will reduce 30%~50% into the exhaust gas volumn of next stage, can reduce into the exhaust gas volumn of next stage adsorption tower The ability of booster fan and secondary absorption tower, so as to reduce investment and operating cost.Avoid discharge chamber middle and upper part in the prior art Clean flue gas is mutually gone here and there mixed with flue gas of the bottom containing pollutant.

During flue gas enters adsorption tower by active carbon bed, the oxious component in flue gas is purified, due in adsorption tower Activated carbon from top to bottom, top is the stronger activated carbon of adsorption capacity, as activated carbon moves down, the oxious component of absorption Increase, its adsorption cleaning ability reduces, and the oxious component after purification in flue gas gradually increases, will so be mixed together up and down flat It certainly will can not reach fume emission requirement afterwards, if the concentration relatively low flue gas for being capable of qualified discharge in top directly discharged, by under The exceeded flue gas in portion returns to adsorption tower air inlet and purified again, or is purified into secondary absorption tower.

It is an object of the invention to provide a kind of new flue gas desulfurization and denitrification device, wherein the discharge chamber of adsorption tower is divided into upper and lower two Layer or multilayer.Stop of the activated carbon in active carbon bed is adjusted by adjusting adsorption tower active carbon bed bottom discharge valve (5) Time, it is ensured that pollutant load is in the range of meeting the requirements or meeting regulation from discharge chamber upper strata or the flue gas discharged at the middle and upper levels. That is, limit value of the content less than setting.

According to the first embodiment of the present invention, there is provided a kind of flue gas desulfurization and denitrification device, it include primary adsorption tower (T1) and Regenerating active carbon tower (or Analytic Tower) (T3), wherein activated carbon Analytic Tower (T3) have the heating zone on top, middle part buffering area and under The cooling zone in portion, hot gas input pipe (L1a) is connected to respectively in the following side of top heating zone and upper lateral part and hot gas is defeated Outlet pipe (L1b), cooling gas input pipe (L2a) is connected to respectively in the following side of bottom cooling zone and upper lateral part and cooling gas is defeated Outlet pipe (L2b), the sour gas conveyance conduit (L3a) that analytically the buffering area sidepiece in the middle part of tower (T3) is drawn are connected to acid making system, It is characterized in that：A hot gas branch pipe (L3a') has been separated from sour gas conveyance conduit (L3a) initiating terminal (or front end), Also, the other end of the hot gas branch pipe (L3a') connected with hot gas input pipe (L1a) or with hot gas efferent duct (L1b) Connection so that the hot gas branch pipe (L3a') is as the branch pipe separated from hot gas input pipe (L1a) or is used as from heating gas The branch pipe separated on body efferent duct (L1b)；

Wherein primary adsorption tower (T1) include agent structure (1), the feeding warehouse (2) at the top of primary adsorption tower (T1), inlet plenum (3), Lead to former flue gas conveying i.e. the first flue of flue (L1), adsorption tower Lower Hold discharge valve (4), active carbon bed bottom of inlet plenum (3) Portion's discharge valve (5), porous plate (6) and discharge chamber.

Preferably, discharge chamber is divided into top discharge chamber (a) and bottom discharge chamber (b), wherein for defeated from top discharge chamber (a) The second flue (L2) for going out pure flue gas is communicated to blowdown stack, and for the output flue gas from bottom discharge chamber (b) It is that the first flue (L1) merges or converged that three flues (L3), which return to the upstream of inlet plenum (3) and former flue gas conveying flue,.

Typically, wherein primary adsorption tower (T1) has an active carbon bed, two active carbon beds or multiple active carbon beds (A, B, C), preferably 2-5 bed.

Typically, the tower height of primary adsorption tower (T1) is 10-50m, preferably 13-45m, preferably 15-40m, more preferably 18-35m.

Typically, the ratio between top discharge chamber (a) and the height of bottom discharge chamber (b) in vertical direction are 0.7-1.3:1, preferably 0.8-1.2:1, preferably 0.9-1.1:1, such as 1:1.

Typically, described two or multiple active carbon beds are separated by porous plate to be formed.

According to the second embodiment of the present invention, there is provided a kind of flue gas desulfurization and denitrification device, it includes:

1) the primary adsorption tower (T1) and secondary absorption tower (T2) of series connection, the adsorption tower (T1) and (T2) tower height be independently of one another, Such as 10-50m, more preferably preferably 13-45m, preferably 15-40m, 18-35m；With

2) regenerating active carbon tower (or Analytic Tower) (T3),

Wherein activated carbon Analytic Tower (T3) has heating zone, the buffering area at middle part and the cooling zone of bottom on top, is heated on top The following side in area and upper lateral part are connected to hot gas input pipe (L1a) and hot gas efferent duct (L1b) respectively, are cooled down in bottom The following side in area and upper lateral part are connected to cooling gas input pipe (L2a) and cooling gas efferent duct (L2b) respectively, analytically tower (T3) The sour gas conveyance conduit (L3a) that the buffering area sidepiece at middle part is drawn is connected to acid making system, it is characterised in that：From sour gas The initiating terminal (or front end) of conveyance conduit (L3a) has separated a hot gas branch pipe (L3a'), also, the hot gas branch pipe (L3a') the other end is connected with hot gas input pipe (L1a) or connected with hot gas efferent duct (L1b) so that the heating gas Body branch pipe (L3a') divides as the branch pipe separated from hot gas input pipe (L1a) or as from hot gas efferent duct (L1b) The branch pipe gone out；

Wherein, primary adsorption tower (T1) includes agent structure (1), feeding warehouse (2), inlet plenum at the top of primary adsorption tower (T1) (3) former flue gas conveying i.e. the first flue of flue (L1), adsorption tower Lower Hold discharge valve (4), active-carbon bed of inlet plenum (3), is led to Layer bottom discharge valve (5), porous plate (6) and discharge chamber,

Secondary absorption tower (T2) includes agent structure (1), the feeding warehouse (2) at the top of adsorption tower (T2), inlet plenum (3 '), logical respectively To the 3rd flue (L3), adsorption tower Lower Hold discharge valve (4), active carbon bed bottom discharge valve (5), the porous plate of inlet plenum (3 ') (6) and discharge chamber (9), and

The bottom discharge chamber (b) of primary adsorption tower (T1) is connected to the inlet plenum (3 ') of secondary absorption tower (T2) by pipeline.

