CN1332029A - Semi-dry fume-purifying linear pulse electron beam method - Google Patents
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- CN1332029A CN1332029A CN00109849A CN00109849A CN1332029A CN 1332029 A CN1332029 A CN 1332029A CN 00109849 A CN00109849 A CN 00109849A CN 00109849 A CN00109849 A CN 00109849A CN 1332029 A CN1332029 A CN 1332029A
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Abstract
The present invention relates to the method of removing SOx and/or NOx from smoke. High temperature smoke from factory, after being dedusted, is first spilled in a spray drier to lower temperature and increase humidity while collecting large particle over 100 microns and small particle below 100 microns, and then is mixed with heated ammonia, reacted in a radiator under the radiation of electronic beam produced by a linear pulse accelerator, and spilled with solution in a wet electrostatic duster to dissolve ammonia sulfate and/or ammonia nitrate. The method of the present invention has low power consumption, small volume of equipment, no effluent resulting in secondary pollution and less ammonia leakage.
Description
The present invention relates to remove the method for flue gas sulphur oxide and/or nitrogen oxide, it is a kind of by injecting ammonia more specifically to say so, and utilizes pulsed electron beam with oxysulfide and/or the conversion of nitrogen oxides flue gas cleaning treatment method for the low energy consumption of chemical fertilizer.
Along with the coal combustion high coal of sulfur-bearing particularly, the flue gas that is produced has brought severe contamination to environment, and flue gas desulfurization has become the important topic of environmental improvement.The method of flue gas desulfurization has a variety of.But a lot of methods can produce a large amount of waste water and waste residue when removing sulfur dioxide in flue gas, need the flower substantial contribution that these waste water and waste residue are handled once more, otherwise can produce secondary pollution to environment.The electron beam flue gas purifying method is a kind of advanced person's of present flue gas desulfurization a method.It does not produce waste water, waste residue, and the byproduct of generation can be made chemical fertilizer, can not produce secondary pollution to environment, and flue gas can also remove nitrogen oxide and volatile organic matter (VOC) in the process of desulfurization, is the flue gas desulfurization new and high technology of 21st century.
The processing method of electron beam flue gas has two kinds at present: a kind of is dry method, and another kind is a semidry method.
Chinese patent literature CN1225035A has introduced the purification method of electron beam dry method flue gas.This method is the high-temperature flue gas that comes out from boiler, use earlier the heat exchanger cooled flue gas, in cooling tower, high-temperature flue gas is sprayed water again, with flue gas cool-down, humidification, in radiation chamber, ammonia, water, the mixed flue gas of air are shone with electron beam, complicated chemical reaction takes place with ammonia, water, oxygen in oxysulfide in the flue gas and/or nitrogen oxide under the irradiation of electron beam, generate ammonium sulfate and/or ammonium nitrate, the reactant that generates is collected with a dust arrester by the system outlet place, and flue gas after being purified just can directly be discharged.The shortcoming of the method for this purification flue gas is: because the ammonium sulfate and the ammonium nitrate aerosol that generate behind the irradiation are very little, the footpath grain is micron dimension just, and ammonium sulfate and ammonium nitrate are very soluble in water, so these aerocolloidal hygroscopicity are very strong, be easy to attached on the dust arrester electrode and on the pipeline, form one deck shell, influence later collecting effect.For removing these attachments, must add many scraper plates and rapping apparatus; Collected byproduct in the dust arrester ash bucket because particle is too little, and lumps, as fertilizer selling, just must be set up Granulation Equipments simultaneously, has just increased the energy consumption and the fault rate of whole system.In order to improve desulfurization degree, denitration rate, usually will improve the ammonia amount of annotating, and when reaction was insufficient, owing to there is not to absorb the surplus measure that removes ammonia, unnecessary gas ammonia will enter atmosphere with flue gas, and ease ammonia takes place, and formed secondary pollution in addition.For fear of the generation of this situation, have only to reduce and annotate the ammonia amount, cause the reduction of system's desulfurization degree and denitration rate.
