CN107398155A - Low-temp desulfurization denitrating system in a kind of coking of coal - Google Patents

Low-temp desulfurization denitrating system in a kind of coking of coal Download PDF

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Publication number
CN107398155A
CN107398155A CN201710730471.1A CN201710730471A CN107398155A CN 107398155 A CN107398155 A CN 107398155A CN 201710730471 A CN201710730471 A CN 201710730471A CN 107398155 A CN107398155 A CN 107398155A
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ammonia
flue gas
coking
electron
temperature
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李绍明
李波
李斌
李少洪
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Pingxiang Huaxing Chemical Equipment Packing Co Ltd
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Pingxiang Huaxing Chemical Equipment Packing Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8628—Processes characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/202—Alkali metals
    • B01D2255/2022—Potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/202—Alkali metals
    • B01D2255/2027—Sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/204—Alkaline earth metals
    • B01D2255/2045—Calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20707—Titanium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20723—Vanadium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20769—Molybdenum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20776—Tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/209—Other metals
    • B01D2255/2092—Aluminium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/30—Silica
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

Abstract

The invention discloses low-temp desulfurization denitrating system in a kind of coking of coal, it is characterised in that：Including ammonia tank, evaporator, blender, dilution air, preheater, SCR reactors, compressor reducer, heater, temperature controller and electron beam processor, SCR reactors include being located at reaction cavity, ammonia-spraying grid, catalyst and thermostatic control chamber, ammonia-spraying grid is connected with heater, preheater, electron beam processor includes upper process chamber and lower process chamber, power supply and multiple electron accelerators in parallel are provided with upper process chamber, for lower process chamber formed with electron reaction chamber, catalyst main component is TiO by weight percentage275~81%, WO37~11%, MO30.5~1%, V2O50~3%, SiO26~9%, Al2O31~2%, CaO 0.5~2%, Na2O 0~0.5%, K2O 0~0.5%.