Preferably, the discharge chamber of primary adsorption tower (T1) is divided into top discharge chamber (a), bottom discharge chamber (b), wherein for from The second flue (L2) of the pure flue gas of output is communicated to blowdown stack in top discharge chamber (a), for from bottom discharge chamber (b) 3rd flue (L3) of middle output flue gas is communicated to the inlet plenum (3 ') of secondary absorption tower (T2), and optionally, is inhaled from two level The 4th flue (L4) of output flue gas leads to after merging or converge with the second flue (L2) in the discharge chamber (9) of attached tower (T2) Blowdown stack；Or

The discharge chamber of primary adsorption tower (T1) is divided into top discharge chamber (a), middle part discharge chamber (c) and bottom discharge chamber (b), wherein using Blowdown stack is communicated in the second flue (L2) of the pure flue gas of output from the top discharge chamber (a), for from bottom outlet 3rd flue (L3) of output flue gas is communicated to the inlet plenum (3 ') of secondary absorption tower (T2) in room (b), for from middle part discharge chamber (c) the 5th flue (L5) of output flue gas is respectively communicated to the second flue (L2) or the 3rd flue gas via switching valve (10) in Pipeline (L3), and optionally, the 4th flue (L4) and second of output flue gas from secondary absorption tower (T2) discharge chamber (9) Flue (L2) merges or leads to blowdown stack after converging.

In this application, it is preferable that primary adsorption tower (T1) can be used side by side with two or more.Secondary absorption tower (T2) It can be used side by side with two or more.The discharge chamber of primary adsorption tower (T1) arranged side by side is individually insulated into upper and lower two chambers Three chambers (a, c, b) of (a, b) or upper, middle and lower, i.e. it is divided into two levels or three levels, and, it is further preferred that from different absorption The pipeline of flue gas is discharged in the chamber of the same level of tower can merge or converge.When the primary adsorption tower (T1) of symmetrical expression double tower form During with two or more primary adsorption tower (T1) arranged side by side, then each symmetrical expression double tower as primary adsorption tower (T1) arranged side by side Discharge chamber is individually insulated into three chambers (a, c, b) of upper and lower two chambers (a, b) or upper, middle and lower, i.e. is divided into two levels or three layers Level, and, it is further preferred that the pipeline of flue gas is discharged from the chamber of the same level of different adsorption towers can merge or converge.

Typically, primary adsorption tower (T1) or secondary absorption tower (T2) have independently of one another an active carbon bed, two it is active-carbon bed Layer or multiple active carbon beds (A, B, C), preferably 2-5 bed.Described two or multiple active carbon beds separate institute by porous plate Formed.

Typically, primary adsorption tower (T1) has identical or different structure snd size each other with secondary absorption tower (T2).

Typically, the tower height of primary adsorption tower (T1) and secondary absorption tower (T2) is 10-50m, preferably 13-45m independently of one another, excellent Select 15-40m, more preferably 18-35m.

Typically, typically, when primary adsorption tower (T1) has top discharge chamber (a) and during bottom discharge chamber (b), top discharge chamber (a) and The ratio between the height of both bottom discharge chambers (b) in vertical direction is 0.7-1.3:1, preferably 0.8-1.2:1, preferably 0.9-1.1:1, Such as 1:1.And when primary adsorption tower (T1) has top discharge chamber (a), middle part discharge chamber (c) and bottom discharge chamber (b), top goes out The ratio between air chamber (a), middle part discharge chamber (c) and the height of bottom discharge chamber (b) three in vertical direction are 0.5-1.0:0.5-1.0: 0.8-1, preferably 0.6-0.9:0.6-0.9:0.8-1, preferably 0.7-0.8:0.7-0.8:0.8-1.

Primary adsorption tower (T1) has identical or different structure snd size each other with secondary absorption tower (T2).

Typically, there is top in the device according to first embodiment and second embodiment, activated carbon Analytic Tower (T3) The cooling zone of heating zone, the buffering area at middle part and bottom, heating gas is connected to respectively in the following side of top heating zone and upper lateral part Body input pipe (L1a) and hot gas efferent duct (L1b), cooling gas is connected in the following side of bottom cooling zone and upper lateral part respectively Body input pipe (L2a) and cooling gas efferent duct (L2b), the sour gas that analytically the buffering area sidepiece in the middle part of tower (T3) is drawn are defeated Pipeline (L3a) is sent to be connected to acid making system (or relieving haperacidity area).

Preferably, a hot gas branch pipe has been separated from sour gas conveyance conduit (L3a) initiating terminal (or front end) (L3a'), also, the other end (such as via valve) of the hot gas branch pipe (L3a') connects with hot gas input pipe (L1a) Or connected with hot gas efferent duct (L1b) so that the hot gas branch pipe (L3a') is as from hot gas input pipe (L1a) The branch pipe that separates or as the branch pipe separated from hot gas efferent duct (L1b).

In this application, it is preferable that primary adsorption tower (T1) can be used side by side with two or more.Secondary absorption tower (T2) It can be used side by side with two or more.The discharge chamber of primary adsorption tower arranged side by side is individually insulated into upper and lower two chambers (a, b) Or three chambers (a, c, b) of upper, middle and lower, i.e. it is divided into two levels or three levels, and, it is further preferred that from different adsorption towers The pipeline of flue gas is discharged in the chamber of same level can merge or converge.When symmetrical expression double tower form primary adsorption tower (T1) with During two or more primary adsorption towers arranged side by side, then the discharge chamber of each symmetrical expression double tower arranged side by side as primary adsorption tower point Three chambers (a, c, b) of upper and lower two chambers (a, b) or upper, middle and lower are not isolated into, i.e. it is divided into two levels or three levels, and, It is further preferred that the pipeline of flue gas is discharged from the chamber of the same level of different adsorption towers can merge or converge.

Generally, due to flue gas is after the processing of primary adsorption tower, some former flue gases (such as 20-60% former flue gas, it is excellent Select 30-50% former flue gas) reach discharge standard, can directly it discharge, so the number of primary adsorption tower is than secondary absorption tower Number is more.Usually, primary adsorption tower is 2-8, preferably 3-6, more preferably 4-5；Secondary absorption tower is 1-6 It is individual, preferably 2-5, more preferably 3-4.Such as：Primary adsorption tower is 4, and secondary absorption tower is 2.