U.S. Pat 5,695,616 have introduced a kind of electron beam purification of flue gases by semidry process method, and its flow process that purifies flue gas is seen Fig. 1.The flow process of this purification flue gas is: after electrostatic precipitator 1 dedusting that flue gas process boiler carries, humidification in spray dryer 2, cooling, in the pipeline before entering radiation chamber 3, in flue gas, inject ammonia, at the indoor pulsed electron beam of irradiation flue gas is shone, through irradiation ammonia, water, oxygen and oxysulfide and/or nitrogen oxide react, generate ammonium sulfate and/or ammonium nitrate aerosol, enter into wet cottrell 4, after water will enter aerosol in the wet cottrell 4 and be washed to solution again, these are cleaned aerocolloidal solution is injected in the spray dryer 2, be used for humidification, cooling enters into the flue gas of spray dryer 2, will react the ammonium sulfate and/or the ammonium nitrate that generate simultaneously again and form accessory substance, can reach about 100 microns through the particle diameter after the spray-drying, can directly collect as fertilizer selling.Because ammonium sulfate and ammonium nitrate are very easily water-soluble, the wet cottrell water generates solution with the reactant of collecting, and inside and outlet conduit place water spray at radiation chamber can solve the problem that byproduct adheres to.Because the environment of low temperature, high humidity is easy to the chemical reaction behind the irradiation, nearly 1/3 reaction can be carried out in wet cottrell, can prolong reaction time and space like this, improves desulfurization degree under the prerequisite that does not increase irradiation dose, reduces system energy consumption; For improving desulfurization degree, denitration rate, need to increase and annotate the ammonia amount simultaneously, this ammonia just might occur escaping, because ammonia is soluble in water, utilizes the water in the wet cottrell can absorb ease ammonia, prevents secondary pollution.But the weak point of the method for this purification flue gas is, spray dryer the dry product particulate that goes out is too for a short time is normal distribution, some is the bulky grain more than 100 microns, also exist many tens microns granules simultaneously, the particle major part that drops on the spray dryer bottom by gravity is the bigger particle of particle diameter, and the particle of small particle diameter then can flow to into radiation chamber with flue gas, loss part electron-beam dose, these granules circulate in system, and system also can increase energy consumption.In addition, cleaning in the wet cottrell, it is a certain amount of that flush water must reach, could wash away attached to electrode and inner byproduct, and so big solution amount is all directly injected spray dryers when dry after will cleaning, because the required temperature drop of exhaust gas volumn and flue gas is certain, so the water yield that can evaporate just has certain limit, the solution amount that sprays into is too big, flue gas can't evaporate moisture wherein fully, and the wet end will appear in spray dryer, collects less than the byproduct of doing, for the byproduct that obtains to sell, must increase Granulation Equipments, so increase system energy consumption and cost, two come the effect of spray dryer not bring into play.
The method that has adopts the transformer type pulsatron, because problems such as insulation, its beam energy only can reach about 0.8～1.2Mev, the maximum range of the electron beam of this energy in flue gas is about 4 meters, consider the uniformity and the service area of electron field, in fact available scope is below 3 meters, when the exhaust gas volumn of handling when need is big, just must shunt irradiation, be about to flue gas and introduce several radiation chambers respectively and carry out irradiation, the flue gas that only can be used for the small power plant below 50,000 kilowatts is handled; Be used for large power plant, 300,000 kilowatts power plant for example, must be provided with 6 respectively is in the parallel radiation chamber radiation chamber of 3 rice diameters 1～2 electron gun to be set, come the treatment and purification flue gas, system equipment is bulky like this, and cost increases, and brings big difficulty to engineering again.
Purpose of the present invention just is to overcome the weak point in the above-mentioned prior art, and it is low to work out a kind of energy consumption, and equipment is simple, has high desulfurization, denitration rate, the flue gas purifying technique of the straight pulse electron beam semidry method of small size again.