Description

Low-temp desulfurization denitrating system in a kind of coking of coal
Technical field
The present invention relates to coking of coal fume treatment field, more particularly to low-temp desulfurization denitrating system in a kind of coking of coal.
Background technology
Coking of coal is also known as coal high-temperature retorting.Using coal as raw material, in the case where completely cutting off air conditionses, 950 DEG C or so are heated to, warp High-temperature retorting produces coke, while obtains coal gas, coal tar and a kind of coal conversion process for reclaiming other chemical products.It is same in this Caused flue gas pollutant, include SO2, NOx, CO2, Hg etc., be environment protection, it is necessary to handle flue gas after It could discharge.
According to Processing tecchnics in sulfur removal technology, dry desulfurization, wet desulphurization and semi-dry desulphurization are segmented into.Dry method takes off Sulphur：Important is circulating fluid bed reactor desulfurization.After lime stone adds CFBB, two step high-temperature gas-solids will occur Reaction：Combustion decomposition is reacted and sulfosaltization reaction, by the two reactions come desulfurization.
Wet desulphurization：Limestone/lime-gypsum wet, boiler smoke are pressurized through booster fan, are handed over by gas-gas heat Enter desulfurizing tower after the cooling of parallel operation exchanged heat, flow through desulfurizing tower from bottom to top, formed with top-down limestone/lime slurries Reverse flow, while heat exchange and chemical reaction occurs, remove the SO2 in flue gas.Flue gas after purification removes through demister The drop carried in flue gas, discharged after being heated up by airair heat exchanger from chimney.Reaction product CaSO3 enters desulfurizing tower The slurry pool of bottom, the air blasted by oxygenation blower fan force oxidation, generate CaSO4, then generate gypsum.In order that slurry Calcium sulfate in liquid pool keeps certain concentration, and the gypsum of generation need to be discharged constantly, and fresh limestone/lime slurries need continuous Supplement, calcium plaster obtain the higher gypsum of purity after dehydration.
Semi-dry desulphurization：Spray dryer flue gas desulfurization and circulating fluid bed flue-gas desulfurizing (can also be semidry method, finally Processing is different).Lime mixes in digester after digestion with desulfurizing byproduct and part coal ash after crushing, and mixing is made Slurries, boosted through slurries pump and be sent into rotary sprayer, it is dispersed in tower after atomization.Heat smoke tangentially enters cigarette from tower top Qi leel orchestration, while gone downstream with droplet.SO2 in chemical reaction absorption flue gas occurs while evaporation drying for droplet.
According to Processing tecchnics in denitrating technique, Dry denitration and wet denitration are segmented into.Choosing popular at present Selecting property catalytic reduction method (SCR) and non-selective catalytic reduction (SNCR).Wherein, SCR is in the presence of catalyst, is utilized Reducing agent (liquefied ammonia, ammoniacal liquor or urea) generates harmless ammonia and water with the NOx reactions in flue gas, so as to remove in flue gas NOx.Selectivity refers to that in the effect of catalyst and under oxygen existence condition NH3 is preferential and reduction elimination reaction occurs for NOx, Nitrogen and water are generated, and the oxygen in flue gas of getting along well carries out oxidation reaction.In the presence of catalyst, selective catalytic reduction (SCR) reaction temperature is between 230~350 DEG C.And temperature is usually 180 DEG C or so after the recovery of China's waste heat of coke-oven flue gas, It is not reaching to the Active pharmaceutical of catalyst.
The content of the invention
The technical problem to be solved in the present invention is the present situation for prior art, there is provided low-temp desulfurization takes off in a kind of coking of coal Nitre system, realize the desulfurization to flue gas and denitrating technique.
Technical scheme is used by the present invention solves above-mentioned technical problem：Low-temp desulfurization denitration system in a kind of coking of coal System, it is characterised in that：Evaporator including the ammonia tank for storing liquefied ammonia, for realizing liquid ammonia gasification, for by ammonia and Blender that air is mixed, for introducing air into the dilution air, preheating that realization is diluted to ammonia in blender Device, SCR reactors, for flue gas is compressed compressor reducer, to flue gas part heating heater, for controlling SCR to react The temperature controller and electron beam processor of temperature, ammonia tank are connected with evaporator in device, and wherein the one of evaporator and blender Individual entrance point is connected, and dilution air is connected with another entrance point of blender, and the port of export of blender is connected with preheater, Need flue gas to be processed be connected with compressor reducer, compressor reducer is connected with heater, the SCR reactors including be located at reaction cavity, Ammonia-spraying grid positioned at reaction cavity top, the catalyst being filled in reaction cavity and take shape in reaction cavity peripheral part Thermostatic control chamber, the ammonia-spraying grid upper end are connected with heater, and ammonia-spraying grid sidepiece is connected with preheater, temperature controller with Thermostatic control chamber is connected, and the electron beam processor includes upper process chamber and lower process chamber, be provided with upper process chamber power supply and Multiple electron accelerators in parallel, each electron accelerator have electrospray mouth, and lower process chamber is formed with electron reaction chamber, electricity The side of sub- reaction chamber connects with the port of export of evaporator and connected with the outlet at bottom of SCR reactors, electron reaction respectively The opposite side connection chimney of chamber, the catalyst main component is TiO by weight percentage275~81%, WO37~ 11%, MO30.5~1%, V2O50~3%, SiO26~9%, Al2O31~2%, CaO 0.5~2%, Na2O 0~ 0.5%, K2O 0~0.5%.