According to the third embodiment the present invention, there is provided a kind of use is according to the cigarette of the desulfuring and denitrifying apparatus of first embodiment Desulfurization method of denitration, this method comprise the following steps：

I) desulphurization and denitration step：Former flue gas is transported in primary adsorption tower (T1) inlet plenum (3) via the first flue (L1) One or more active carbon beds of primary adsorption tower (T1), flue gas and the addition at the top of primary adsorption tower (T1) are flowed successively through afterwards Activated carbon carries out cross-current type contact, the pollutant (such as oxysulfide, nitrogen oxides, dust, dioxin) wherein contained by flue gas Removed or partly removed by activated carbon, flue gas is entered in primary adsorption tower (T1) discharge chamber afterwards, has adsorbed pollutant Activated carbon is then discharged from primary adsorption tower (T1) bottom；Preferably, while aforesaid operations, dilution ammonia is passed through one-level It is passed into the flue gas input channel (L1) of adsorption tower (T1) and optionally in primary adsorption tower (T1)；With

II) activated carbon analyzing step：The activated carbon for having adsorbed pollutant is transferred to top from the bottom of primary adsorption tower (T1) Heating zone and bottom cooling zone a kind of activated carbon Analytic Tower (T3) heating zone in, allow activated carbon to be parsed, regenerated, And the activated carbon after parsing, regenerating is discharged after passing downwardly through cooling zone from desorber (T3) bottom；Wherein：In resolving Nitrogen is passed into Analytic Tower (T3) top, and nitrogen is passed through Analytic Tower (T3) via the second nitrogen pipeline optionally together Bottom；With, the nitrogen being passed through in Analytic Tower (T3) by from activated carbon thermal desorption include SO₂And NH₃Gaseous contamination inside Thing is taken out of from the centre portion between the heating zone and cooling zone of desorber (T3) and delivers to system via sour gas pipeline (L3a) Acid system；

Wherein, allowing including SO₂And NH₃Gas pollutant (i.e. sour gas) inside conveys via sour gas pipeline (L3a) To before acid making system, using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) output hot gas, makes hot gas flow through sour gas pipeline (L3a) to preheat sour gas pipeline (the L3a) (example in Such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, it is further preferred 300-380 DEG C, more preferably 320-360 DEG C)； With optionally, including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops running through sour gas pipeline (L3a) Afterwards, exported using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) Hot gas, hot gas is allowed to purge the sour gas pipeline (L3a), to remove the acidity of residual in sour gas pipeline (L3a) Gas.

Preferably, the I) desulphurization and denitration step is carried out as follows：Former flue gas is transported to one-level via the first flue (L1) Flow successively through one or more active carbon beds of primary adsorption tower (T1) after in the inlet plenum (3) of adsorption tower (T1), flue gas with from The activated carbon added at the top of primary adsorption tower (T1) carries out cross-current type contact, pollutant (such as oxysulfide, nitrogen wherein contained by flue gas Oxide, dust, dioxin etc.) removed or partly removed by activated carbon, flue gas enters the upper of primary adsorption tower (T1) afterwards In portion's discharge chamber (a) and bottom discharge chamber (b), the flue gas of discharge is via the second cigarette from the top discharge chamber (a) of primary adsorption tower (T1) Feed channel (L2) is delivered to blowdown stack to be discharged, and discharge contains less from the bottom discharge chamber (b) of primary adsorption tower (T1) The flue gas for measuring pollutant converges via the conveying return of the 3rd flue (L3) with the former flue gas in the first flue (L1), and adsorbs The activated carbon of pollutant is then discharged from primary adsorption tower (T1) bottom；Preferably, while aforesaid operations, by diluted ammonia Gas is passed through in the flue gas input channel (L1) of primary adsorption tower (T1) and is optionally passed into primary adsorption tower (T1).

It is preferred that the rotating speed by adjusting primary adsorption tower (T1) active carbon bed bottom discharge valve (5), to adjust primary adsorption tower (T1) residence time of activated carbon or speed is moved down in active carbon bed in so that in the top discharge chamber (a) of primary adsorption tower (T1) Flue gas pollutant load in the range of meeting the requirements or meeting regulation.That is, limit value of the content less than setting.

It may further be preferable that before the startup of activated carbon analyzing step or allowing including SO₂And NH₃Gas pollutant inside is (i.e. Sour gas) be delivered to acid making system via sour gas pipeline (L3a) before, using hot gas branch pipe (L3a') from heating gas Hot gas is exported in body input pipe (L1a) or from hot gas efferent duct (L1b), hot gas is flowed through sour gas pipeline (L3a) come preheat the sour gas pipeline (L3a) (such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, further It is preferred that 300-380 DEG C, more preferably 320-360 DEG C).

It is further preferred that after activated carbon analyzing step terminates or including SO₂And NH₃Gas pollutant (i.e. sour gas) inside After stopping running through sour gas pipeline (L3a), using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from Output hot gas, allows hot gas to purge the sour gas pipeline (L3a), to remove acidity in hot gas efferent duct (L1b) The sour gas of residual in gas pipeline (L3a).

According to the 4th embodiment of the present invention, there is provided a kind of use is according to the cigarette of the desulfuring and denitrifying apparatus of the second embodiment 2 Desulfurization method of denitration, this method comprise the following steps：

I) desulphurization and denitration step：

1) former flue gas flows successively through one-level after being transported to via the first flue (L1) in primary adsorption tower (T1) inlet plenum (3) One or more active carbon beds of adsorption tower (T1), flue gas carry out cross-current type with the activated carbon added at the top of primary adsorption tower (T1) Contact, the pollutant (such as oxysulfide, nitrogen oxides, dust, dioxin) wherein contained by flue gas is by activated carbon removing or portion Divide removing, afterwards,

2) flue gas is entered in primary adsorption tower (T1) discharge chamber, has adsorbed the activated carbon of pollutant then from primary adsorption tower (T1) Discharge bottom；The flue gas containing a small amount of pollutant of discharge is conveyed via pipeline from the bottom discharge chamber (b) of primary adsorption tower (T1) Into the inlet plenum (3 ') of secondary absorption tower (T2) and one or more active carbon beds of secondary absorption tower (2) are flowed successively through, wherein Pollutant (such as oxysulfide, nitrogen oxides, dust, dioxin) contained by flue gas is further removed by activated carbon；From two level The flue gas of discharge is discharged by chimney in the discharge chamber (10) of adsorption tower (T2), has adsorbed the activated carbon of pollutant then from secondary absorption Discharge tower (T2) bottom；Preferably, while aforesaid operations, dilution ammonia is passed through to the first flue gas of primary adsorption tower (T1) Pipeline (L1), which neutralizes, is optionally passed through in the pipeline that flue gas is conveyed for secondary absorption tower (T2) and is optionally passed into primary adsorption tower (T1) and/or in secondary absorption tower (T2)；