A kind of semi-dry fume-purifying linear pulse electron beam method of the present invention, from the high-temperature flue gas of factory after the electrostatic precipitator dedusting of factory's autogamy, the flue gas that contains oxysulfide and/or nitrogen oxide, dirt, at first through the spray-drying installation spray, cooling, humidification flue gas, the particle diameter of collecting dry in the bottom of spray-drying installation is at bulky grain byproduct more than 100 microns; Flue gas stream behind cooling, humidification is brought remaining granule byproduct below 100 microns in the dust collect plant into, and remaining particle diameter is collected in the dust collect plant at the byproduct below 100 microns; The overheated ammonia that is heated to 40-120 ℃ is injected in the inlet duct of radiation chamber, mix back formation mist enters in the radiation chamber with the flue gas that exports from dust collect plant, after reacting generation byproduct of ammonium sulfate and/or ammonium nitrate under the electron beam irradiation that the straight pulse accelerator produces, byproduct enters in the wet cottrell with flue gas, the solution after heating from solution tank enters in the wet cottrell and sprays, byproduct of ammonium sulfate and/or ammonium nitrate are dissolved in the solution that sprays into, after byproduct is dissolved in the solution that sprays into, flow in the solution tank again; Enter in the spray-drying installation from the solution in the solution tank, spray, cooling, humidification flue gas be drying byproducts simultaneously.
From the 1500-4 of factory * 10
5Standard cubic meter/hour high-temperature flue gas is after the electrostatic precipitator of factory's autogamy, the flue gas that contains oxysulfide and/or nitrogen oxide, dirt, its dust content is the 1-10% percetage by weight, contain oxysulfide 500～5000ppm, contain nitrogen oxide 100～1500ppm, the temperature of flue gas is 120-260 ℃.Said factory can be the factory that power plant etc. produces flue gas.Temperature is 120-260 ℃ a flue gas, at first pass through spray-drying installation, said spray-drying installation can be a spray dryer 10, in spray dryer 10, after high-temperature flue gas will evaporate from the solution that sprays into spray dryer 10 of solution tank 15, make flue gas cool-down, humidification, the flue gas of every standard cubic meter can evaporate 0.05～0.1 kilogram solution, can directly collect dry particle diameter major part in the bottom of spray dryer at bulky grain byproduct of ammonium sulfate and/or ammonium nitrate more than 100 microns.The collected oarse-grained byproduct more than 100 microns accounts for more than 50% of byproduct total amount.Flue gas behind process cooling, the humidification passes through dust arrester with the flow velocity of 0.8-1.2 meter per second, simultaneously remaining granule byproduct below 100 microns is collected in the dust collect plant (being dust arrester again), said dust collect plant can be wherein a kind of of dry electrostatic cleaner 11 or cyclone dust collectors, sack cleaner, for example dry electrostatic cleaner 11 can be collected dry electrostatic cleaner 11 in the ash bucket of bottom basically with remaining byproduct below 100 microns, its byproduct can collect altogether the 4-136844 kilogram/hour.In the pipeline of radiation chamber 12 inlet, spray into the overheated ammonia 1-35000 kilogram that is heated to 40-120 ℃/hour, flue gas and overheated ammonia are mixed voluntarily, form the mist of flue gas and overheated gas ammonia, enter radiation chamber 12.For guaranteeing to have certain exposure time, the flow velocity of the mist of flue gas and overheated gas ammonia in radiation chamber is the 0.1-23 meter per second, and the oxygen in the flue gas, water generate OH, O, HO under the electron beam irradiation that the RF pulsatron produces at this moment