Preferably, the heating-up temperature of the heater is 230~350 DEG C.
Preferably, the heating-up temperature of the preheater is 230~350 DEG C.
Preferably, the temperature that controls of the temperature controller is 300~400 DEG C.
Further, the flue gas first passes through deduster before compressor reducer is entered.
Preferably, the ratio of the NH3 and NO are 1.
Compared with prior art, the advantage of the invention is that：Temperature is usual after being reclaimed due to waste heat of coke-oven flue gas of the present invention For 180 DEG C or so, and the reaction temperature of catalyst is not reaching to the Active pharmaceutical of catalyst, this hair between 230~350 DEG C It is bright to need flue gas to be processed to be compressed using compressor reducer, on the one hand nitrogen oxides and oxysulfide in raising unit volume Concentration, be on the other hand favorably improved the temperature of flue gas, meanwhile, using heater to flue gas enter SCR reactors before carry out Heating so that flue gas is close to catalyst reaction temperatures, in addition, the present invention is using ammonia as the common reducing agent of desulfurization and denitration, The canned truck transport of reducing agent, is stored in ammonia tank with liquid form, and liquid ammonia is before SCR system flue gas is injected via steaming Device evaporation gasification is sent out, the ammonia and diluent air of gasification mix, meanwhile, preheated by preheater so that reducing agent and air mixing Gas is sprayed into the flue gas of SCR reactors upper ends by ammonia-spraying grid close to the catalytic temperature of catalyst, meanwhile, utilize temperature Controller is controlled to the temperature in the reaction cavity of SCR reactors, flue gas, reducing agent and catalyst in SCR reactors The temperature control of reaction cavity within the scope of preferable temperature, in SCR reactors urge by reducing agent and flue gas after being sufficiently mixed Reacted in the presence of agent, remove NOx, finally, the flue gas for eliminating NOx enters back into the electron reaction of electron beam processor Chamber, meanwhile, enter electron reaction intracavitary together from the ammonia that evaporator comes out as reducing agent, the electronics above electron reaction chamber Accelerator sprays substantial amounts of electronics to electron reaction intracavitary, realizes the desulfurization process to flue gas, meanwhile, electron accelerator also has Certain denitration function, so as to further carry out denitration to the residual NOx in flue gas.
Brief description of the drawings
Fig. 1 is the structural representation of low-temp desulfurization denitrating system in coking of coal in the embodiment of the present invention.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing embodiment.
Embodiment 1
As shown in figure 1, low-temp desulfurization denitrating system in coking of coal in this implementation, including for storing the ammonia tank of liquefied ammonia 1st, for realize liquid ammonia gasification evaporator 2, for ammonia and air are mixed blender 3, for introducing air into Realize in blender 3 dilution air 4 being diluted to ammonia, preheater 7, SCR reactors 5, for being compressed to flue gas Compressor reducer 10, to flue gas part heating heater 9, temperature controller 8 and electronics for controlling temperature in SCR reactors 5 Beam processor 6.
Wherein, ammonia tank 1 is connected with evaporator 2, and evaporator 2 is connected with one of entrance point of blender 3, dilutes wind Machine 4 is connected with another entrance point of blender 3, and the port of export of blender 3 is connected with preheater 7, it is preferable that the preheating The heating-up temperature of device 7 be 230~350 DEG C, it is necessary to processing flue gas first pass through deduster 11 after be connected with compressor reducer 10, compressor reducer 10 are connected with heater 9, it is preferable that the heating-up temperature of heater 9 is 230~350 DEG C, and SCR reactors 5 include being located at reaction chamber Body 53, the ammonia-spraying grid 51 positioned at the top of reaction cavity 53, the catalyst 52 being filled in reaction cavity 53 and take shape in anti- Answer the thermostatic control chamber 54 of the peripheral part of cavity 53, the upper end of ammonia-spraying grid 51 is connected with heater 9, the sidepiece of ammonia-spraying grid 51 with Preheater 7 is connected, and temperature controller 8 is connected with thermostatic control chamber 54, it is preferable that the temperature that controls of the temperature controller 8 is 300~400 DEG C, electron beam processor 6 includes upper process chamber 61 and lower process chamber 62, and the He of power supply 63 is provided with upper process chamber 61 Multiple electron accelerators 64 in parallel, each electron accelerator 64 have electrospray mouth, and lower process chamber 62 is formed with electron back Chamber 621 is answered, the side of electron reaction chamber 621 connects with the port of export of evaporator 2 and gone out with the bottom of SCR reactors 5 respectively Mouth connection, the opposite side connection chimney 12 of electron reaction chamber 621.