With

II) activated carbon analyzing step：The activated carbon of pollutant will have been adsorbed from the bottom of primary adsorption tower (T1) and/or secondary absorption The bottom of tower (T2) is transferred to a kind of heating zone of activated carbon Analytic Tower (T3) of the cooling zone of heating zone and bottom with top In, allow activated carbon to be parsed, regenerated, and the activated carbon after parsing, regenerating is downward through cooling zone afterwards from desorber (T3) Discharge bottom；Wherein：Nitrogen is passed into Analytic Tower (T3) top in resolving, and optionally together passed through nitrogen Analytic Tower (T3) bottom is passed through by the second nitrogen pipeline；Be passed through nitrogen in Analytic Tower (T3) by the thermal desorption from activated carbon Including SO₂And NH₃Gas pollutant inside is taken out of and passed through from the centre portion between the heating zone and cooling zone of desorber (T3) Acid making system is delivered to by sour gas pipeline (L3a)；

Wherein, allowing including SO₂And NH₃Gas pollutant (i.e. sour gas) inside conveys via sour gas pipeline (L3a) To before acid making system, using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) output hot gas, makes hot gas flow through sour gas pipeline (L3a) to preheat sour gas pipeline (the L3a) (example in Such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, it is further preferred 300-380 DEG C, more preferably 320-360 DEG C)； With optionally, including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops running through sour gas pipeline (L3a) Afterwards, exported using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) Hot gas, hot gas is allowed to purge the sour gas pipeline (L3a), to remove the acidity of residual in sour gas pipeline (L3a) Gas.It is preferred that primary adsorption tower (T1) can be used side by side with two or more (such as 2-6, such as 3 or 4)；With/ Or, secondary absorption tower (T2) can be used with two or more (such as 2-4, such as 3) side by side.

Preferably, the I) desulphurization and denitration step is carried out as follows：

2) when primary adsorption tower (T1) has top discharge chamber (a) and bottom discharge chamber (b), flue gas enters primary adsorption tower (T1) Top discharge chamber (a) and bottom discharge chamber (b) in, and adsorbed the activated carbon of pollutant and then discharged from primary adsorption tower (T1) bottom； Wherein, the flue gas of discharge is delivered to discharge cigarette via the second flue (L2) from the top discharge chamber (a) of primary adsorption tower (T1) Chimney is to be discharged, and the flue gas containing a small amount of pollutant of discharge is via the 3rd flue gas from the bottom discharge chamber (b) of adsorption tower (T1) Pipeline (L3) is delivered in the inlet plenum (3 ') of secondary absorption tower (T2) and flows successively through the one or more living of secondary absorption tower (T2) Property charcoal bed, the flue gas of discharge is delivered to and second via the 4th flue (L4) from secondary absorption tower (T2) discharge chamber (9) Flue gas in flue (L2) converges and then discharged, or,

When primary adsorption tower (T1) has top discharge chamber (a), middle part discharge chamber (c) and bottom discharge chamber (b), flue gas enters one In the top discharge chamber (a) of level adsorption tower (T1), middle part discharge chamber (c) and bottom discharge chamber (b), and the activated carbon of pollutant is adsorbed Then discharged from primary adsorption tower (T1) bottom；Wherein, from the top discharge chamber (a) of primary adsorption tower (T1) discharge flue gas via Second flue (L2) is delivered to blowdown stack to be discharged, and discharge contains from the bottom discharge chamber (b) of adsorption tower (T1) The flue gas of a small amount of pollutant is delivered in the inlet plenum (3 ') of secondary absorption tower (T2) and flowed successively through via the 3rd flue (L3) One or more active carbon beds of secondary absorption tower (T2), from secondary absorption tower (T2) discharge chamber (9) flue gas of discharge via 4th flue (L4), which is delivered to, to be converged with the flue gas in the second flue (L2) and then discharges, from primary adsorption tower (T1) Middle part discharge chamber (c) in discharge flue gas via the 5th flue (L5) be transported through switch valve (10) switching and difference Converge with the flue gas in the second flue (L2) or converge with the flue gas in the 3rd flue (L3), adsorbed the activity of pollutant Charcoal is then discharged from secondary absorption tower (T2) bottom；Preferably, while aforesaid operations, dilution ammonia is passed through primary adsorption The first flue (L1) of tower (T1), which neutralizes, to be optionally passed through in the 3rd flue (L3) that flue gas is conveyed for secondary absorption tower (T2) And optionally it is passed into primary adsorption tower (T1) and/or secondary absorption tower (T2).

In the method according to the third and fourth embodiment, it is preferred that by adjusting unloading for adsorption tower active carbon bed bottom Valve (5) is expected to adjust residence time of the activated carbon in active carbon bed, it is ensured that from primary adsorption tower (T1) top discharge chamber (a) In or from the top discharge chamber (a) of primary adsorption tower (T1) and middle part discharge chamber (c) pollutant load is meeting in the flue gas of discharge It is required that or in the range of meeting regulation.

In this application, " optionally " represent carry out or without." optional " represent to be with or without.

In the prior art, when activated carbon analyzing step starts, hot sour gas at the beginning or is flowing through cold (such as locate early stage In environment temperature) sour gas pipeline (L3a) when and cause temperature to reduce, so as to condense, formed liquid acid, liquid acid pair Sour gas pipeline (L3a) has strong corrosion effect.In order to solve this problem, typically set in sour gas pipeline (L3a) periphery Put heat tracing pipe and outermost layer sets heat-insulation layer.Ensure that sour gas is flowing through sour gas pipeline by heat tracing pipe hot gas (L3a) temperature when is higher than dew point, i.e. allows acidic components to keep gaseous state.

Present inventor is had found by studying, and before the startup of activated carbon analyzing step, is passed through in advance by using hot gas The pipeline is preheated in sour gas pipeline (L3a), is preheated to the temperature of the dew point higher than sour gas, such as is preheated to 250-450 DEG C of temperature, preferably 280-400 DEG C, more preferably 300-380 DEG C, more preferably 320-360 DEG C of temperature. When sour gas flows continuously through sour gas pipeline (L3a), the heat entrained by sour gas is enough to maintain sour gas pipeline (L3a) temperature, its cooling is prevented.

It is further preferred that including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops running through sour gas pipeline (L3a) after or after activated carbon analyzing step terminates, immediately using hot gas branch pipe (L3a') from hot gas input pipe (L1a) hot gas is exported in or from hot gas efferent duct (L1b), allows hot gas to purge the sour gas pipeline (L3a), To remove residual or the sour gas being detained in sour gas pipeline (L3a).