2Free radical and ammonia, water, oxysulfide, nitrogen oxide etc. strong oxidizing property react, and generate ammonium sulfate, ammonium nitrate accessory substance.For ammonium sulfate, the ammonium nitrate that prevents to generate adheres at the outlet conduit of radiation chamber 12 and radiation chamber 12, be equipped with shower nozzle at radiation chamber and outlet conduit two places thereof, water 18 (routine water for industrial use) spray, spray into water and clean attached to ammonium sulfate in the outlet conduit of radiation chamber and radiation chamber and/or ammonium nitrate byproduct, the solution of formation flows in the solution tank 15.The solution of solution tank enters in the wet cottrell 14, sprays.Enter in the wet cottrell from 45-75 ℃ the solution of being heated in the solution tank 15, spray, wash away the byproduct aerosol that dissolving is collected on the electrode and form ammonium sulfate and/or ammonium nitrate solution, its spraying intensity be the 0.1-0.3 ton/square metre.Make wet cottrell 14 keep temperature that is suitable for reacting and the high humidity environment that helps reacting like this, be reflected in the wet cottrell 14 and proceed.Be injected in the wet cottrell 14, in solution tank 15, be heated to 45-75 ℃ solution with the dissolving of byproduct of ammonium sulfate and/or ammonium nitrate after, flow in the solution tank again.Finally make the concentration of the solution in the solution tank 15 will reach an equilibrium valve.According to needed humidification amount of the flue gas of the inlet that enters spray dryer 10 and temperature drop, from solution tank 15, draw after a part of solution heater via 16 is heated to 45-120 ℃, be injected in the spray dryer 10 and spray cooling, humidification flue gas, drying byproducts.Solution tank 15 can supplementing water, and the addition of the supplementing water 19 of solution tank 15 is controlled according to the liquid level of solution tank, amount of makeup water equal the evaporation capacity 40-160000 kilogram of solution in spray dryer and wet cottrell/hour.Flue gas after the final process purified treatment is through heating, dehumidify or directly entering in the atmosphere, and the leakage rate of system's ammonia is less than 10ppm.Reaction temperature in radiation chamber is controlled at 45-85 ℃ for good.
According to existing current density and each SO of removal
2The relation of molecule institute energy requirement (Igrat ' ev be published in " Clearning flue gasby pulesd electron beams " in [Sov.Tech.Phys.Lett.18,745-46 (1992)]), experiment are pointed out to reach 4mA/cm when electron stream density
2The time, remove each SO
2(its current density is less than 2mA/cm than conventional DC transformer for molecule institute energy requirement
2) want little 20 times, can reduce system energy consumption greatly.In system, adopt and to have high electron energy (2Mev～10Mev) and high electron stream density (4mA/cm according to us
2) novel RF (Radio frequency) straight pulse electron accelerator, the Omega-P company of the U.S. this straight pulse accelerator on sale at present domesticly also and abroad is being in harmony this novel accelerator of light co-production about company.The power of novel RF straight pulse electron accelerator is 300 kilowatts to the maximum, and frequency is 1.2 * 10
5～1.5 * 10
9Hertz, its institute's electrons emitted energy can reach 2Mev (range is 8 meters), like this when handling big exhaust gas volumn, keep flue gas flow rate under the condition of 0.1～23 meter per second, bigbore radiation chamber can be adopted, just identical even more excellent treatment effect can be reached with the linac that is equivalent to 1/5～1/3 conditional electronic rifle power.It is the pulsatron of being mentioned in 95107186.6 that sort accelerator is different from the Chinese patent literature patent No., and its pulsewidth is 10
-8～10
-5Second, and the pulsewidth of RF straight pulse accelerator is 10
-4～10
-3Second, dutycycle is greater than 0.002, less than 0.02.Adopt one to two RF straight pulse electron accelerator, just can handle 4 * 10
6Nm
3The big exhaust gas volumn of/h has also been saved the required energy consumption of gas cleaning simultaneously greatly, reduces equipment volume, saves equipment investment.