The main component of catalyst 52 is TiO by weight percentage275~81%, WO37~11%, MO30.5~ 1%, V2O50~3%, SiO26~9%, Al2O31~2%, CaO 0.5~2%, Na2O 0~0.5%, K2O 0~ 0.5%.Research finds WO3With MoO3The heat endurance of catalyst 52 can be improved, and V can be improved2O5With TiO2Between electronics Effect, improve activity, selectivity and the mechanical strength of catalyst 52, in addition, MoO3The anti-of catalyst 52 can also be strengthened As2O3Poisoning capability, catalyst carrier primarily serve support, the scattered, effect of stable catalytic activity material, while TiO2Itself Also there is faint catalytic capability, from the TiO of Detitanium-ore-type2As the carrier of SCR catalyst 52, with other oxides (such as Al2O3、ZrO2) carrier compares, TiO2Suppress SO2The ability of oxidation is strong, can disperse the vanadium species and TiO on surface well2Half Conductor essence.
In addition, being provided with NO concentration detector in compressor reducer 10, NH is provided with blender 33Concentration Testing Device, by controlling the concentration of the NO in compressor reducer 10 and controlling NH in blender 33Concentration, realize NH3Connect with NO proportioning Nearly 1, so as at utmost improve catalytic effect.
Temperature is usually 180 DEG C or so after being reclaimed due to waste heat of coke-oven flue gas of the present invention, and the reaction temperature of catalyst 52 Between 230~350 DEG C, the Active pharmaceutical of catalyst 52 is not reaching to, the present invention will need cigarette to be processed using compressor reducer 10 Gas is compressed, and is on the one hand improved the concentration of nitrogen oxides and oxysulfide in unit volume, is on the other hand favorably improved cigarette The temperature of gas, meanwhile, flue gas is heated before SCR reactors 5 are entered using heater 9 so that flue gas is close to catalyst 52 reaction temperatures, in addition, of the invention using ammonia as the common reducing agent of desulfurization and denitration, the canned truck transport of reducing agent, It is stored in liquid form in ammonia tank 1, liquid ammonia evaporates via evaporator 2 and gasified before SCR reactors 5 are injected, gasification Ammonia and diluent air mixing, meanwhile, preheated by preheater 7 so that reducing agent and air gas mixture are close to catalyst 52 Catalytic temperature, sprayed into by ammonia-spraying grid 51 in the flue gas of the upper end of SCR reactors 5, meanwhile, it is anti-to SCR using temperature controller 8 The temperature in the reaction cavity 53 of device 5 is answered to be controlled, flue gas, reducing agent and catalyst reaction cavity 53 in SCR reactors 5 Temperature control within the scope of preferable temperature, reducing agent and flue gas after the being sufficiently mixed catalyst 52 in SCR reactors 5 Reacted under effect, remove NOx, finally, the flue gas for eliminating NOx enters back into the electron reaction chamber of electron beam processor 6 621, meanwhile, enter together in electron reaction chamber 62 from the ammonia that evaporator 2 comes out as reducing agent, on electron reaction chamber 621 The electron accelerator 64 of side sprays substantial amounts of electronics into electron reaction chamber 621, realizes the desulfurization process to flue gas, meanwhile, electricity Sub- accelerator 64 also has certain denitration function, so as to further carry out denitration to the residual NOx in flue gas.
Further, electronics is to the SOx in flue gas and NOx cutting mechanisms：
Mainly 3 stages of experience,
(1) in the presence of electron beam, the main component in flue gas is ionized or excited, and produces the very strong freedom of oxidisability Base, such as OH, O, HO2Deng；
(2) free radical caused by aoxidizes the SO in flue gas at a terrific speed2, NOx, generate the oxysulfide and nitrogen of high price Oxide, generation sulfuric acid and nitric acid etc. are then acted on water；
(3) sulfuric acid of generation and nitric acid and the ammonia added in advance carry out neutralization reaction, generate ammonium sulfate and ammonium nitrate particulate； Unreacted ammonia continues thermal chemical reaction generation ammonium sulfate in the gas flow in flue gas.
H2SO4+2NH3→(NH4)2SO4
HNO3+NH3→NH4NO3
SO2+2NH3+H2O+1/2O2→(NH4)2SO4
Embodiment 2
Embodiment 2 with embodiment 1, wherein, the main component of catalyst 52 is TiO by weight percentage275%, WO3 7%, MO30.5%, SiO26%, Al2O31%, CaO 0.5%.The heating-up temperature of preheater 7 is 230 DEG C；Heater 9 Heating-up temperature is 230 DEG C；The temperature that controls of temperature controller 8 is 300 DEG C.
Embodiment 3
Embodiment 3 with embodiment 1, wherein, the main component of catalyst 52 is TiO by weight percentage277%, WO3 9%, MO30.6%, V2O51%, SiO27%, Al2O31.5%, CaO 1%, Na2O 0.2%, K2O 0.3%.Preheater 7 Heating-up temperature be 280 DEG C；The heating-up temperature of heater 9 is 280 DEG C；The temperature that controls of temperature controller 8 is 320 DEG C.
Embodiment 4
Embodiment 4 with embodiment 1, wherein, the main component of catalyst 52 is TiO by weight percentage278%, WO3 10%, MO30.8%, V2O52%, SiO28%, Al2O31.8%, CaO 1.5%, Na2O 0.4%, K2O 0.4%.Preheating The heating-up temperature of device 7 is 300 DEG C；The heating-up temperature of heater 9 is 300 DEG C；The temperature that controls of temperature controller 8 is 380 DEG C.
Embodiment 5
Embodiment 5 with embodiment 1, wherein, the main component of catalyst 52 is TiO by weight percentage281%, WO3 11%, MO31%, V2O53%, SiO29%, Al2O32%, CaO 2%, Na2O 0.5%, K2O 0.5%.Preheater 7 Heating-up temperature is 350 DEG C；The heating-up temperature of heater 9 is 350 DEG C；The temperature that controls of temperature controller 8 is 400 DEG C.