That is, before the startup of activated carbon analyzing step or allowing including SO₂And NH₃Gas pollutant inside is (i.e. acid Gas) be delivered to acid making system via sour gas pipeline (L3a) before, it is defeated from hot gas using hot gas branch pipe (L3a') Enter in pipe (L1a) or hot gas is exported from hot gas efferent duct (L1b), hot gas is flowed through sour gas pipeline (L3a) Come preheat the sour gas pipeline (L3a) (such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, more preferably 300-380 DEG C, more preferably 320-360 DEG C).

In addition, after activated carbon analyzing step terminates or including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops After fluid stopping peracidity gas pipeline (L3a), using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from adding Output hot gas, allows hot gas to purge the sour gas pipeline (L3a), to remove sour gas in hot gas efferent duct (L1b) The sour gas of residual in body pipeline (L3a).

Activated carbon analytically be sent into by top of tower, is discharged from tower bottom.Bringing-up section on Analytic Tower top, has adsorbed polluter Activated carbon is heated to more than 400 DEG C, and is kept for more than 3 hours, the SO being tightly held by activated carbon₂It is released, generation is " rich Sulphur gas (SRG) ", SRG are delivered to relieving haperacidity workshop section (or acid making system) and produce H₂SO₄.The NOX hairs being tightly held by activated carbon Raw SCR or SNCR reactions, while wherein bioxin is largely decomposed.Analytic Tower parses institute's calorific requirement by a hot-blast stove There is provided, after blast furnace gas burns in hot-blast stove, heat smoke (via pipeline L1a) is sent into the shell side of Analytic Tower.Hot gas after heat exchange (L1b) it is most of return in hot air circulation blower (another fraction is then outer to drain into air), hot-blast stove is sent into by it and is newly burnt High temperature hot gas mixes.Cooling section is provided with Analytic Tower bottom, blasting air via pipeline (L2a) takes the heat of activated carbon out of.It is cold But section is provided with cooling blower, blasts cold wind and cools down activated carbon, then outer to drain into air.The activated carbon warp that Analytic Tower comes out Activated carbon sieve screening is crossed, the tiny activated carbon granule and dust less than 1.2mm are removed, the adsorption capacity of activated carbon can be improved. Activated carbon sieve oversize is the strong activated carbon of adsorption capacity, and activated carbon is delivered to adsorption tower by activated carbon conveyer and recycled, Screenings then enters ash silo.Need to be protected with nitrogen in resolving, the SO that nitrogen will parse as carrier simultaneously₂ Taken out of Deng pernicious gas.Nitrogen is analytically passed through tower upper and lower part, and discharge is collected among Analytic Tower, while by activated carbon Adsorbed SO₂Take out of, and deliver to acid making system and go relieving haperacidity.When nitrogen is passed through above Analytic Tower, added with nitrogen heater Hot to 100 DEG C or so are passed through in Analytic Tower again.

Here, the primary adsorption tower of series connection and secondary absorption tower refer to：The exhanst gas outlet of primary adsorption tower is connected to two via pipeline The gas approach of level adsorption tower.

Design and its absorbing process for flue gas (or waste gas) adsorption tower, have had many documents to have been disclosed in the prior art, See, for example, US5932179, JP2004209332A, and JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A.The application is no longer described in detail.

In the present invention, for adsorption tower (T1) or for primary adsorption tower (T1) or secondary absorption tower (T2), single column list can be used Bed designs；Or the design of single-tower muiti-bed layer, such as inlet plenum (3)-desulphurized aetivated carbon bed (A)-denitration activity charcoal bed (B)-outlet Room, or such as inlet plenum (3)-desulphurized aetivated carbon bed (A)-desulphurization denitration active carbon bed (B)-denitration activity charcoal bed (C)-outlet Room.The more bed designs of symmetrical expression double tower can also be used, as shown in Figures 7 and 8.

In this application, primary adsorption tower (T1) is used as primary adsorption tower.Secondary absorption tower (T2) is used as secondary absorption tower.As The primary adsorption tower (T1) of primary adsorption tower can be used side by side with two or more.Secondary absorption tower as secondary absorption tower (T2) can also be used side by side with two or more.When symmetrical expression double tower using it is two or more side by side as primary adsorption tower when, Then the discharge chamber of each symmetrical expression double tower arranged side by side as primary adsorption tower be individually insulated into upper and lower two chambers (a, b) or on In lower three chambers (a, c, b), i.e. be divided into two levels or three levels, and, it is preferred that from the identical of different adsorption towers The pipeline of flue gas is discharged in the chamber of level can merge or converge.

In general, it is independently of one another for the primary adsorption tower (T1) in the application and the tower height of secondary absorption tower (T2), such as 10-50m, preferably 13-45m, preferably 15-40m, more preferably 18-35m.Primary adsorption tower (T1) and secondary absorption tower (T2) that This can use identical or different structure snd size, it is preferred to employ identical structure snd size.The tower height of adsorption tower refers to The height of the height, the i.e. agent structure of tower of activated carbon entrance at the top of adsorption tower is exported to from absorption tower bottom activated carbon.

In the present invention, do not required particularly for Analytic Tower, the Analytic Tower of prior art can be used in the present invention.It is preferred that , Analytic Tower is the vertical Analytic Tower of shell pipe type, and wherein activated carbon inputs from tower top, flows downwardly through tube side, then reaches tower Bottom, and hot gas then flows through shell side, hot gas enters from the side of tower, the activated carbon with flowing through tube side carry out heat exchange and Cooling, then exported from the opposite side of tower.In the present invention, do not required particularly for Analytic Tower, the parsing of prior art Tower can be used in the present invention.Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type (or package type), wherein activated carbon from Tower top inputs, and flows downwardly through the tube side of top heating zone, then reaches one and is between top heating zone and bottom cooling zone One cushion space, the tube side of bottom cooling zone is then flowed through, then reaches bottom of towe, and hot gas (or high-temperature hot-air) then flows The shell side in heated area, hot gas (400-450 DEG C) analytically the heating zone of tower side enter, with flowing through heating zone tube side Activated carbon carries out indirect heat exchange and cooled, and is then exported from the opposite side of the heating zone of tower.Cool down the cooling zone of wind analytically tower Side enter, with flow through cooling zone tube side parsed, regenerate activated carbon progress indirect heat exchange.Indirect heat exchange it Afterwards, cooling wind is warming up to 90-130 DEG C (such as from about 100 DEG C).

In general, generally there is the tower of 10-45m, preferably 15-40m, more preferably 20-35 rice for the Analytic Tower in the present invention It is high.Desorber generally has 6-100 ㎡, preferably 8-50 ㎡, more preferably 10-30 ㎡, further preferred 15-20 ㎡ main body Cross-sectional area.