The used equipment of method of the present invention is seen Fig. 2, and its equipment comprises: spray dryer 10, dry electrostatic cleaner 11, radiation chamber 12, straight pulse electron accelerator 13, wet cottrell 14, solution tank 15, heater 16, notes ammonia system 17, water 18, supplementing water 19.The inlet of spray dryer 10 links to each other through the electrostatic precipitator outlet of the piping and the autogamy of power plant (or factory of other generation flue gas), the inlet of dry electrostatic cleaner 11 or cyclone dust collectors or sack cleaner links to each other with the exhanst gas outlet of spray dryer through piping, the inlet of radiation chamber 12 links to each other through the exhanst gas outlet of piping with dry electrostatic cleaner 11, annotate ammonia system 17 and annotate ammonia to flue gas in the pipeline of radiation chamber 12 inlet front ends, the straight pulse electron accelerator carries out irradiation to the flue gas that flows through radiation chamber.For the ease of installing, safeguarding, preferably will speed up the top that device places radiation chamber.The exhanst gas outlet pipeline of the pipeline of the smoke inlet of wet cottrell 14 and radiation chamber 12 links to each other.Solution tank 15 is positioned at the below of wet cottrell, in solution tank 15 or outside be provided with heating facility, the solution that sprays into wet cottrell 14 flows into again in the solution tank 15.For prevent that byproduct from adhering in radiation chamber and pipeline, spray into cleaning radiation chamber and pipeline with industry water 18, formed solution is also introduced solution tank 15 by pipeline, solution tank also is provided with and replenishes pipeline 19, can add supplementing water according to the height of liquid level in the groove, solution tank has two tapholes, the solution that sprays into wet cottrell 14 purging systems is drawn from an outlet of solution tank, another outlet is connected with the atomizer of spray dryer 10, solution introduced in the spray dryer spraying, cooling, humidification flue gas be drying byproducts simultaneously.
30～45% the path grain particle below 100 microns is brought in dry electrostatic cleaner or cyclone dust collectors or the sack cleaner with flue gas stream.Though some granules can be used as reaction nuclear in the radiation chamber, help the generation of byproduct of ammonium sulfate and/or ammonium nitrate, but many will absorb a part of electron beam, waste some irradiation doses, this part byproduct circulates in system simultaneously, also can increase system energy consumption, therefore adopt dry electrostatic cleaner, cyclone dust collectors, sack cleaner a kind of equipment is wherein collected most of granule byproduct of ammonium sulfate and/or ammonium nitrate, having only seldom, part granule byproduct flows to into radiation chamber 12 with flue gas, because these short grained particle diameter byproducts that above-mentioned dust collection device is collected also can reach tens microns, so the byproduct of collecting just need not granulation once more.
Wet cottrell is to clean, wash away the dust arrester that is collected in the byproduct on the electrode repeatedly with a large amount of water.The quantity of circulating water of system during according to the wet cottrell optimum process condition established a solution tank 15, and in the design of the holdup time of reflux line, pipeline is longer according to solution for the volume of solution tank, it is slow to reflux, the volume of solution tank 15 will be big, make solution in the process of circulation, can dry bottom in the groove.Washing away the solution that forms behind the wet cottrell flows in the solution tank 15, spray in the wet cottrell repeatedly with the circulation of the solution in the solution tank 15 again, flow is decided according to the process conditions of wet scrubber, and this is that the one of ordinary skill in the art all knows.Draw one solution from solution tank and spray into the spray dryer 10, the solution amount of being drawn from solution tank determines that according to the humidification amount and the temperature drop of flue gas needs this just can prevent the 10 wet ends of spray dryer and cut down the consumption of energy.Flue gas can produce reaction heat through electron beam irradiation in radiation chamber 12, in order to make the reaction behind the irradiation continue in the environment of low temperature, high humidity, to carry out, solution need be heated to more than the dew-point temperature of flue gas, spray in the wet cottrell, just can make flue gas humidification, cooling, but heating-up temperature is also unsuitable too high, one wastes energy, two can't be heated to 45-75 ℃ in the general solution tank 15 and get final product flue gas cool-down.And the solution temperature that sprays in the spray dryer 10 is high, and one can the reduction equipment volume, and two prevent that the situation at the wet end of spray dryer from occurring, and therefore will be heated to the solution that sprays in the spray dryer 10 about 45-120 ℃ once more.
Method of the present invention can be used for various large coal-fired boiler institute such as purified treatment central heating stations, thermal power plant, steel mill discharged flue gas, also can be used for other sulfur-bearing and/or nitrogenous exhaust-gas treatment.