Claims (6)

  1. A kind of 1. low-temp desulfurization denitrating system in coking of coal, it is characterised in that：Including the ammonia tank for storing liquefied ammonia, for reality The evaporator of existing liquid ammonia gasification, the blender, real in blender for introducing air into for ammonia and air to be mixed The dilution air that is now diluted to ammonia, preheater, SCR reactors, for flue gas is compressed compressor reducer, to flue gas Heater, the temperature controller and electron beam processor for controlling SCR reactor temperatures of part heating, ammonia tank and evaporation Device is connected, and evaporator is connected with one of entrance point of blender, another entrance point phase of dilution air and blender Even, the port of export and preheater of blender are connected, it is necessary to which the flue gas of processing is connected with compressor reducer, and compressor reducer is connected with heater, The SCR reactors include positioned at reaction cavity, the ammonia-spraying grid positioned at reaction cavity top, are filled in urging in reaction cavity Agent and the thermostatic control chamber for taking shape in reaction cavity peripheral part, the ammonia-spraying grid upper end are connected with heater, spray ammonia lattice Grid sidepiece is connected with preheater, and temperature controller is connected with thermostatic control chamber, the electron beam processor include upper process chamber and Lower process chamber, power supply and multiple electron accelerators in parallel is provided with upper process chamber, each electron accelerator has electronics spray Loophole, lower process chamber connected respectively with the port of export of evaporator formed with electron reaction chamber, the side of electron reaction chamber and and The outlet at bottom connection of SCR reactors, the opposite side connection chimney of electron reaction chamber, the catalyst main component is with weight hundred Ratio is divided to be calculated as TiO275~81%, WO37~11%, MO30.5~1%, V2O50~3%, SiO26~9%, Al2O31~ 2%, CaO 0.5~2%, Na2O 0~0.5%, K2O 0~0.5%.
  2. 2. low-temp desulfurization denitrating system in coking of coal according to claim 1, it is characterised in that：The heating of the heater Temperature is 230~350 DEG C.
  3. 3. low-temp desulfurization denitrating system in coking of coal according to claim 2, it is characterised in that：The heating of the preheater Temperature is 230~350 DEG C.
  4. 4. low-temp desulfurization denitrating system in coking of coal according to claim 3, it is characterised in that：The temperature controller It is 300~400 DEG C to control temperature.
  5. 5. low-temp desulfurization denitrating system in coking of coal according to claim 1, it is characterised in that：The flue gas is entering pressure Deduster is first passed through before contracting device.
  6. 6. low-temp desulfurization denitrating system in the coking of coal according to any one of claim 1 to 5, it is characterised in that：The NH3 Ratio with NO is 1.
CN201710730471.1A 2017-08-23 2017-08-23 Low-temp desulfurization denitrating system in a kind of coking of coal Pending CN107398155A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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CN108479326A (en) * 2018-03-12 2018-09-04 东北师范大学 Mutually vertical reflecting electron beam resonance snowslide sulphur removal nitre system
CN108404931A (en) * 2018-05-16 2018-08-17 江苏浩日朗环保科技有限公司 Compound SCR denitration catalyst and preparation method thereof

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