In the present invention, " chamber of same level " refers to two or more adsorption towers, and the discharge chamber of each adsorption tower is divided into Upper and lower two chambers (or being divided into the chamber of upper, middle and lower three), the upper chamber of all adsorption tower discharge chambers are the chamber of same level Room, the middle chamber of all adsorption tower discharge chambers are also the chamber of same level, and similarly, the lower chambers of all adsorption tower discharge chambers are The chamber of same level.

" parse " and be used interchangeably with " regeneration " in this application.

Advantages of the present invention

1st, activated carbon analyzing step startup before or allowing including SO₂And NH₃Gas pollutant (i.e. sour gas) warp inside Before being delivered to acid making system by sour gas pipeline (L3a), with hot gas branch pipe (L3a') from hot gas input pipe (L1a) In or from the hot gas efferent duct (L1b) output hot gas is used to preheat the sour gas pipeline, and, parsed in activated carbon After step terminates, hot gas is allowed to purge the sour gas pipeline (L3a), to remove residual in sour gas pipeline (L3a) Sour gas.Corrosiveness of the sour gas to sour gas conveyance conduit can significantly be prevented.

2nd, the technique of the application and device are strong using the big detergent power of adsorption capacity of adsorption tower upper active charcoal, good purification, The characteristics of oxious component concentration after purification in flue gas is low, adsorption tower discharge chamber is divided into two layers up and down by a past entirety Or multilayer, the flue gas after being purified by adsorption tower is carried out segmentation according to degree of purification and enter different flues, be harmful into flue gas Part concentration flue up to standard is directly discharged into chimney, it is impossible to which the flue gas of qualified discharge then enters next stage adsorption tower or returns adsorption tower Entrance purifies again, so will reduce 30%~50% into the exhaust gas volumn of next stage, and can reduce booster fan and secondary absorption The ability of tower, so as to reduce investment and operating cost.

Brief description of the drawings

Fig. 1 is the desulfuring and denitrifying apparatus and process flow diagram that include activated carbon adsorber and regenerating active carbon tower of prior art.

Fig. 2 is the process flow diagram of the out of stock device of flue gas desulfurization (SUMITOMO CHEMICAL company) of prior art.

Fig. 3 is the process flow diagram of the out of stock device of another flue gas desulfurization (Shanghai Ke Liu companies) of prior art.

Fig. 4 is the process flow diagram of the flue gas desulfurization and denitrification device of first embodiment of the present invention.

Fig. 5 is the process flow diagram of the flue gas desulfurization and denitrification device of second embodiment of the present invention.

Fig. 6 is the process flow diagram of another flue gas desulfurization and denitrification device of second embodiment of the present invention.

Fig. 7 is the schematic diagram of the adsorption tower of the more beds of symmetrical expression double tower (gapless space between each bed) design of the present invention.

Fig. 8 is the schematic diagram of the adsorption tower of the more beds of symmetrical expression double tower (having clearance space between each bed) design of the present invention.

Reference

T1：Adsorption tower or primary adsorption tower；T2：Secondary absorption tower；1：The main body of adsorption tower；2：Active carbon material feeding storehouse；3 Or 3 '：Adsorption tower inlet plenum, 4：The discharge valve (or rotary valve) of adsorption tower Lower Hold；5：The roll-type feed of active carbon bed bottom Machine (or rotary valve)；6：Porous barrier；7：Booster fan；8、8a、8b：Activated carbon conveyer；9：Secondary absorption tower Discharge chamber；10：Switching valve.

A、B、C、D、E：Active carbon bed；a：Top discharge chamber, c：Middle part discharge chamber, b：Bottom discharge chamber；L1： Former flue gas conveying flue or the first flue；L2：Second flue (or neat stress conveyance conduit)；L3：3rd fume pipe Road；L4：4th flue；L5：5th flue.

T3：Desorber (or regenerator)；S1：Activated carbon vibratory sieve；N2：Nitrogen delivery pipe.

L1a：Hot gas input pipe；L1b：Hot gas efferent duct ()；L2a：Cooling gas input pipe；L2b：Cool down gas Body efferent duct；L3a：Sour gas conveyance conduit；L3a'：Hot gas branch pipe.

h:Adsorption section height.

Specific embodiment

The SO in all embodiments, former flue gas₂And NO_xContent be respectively 300mg/Nm³-4000mg/Nm³With 200 mg/Nm³-500mg/Nm³。

The embodiment of the application is described below：

2) regenerating active carbon tower (or Analytic Tower) (T3),

Typically, when primary adsorption tower (T1) has top discharge chamber (a) and bottom discharge chamber (b), top discharge chamber (a) and bottom go out The ratio between the height of both air chambers (b) in vertical direction is 0.7-1.3:1, preferably 0.8-1.2:1, preferably 0.9-1.1:1, such as 1:1. And when primary adsorption tower (T1) has top discharge chamber (a), middle part discharge chamber (c) and bottom discharge chamber (b), top discharge chamber (a), The ratio between middle part discharge chamber (c) and the height of bottom discharge chamber (b) three in vertical direction are 0.5-1.0:0.5-1.0:0.8-1, preferably 0.6-0.9:0.6-0.9:0.8-1, preferably 0.7-0.8:0.7-0.8:0.8-1.

Preferably, a hot gas branch pipe has been separated from sour gas conveyance conduit (L3a) initiating terminal (or front end) (L3a'), also, the other end (such as via valve) of the hot gas branch pipe (L3a') connects with hot gas input pipe (L1a) And/or connected with hot gas efferent duct (L1b) so that the hot gas branch pipe (L3a') is used as from hot gas input pipe (L1a) On the branch pipe that separates or as the branch pipe separated from hot gas efferent duct (L1b).

It is preferred that the rotating speed by adjusting primary adsorption tower (T1) bed bottom discharge valve (5), active in primary adsorption tower (T1) to adjust The residence time of activated carbon or speed is moved down in charcoal bed so that the dirt of the flue gas in the top discharge chamber (a) of primary adsorption tower (T1) Thing content is contaminated in the range of meeting the requirements or meeting regulation.That is, limit value of the content less than setting.

I) desulphurization and denitration step：

With

It is preferred that primary adsorption tower (T1) can be used side by side with two or more (such as 2-6, such as 3 or 4)；And/or Secondary absorption tower (T2) can be used with two or more (such as 2-4, such as 3) side by side.