The advantage of semi-dry fume-purifying linear pulse electron beam method of the present invention just is:
1. owing to increased for example dry electrostatic cleaner of a dust arrester in the exit of spray dryer 10, the overwhelming majority of the byproduct of ammonium sulfate of tens microns of the particle diameters that brings out with flue gas stream from the spray dryer exit and/or ammonium nitrate is collected the dry electrostatic cleaner, prevented that the little accessory substance of a large amount of particle diameters from entering in the radiation chamber 12, greatly reduce the loss of electron-beam dose, reduced the energy consumption of system, make full use of the heat energy of flue gas again, saved Granulation Equipments again.
2. owing to adopted the straight pulse accelerator to replace accelerator used in the prior art, big exhaust gas volumn be can handle, desulfurization degree, denitration rate improved again, reduced the number of irradiation institute's energy requirement and electron accelerator, dwindle the system equipment volume, reduced plant area, reduced cost.
3. spray in the wet cottrell with the solution in the solution tank 15 and clean repeatedly, wash away, improved the concentration of the solution in the solution tank 15, be injected to the solution in the solution tank 15 again and carry out drying in the spray dryer 10, solution tank 15 can add make-up water according to level control, and solution recycles, there is not waste water to discharge, do not cause secondary pollution, can avoid so again occurring the wet end in the spray dryer, reduced system energy consumption again.
4. owing to adopted wet cottrell, be injected to the aqueous solution in the wet cottrell, can dissolved ammonia, make in the system leakage rate of ammonia little, help protecting environment.
The process flow diagram of Fig. 1 prior art (US5,695,616)
Among the figure, 1 is electrostatic precipitator, and 2 is spray dryer, and 3 is radiation chamber, and 4 is wet cottrell, and 20 for replenishing water pipe, and ammonia supply equipment is arranged in the system.
The schematic flow sheet of Fig. 2 semi-dry fume-purifying linear pulse electron beam method of the present invention
Among the figure, 10 is spray dryer, and 11 is dry electrostatic cleaner, and 12 is radiation chamber, and 13 is the straight pulse electron accelerator, and 14 is wet cottrell, and 15 is solution tank, and 16 is heater, and 17 for annotating ammonia system, and 18 is industry water, and 19 is condensate make-up piping.
Below with embodiment semi-dry fume-purifying linear pulse electron beam method of the present invention is further described; to help method of the present invention and advantage thereof are further understood; protection scope of the present invention is not subjected to the qualification of these embodiment, and protection scope of the present invention is decided by claims.
Embodiment 1
To contain sulfur dioxide concentration 1000ppm, 140 ℃ the flue gas stream 6000nm of nitrous oxides concentration 600ppm
3/ h is incorporated in the spray dryer 10, the dust content of flue gas is 2% percetage by weight, heated from the heater via 16 of solution tank 15 230 kilograms/hour, temperature is that 75 ℃ solution is injected in the spray dryer 10 and sprays, and cooling, humidification flue gas be drying byproducts simultaneously.The flue-gas temperature of spray dryer 10 outlets is 55 ℃, in collectable byproduct of ammonium sulfate in the bottom of spray dryer 10 and ammonium nitrate is 17.9 kilograms/hour, flue gas behind the decreasing temperature and increasing humidity passes through electrostatic precipitator with the flow velocity of 0.8 meter per second, simultaneously remaining granule byproduct below 100 microns is collected in the dry electrostatic cleaner 11, can collect 14.3 kilograms/hour ammonium sulfate and ammonium nitrate byproduct at dry electrostatic cleaner, in the inlet duct of radiation chamber 12, spray into be heated to 55 ℃ 11.83 kilograms/hour of overheated ammonias in flue gas, flue gas with enter in the radiation chamber 12 after ammonia mixes, straight pulse accelerator with one 200 watts carries out irradiation, and its frequency is 2 * 10