In the method according to the third and fourth embodiment, it is preferred that by adjusting unloading for adsorption tower active carbon bed bottom Valve (5) is expected to adjust residence time of the activated carbon in active carbon bed, it is ensured that from adsorption tower (T1) top discharge chamber (a) Or pollutant load is conforming in the flue gas of discharge from the top discharge chamber (a) and middle part discharge chamber (c) of primary adsorption tower (T1) In the range of asking or meeting regulation.

It is preferred that the rotating speed or aperture of the discharge valve (5) by adjusting primary adsorption tower (T1) active carbon bed bottom, to adjust one The residence time of activated carbon or speed is moved down in active carbon bed so that the top outlet of primary adsorption tower (T1) in level adsorption tower (T1) The pollutant load of flue gas in room (a) and optionally the pollutant load of the flue gas in middle part discharge chamber (c) is being met the requirements Or in the range of meeting regulation.That is, limit value of the content less than setting.

In this application, activated carbon is adjusted in active carbon bed by adjusting primary adsorption tower (T1) bed bottom discharge valve (5) In residence time, it is ensured that the top discharge chamber from primary adsorption tower (T1) top discharge chamber (a) or from primary adsorption tower (T1) (a) pollutant load is in the range of meeting the requirements or meeting regulation in the flue gas and in middle part discharge chamber (c) discharged.

In addition, in the prior art, when activated carbon analyzing step starts, hot sour gas at the beginning or is flowing through cold (example early stage Such as be in environment temperature) sour gas pipeline (L3a) when and cause temperature to reduce, so as to condense, formed liquid acid, liquid Acid has strong corrosion effect to sour gas pipeline (L3a).In order to solve this problem, typically in sour gas pipeline (L3a) outside Set sleeve pipe and outermost layer that heat-insulation layer is set in week.Ensure that sour gas is flowing through by being passed through the hot gas of high temperature in sleeve pipe Temperature during sour gas pipeline (L3a) is higher than dew point, i.e. allows acidic components to keep gaseous state.

In the present invention, for adsorption tower (T1) or for primary adsorption tower (T1) or secondary absorption tower (T2), single column list can be used Bed designs；Or the design of single-tower muiti-bed layer, such as inlet plenum (3)-desulphurized aetivated carbon bed (A)-denitration activity charcoal bed (B)-outlet Room or such as inlet plenum (3)-desulphurized aetivated carbon bed (A)-desulphurization denitration active carbon bed (B)-denitration activity charcoal bed (C)-discharge chamber. Symmetric double Deethanizer design can also be used, as shown in Fig. 7 or 8.

Design and regeneration method of active carbon for activated carbon Analytic Tower, have had many documents to have been disclosed in the prior art, JP3217627B2 (JPH08155299A) discloses a kind of Analytic Tower (i.e. desorber), and it uses double seal valve, leads to noble gas sealing, Screening, water cooling (referring to Fig. 3 in the patent).JP3485453B2 (JPH11104457A) disclose regenerator (referring to Figure 23 and 24) preheating section, can be used, double seal valve, leads to noble gas, air cooling or water cooling.JPS59142824A is disclosed from cooling The gas of section is used to preheat activated carbon.Chinese patent application 201210050541.6 (Shanghai Ke Liu companies) discloses the energy of regenerator The scheme recycled is measured, which uses drier 2.JPS4918355B is disclosed using blast furnace gas (blast furnace gas) Carry out regenerated carbon.JPH08323144A discloses the regenerator using fuel (heavy oil or light oil), uses air-heating furnace (ginseng See Fig. 2 of the patent, 11- hot-blast stoves, 12- fuel supply systems).Chinese utility model 201320075942.7 is related to heating dress The emission-control equipment (coal-fired, air heating) of the heater is put and possesses, referring to Fig. 2 in the utility model patent.

The Analytic Tower of the present invention is using air-cooled.

Situation for Analytic Tower analytic ability for 10t activated carbons per hour, traditional handicraft keep the temperature in Analytic Tower 420 Coke-stove gas needed for DEG C is about 400Nm³/ h, combustion air are about 2200Nm³/ h, outer thermal wind exhausting are about 2500Nm³/h；It is required Cooling air 30000Nm³/ h, activated carbon temperature is 140 DEG C after cooling.

Embodiment 1

Using the device and flow shown in Fig. 4.

Embodiment 2

Using the device and flow shown in Fig. 4, still, with the suction shown in the adsorption tower device alternate figures 4 shown in Fig. 7 Attached tower.

Embodiment 3

Using the device and flow shown in Fig. 5.

Embodiment 4

Using the device and flow shown in Fig. 5, still, with two shown in the adsorption tower device alternate figures 5 shown in Fig. 7 Level adsorption tower.

Embodiment 5 (preferably)

Using the device and flow shown in Fig. 6.

Embodiment 6 (preferably)

Using the device and flow shown in Fig. 6, still, with two shown in the adsorption tower device alternate figures 5 shown in Fig. 7 Level adsorption tower.

Embodiment 7 (most preferably)

Using the device and flow shown in Fig. 6, still, with two shown in the adsorption tower device alternate figures 5 shown in Fig. 7 Level adsorption tower.And primary adsorption tower has 3 to be set up in parallel, the flue gas exit pipe of the smoke chamber of the same level of primary adsorption tower Road converges, and flue gas is divided into two strands of inlet plenums for each leading into 2 secondary absorption towers arranged side by side afterwards.From secondary absorption tower (T2) Discharge chamber measures：99.2% desulfurization degree and 92% denitration rate.

Claims

1. a kind of flue gas desulfurization and denitrification device, it includes primary adsorption tower (T1) and regenerating active carbon tower (or Analytic Tower) (T3), wherein Activated carbon Analytic Tower (T3) has heating zone, the buffering area at middle part and the cooling zone of bottom on top, in the downside of top heating zone Portion and upper lateral part are connected to hot gas input pipe (L1a) and hot gas efferent duct (L1b) respectively, in the downside of bottom cooling zone Portion and upper lateral part are connected to cooling gas input pipe (L2a) and cooling gas efferent duct (L2b) respectively, analytically in the middle part of tower (T3) The sour gas conveyance conduit (L3a) that buffering area sidepiece is drawn is connected to acid making system, it is characterised in that：From sour gas delivery pipe The initiating terminal (or front end) in road (L3a) has separated a hot gas branch pipe (L3a'), also, the hot gas branch pipe (L3a') The other end connect with hot gas input pipe (L1a) or connected with hot gas efferent duct (L1b) so that the hot gas branch pipe (L3a') as the branch pipe separated from hot gas input pipe (L1a) or as the branch separated from hot gas efferent duct (L1b) Pipe；

2. device according to claim 1, it is characterised in that：Discharge chamber is divided into top discharge chamber (a) and bottom discharge chamber (b), wherein the second flue (L2) for the pure flue gas of output from top discharge chamber (a) is communicated to blowdown stack, and use The upstream of inlet plenum (3) is returned in the 3rd flue (L3) of the output flue gas from bottom discharge chamber (b) and former flue gas conveying flue is First flue (L1) merges or converged.