5Hertz, pulsewidth is 10
-3Second, dutycycle is 0.01, and the mist of flue gas and overheated ammonia is 4.5 meter per seconds at the flow velocity of radiation chamber, and reaction temperature is 58 ℃ in radiation chamber.Flue gas behind radiation chamber irradiation enters into wet cottrell 14, spray dissolving with extracting the solution that is heated to 56 ℃ from solution tank 15, collect the ammonium sulfate and the ammonium nitrate vapour that produce and bathe glue, clean the electrode of wet cottrell and byproduct of ammonium sulfate and the ammonium nitrate that wet cottrell inside is adhered to, the spraying intensity that is injected to the solution in the wet cottrell 14 is 150 kilograms/square metre, and the solution behind its spray flow into again in the solution tank 15.There is shower nozzle at outlet conduit place at radiation chamber 12 and radiation chamber 12, and water 18 sprays spray into water and clean attached to ammonium sulfate and ammonium nitrate in the outlet conduit of radiation chamber and radiation chamber 12.For keeping the liquid level of solution tank 15, replenish the moisture content of evaporation in spray drying chamber 10 and the wet cottrell 14, the supplementing water that adds in the solution tank 15 is 183.7 kilograms/hour.The final system desulfurization degree can reach 98%, and denitrogenation (being the denitration rate) reaches 88%, and the leakage rate of final ammonia is 3ppm.
Embodiment 2
Used equipment and method of operating are basic identical with embodiment 1 in the present embodiment, and only different is, will contain sulfur dioxide concentration is 850ppm, and nitrous oxides concentration is that 130 ℃ the flue gas of 258ppm flows 3 * 10
5Nm
3/ h is incorporated in the spray dryer 10, and the dust content of flue gas is 5% percetage by weight.With 9129.6 kilograms/hour, temperature is that 75 ℃ solution is injected in the spray dryer 10 and sprays, and cooling, humidification flue gas be drying byproducts simultaneously.The flue-gas temperature of spray dryer 10 outlets is 55 ℃, and 890 kilograms/hour byproduct of ammonium sulfate and ammonium nitrate can be collected in the bottom of spray dryer 10.Flue gas behind the decreasing temperature and increasing humidity passes through dry electrostatic cleaner with the flow velocity of 1.0 meter per seconds, simultaneously remaining granule byproduct below 100 microns is collected in the dry electrostatic cleaner 11, can collect 712 kilograms/hour byproduct at dry electrostatic cleaner.The overheated ammonia that is heated to 75 ℃ is injected in the flue gas for 435.6 kilograms/hour, flue gas with enter in the radiation chamber 12 after ammonia mixes, carry out irradiation with a 100KW straight pulse accelerator, its frequency is 3 * 10
7Hertz, pulsewidth is 5 * 10
-4Second, dutycycle is 0.05.The mist of flue gas and overheated ammonia is 9 meter per seconds at the flow velocity of radiation chamber, and reaction temperature is 70 ℃ in radiation chamber.Flue gas behind radiation chamber irradiation enters into wet cottrell 14, uses from solution tank 15 and extracts and be heated to 56 ℃ solution spraying to wet cottrell.The spraying intensity that is injected to the solution in the wet cottrell 14 is 160 kilograms/square metre.For keeping the liquid level of solution tank 15, the supplementing water that adds solution tank is 11183.7 kilograms/hour, and the final system desulfurization degree can reach 98%, and denitrification percent (being the denitration rate) reaches 85%, and the leakage rate of final ammonia is 4ppm.