3. device according to claim 1 or 2, wherein primary adsorption tower (T1) have an active carbon bed, two work Property charcoal bed or multiple active carbon beds (A, B, C), preferably 2-5 bed；Described two or multiple active carbon beds are by porous plate Separate to be formed.

4. a kind of flue gas desulfurization and denitrification device, it includes:

1) the primary adsorption tower (T1) and secondary absorption tower (T2) of series connection, and

2) regenerating active carbon tower (or Analytic Tower) (T3),

5. device according to claim 4, it is characterised in that：The discharge chamber of primary adsorption tower (T1) is divided into top outlet Room (a), bottom discharge chamber (b), wherein the second flue (L2) for the pure flue gas of output from top discharge chamber (a) is connected To blowdown stack, the 3rd flue (L3) for the output flue gas from bottom discharge chamber (b) is communicated to secondary absorption tower (T2) Inlet plenum (3 '), and optionally, the 4th flue (L4) of output flue gas and the from secondary absorption tower (T2) discharge chamber (9) Two flues (L2) merge or lead to blowdown stack after converging；Or

6. the device according to claim 4 or 5, wherein primary adsorption tower (T1) or secondary absorption tower (T2) are independently of one another With an active carbon bed, two active carbon beds or multiple active carbon beds (A, B, C), preferably 2-5 bed；Described two Individual or multiple active carbon beds are separated by porous plate to be formed；

And/or

7. according to the device any one of claim 1-6, wherein primary adsorption tower (T1) can with it is two or more simultaneously Row use and/or secondary absorption tower (T2) can also be used side by side with two or more；It is preferred that primary adsorption tower arranged side by side Discharge chamber is individually insulated into three chambers (a, c, b) of upper and lower two chambers (a, b) or upper, middle and lower, i.e. is divided into two levels or three layers Level, and, it is further preferred that the pipeline of flue gas is discharged from the chamber of the same level of different adsorption towers can merge or converge；

Preferably, when the primary adsorption tower (T1) of symmetrical expression double tower form is with two or more primary adsorption towers arranged side by side, then The discharge chamber of each symmetrical expression double tower as primary adsorption tower arranged side by side is individually insulated into upper and lower two chambers (a, b) or upper Lower three chambers (a, c, b), i.e. it is divided into two levels or three levels, and, it is further preferred that the identical layer from different adsorption towers The pipeline of flue gas is discharged in the chamber of level can merge or converge.

8. usage right requires the flue gas desulfurization and denitration method of the desulfuring and denitrifying apparatus any one of 1-3 or 7, this method Comprise the following steps：

It is characterized in that：Allowing including SO₂And NH₃Gas pollutant (i.e. sour gas) inside is via sour gas pipeline (L3a) It is delivered to before acid making system, is exported using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas Output hot gas in (L1b) is managed, hot gas is flowed through sour gas pipeline (L3a) to preheat the sour gas pipeline (L3a) (such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, more preferably 300-380 DEG C, more preferably 320-360℃)；With optionally, including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops running through sour gas After body pipeline (L3a), using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) output hot gas, allows hot gas to purge the sour gas pipeline (L3a), to remove sour gas pipeline (L3a) in The sour gas of middle residual.

9. according to the method for claim 8, wherein I) desulphurization and denitration step is carried out as follows：Former flue gas is via the first cigarette Feed channel (L1) flows successively through primary adsorption tower (T1) one or more after being transported in primary adsorption tower (T1) inlet plenum (3) Active carbon bed, flue gas carries out cross-current type contact with the activated carbon added at the top of primary adsorption tower (T1), wherein contained by flue gas Pollutant (such as oxysulfide, nitrogen oxides, dust, dioxin) is removed or partly removed by activated carbon, and flue gas enters afterwards Enter into the top discharge chamber (a) and bottom discharge chamber (b) of primary adsorption tower (T1), from primary adsorption tower (T1) top discharge chamber (a) The flue gas of middle discharge is delivered to blowdown stack to be discharged via the second flue (L2), from primary adsorption tower (T1) bottom The flue gas containing a small amount of pollutant of discharge returns and the first flue (L1) via the conveying of the 3rd flue (L3) in discharge chamber (b) In former flue gas converge, and adsorbed the activated carbon of pollutant and then discharged from primary adsorption tower (T1) bottom；Preferably, upper While stating operation, dilution ammonia is passed through in the flue gas input channel (L1) of primary adsorption tower (T1) and is optionally passed into one-level In adsorption tower (T1).

10. usage right requires the flue gas desulfurization and denitration method of the desulfuring and denitrifying apparatus any one of 4-7, this method bag Include following steps：

I) desulphurization and denitration step：

With

It is characterized in that：Allowing including SO₂And NH₃Gas pollutant (i.e. sour gas) inside is via sour gas pipeline (L3a) It is delivered to before acid making system, is exported using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas Output hot gas in (L1b) is managed, hot gas is flowed through sour gas pipeline (L3a) to preheat the sour gas pipeline (L3a) (such as be preheated to 250-450 DEG C temperature, preferably 280-400 DEG C, more preferably 300-380 DEG C, more preferably 320-360℃)；With optionally, including SO₂And NH₃Gas pollutant (i.e. sour gas) inside stops running through sour gas After body pipeline (L3a), using hot gas branch pipe (L3a') from hot gas input pipe (L1a) or from hot gas efferent duct (L1b) output hot gas, allows hot gas to purge the sour gas pipeline (L3a), to remove sour gas pipeline (L3a) in The sour gas of middle residual；It is preferred that primary adsorption tower (T1) can be used side by side with two or more；And/or secondary absorption Tower (T2) can be used side by side with two or more.

11. according to the method for claim 10, wherein I) desulphurization and denitration step is carried out as follows：

12. according to the method any one of claim 8-11, wherein by adjusting adsorption tower active carbon bed bottom Discharge valve (5) adjusts residence time of the activated carbon in active carbon bed, it is ensured that from the top discharge chamber of primary adsorption tower (T1) (a) pollutant load exists in or from the top discharge chamber (a) and middle part discharge chamber (c) of primary adsorption tower (T1) in the flue gas of discharge In the range of meeting the requirements or meeting regulation.