Embodiment 3
Equipment and method of operating used in the present embodiment are basic identical with embodiment 1.Only different is that will contain sulfur dioxide concentration is that 1400ppm, nitrous oxides concentration are 180 ℃ of flue gas streams 3 * 10 of 730ppm
6Nm
3/ h is incorporated in the spray dryer 10, and the dust content of flue gas is 9% percetage by weight.With 140300 kilograms/hour, temperature is that 75 ℃ solution is injected in the spray dryer 10 and sprays, and cooling, humidification flue gas be drying byproducts simultaneously.The outlet temperature of spray dryer 10 is 53 ℃, and 47201 kilograms/hour byproduct of ammonium sulfate and ammonium nitrate can be collected in the bottom of spray dryer 10.Flue gas behind the decreasing temperature and increasing humidity passes through dry electrostatic cleaner with the flow velocity of 1.2 meter per seconds, simultaneously remaining granule byproduct below 100 microns is collected in the dry electrostatic cleaner 11, can collect 37761 kilograms/hour byproduct at dry electrostatic cleaner, the overheated ammonia that is heated to 120 ℃ is injected in the flue gas for 21621 kilograms/hour, flue gas with enter in the radiation chamber 12 after ammonia mixes.Because the content of exhaust gas volumn and sulfur dioxide, nitrogen oxide is higher, for reaching the effect of desulfurization preferably, denitration, adopt the straight pulse accelerator of two 300KW to carry out irradiation, can be in a radiation chamber two accelerators arranged side by side or flue gas is introduced two radiation chambers carry out irradiation respectively, its frequency of 300KW straight pulse accelerator is 1 * 10
9Hertz, pulsewidth is 10
-4Second, dutycycle is 0.1, the mist of flue gas and overheated ammonia is 13 meter per seconds at the flow velocity of radiation chamber, reaction temperature is 82 ℃ in radiation chamber, flue gas behind radiation chamber irradiation enters into wet cottrell 14, with extract from solution tank 15 and be heated to 56 ℃ solution spraying to wet cottrell 14, the spraying intensity that is injected to the solution in the wet cottrell 14 is 180 kilograms/square metre.For keeping the liquid level of solution tank 15, replenish the water of evaporation in spray dryer and the wet cottrell, the supplementing water that joins solution tank 15 is 98730 kilograms/hour, and the final system desulfurization degree can reach 96%, denitrification percent (being the denitration rate) reaches 80%, and the leakage rate of final ammonia is 5ppm.
Claims (10)
1. a semi-dry fume-purifying linear pulse electron beam method is characterized in that,
1) from the high-temperature flue gas of factory after the electrostatic precipitator dedusting of factory's autogamy, the flue gas that contains oxysulfide and/or nitrogen oxide, dirt, at first through the spray-drying installation spray, cooling, humidification flue gas, the particle diameter of collecting dry in the bottom of spray-drying installation is at bulky grain byproduct more than 100 microns;
2) stream of the flue gas behind cooling, humidification is brought remaining granule byproduct below 100 microns in the dust collect plant into, and remaining particle diameter is collected in the dust collect plant at the byproduct below 100 microns;
3) will be heated to 40-120 ℃ overheated ammonia is injected in the inlet duct of radiation chamber, mix back formation mist enters in the radiation chamber with the flue gas that exports from dust collect plant, after reacting generation byproduct of ammonium sulfate and/or ammonium nitrate under the electron beam irradiation that the straight pulse accelerator produces, byproduct enters in the wet static dedusting device with flue gas, the solution after heating from solution tank enters in the wet cottrell and sprays, and byproduct of ammonium sulfate and/or ammonium nitrate are dissolved in the solution that sprays into;
4) after byproduct is dissolved in the solution that sprays into, flow in the solution tank again;
5) enter in the spray-drying installation from the solution in the solution tank, spray, cooling, humidification flue gas, spray-drying.
2. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that, from the 1500-4 of factory * 10
5Standard cubic meter/hour high-temperature flue gas is after the electrostatic precipitator of factory's autogamy, the flue gas that contains oxysulfide and/or nitrogen oxide, dirt, its dust content is the 1-10% percetage by weight, contain oxysulfide 500～5000ppm, contain nitrogen oxide 100～1500ppm, the temperature of flue gas is 120-260 ℃.
3. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that spray dryer is 45-90 ℃ with 120-260 ℃ flue gas cool-down to the outlet temperature of spray dryer.
4. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that, flue gas behind cooling, humidification passes through dust arrester with the flow velocity of 0.8-1.2 meter per second, simultaneously remaining granule byproduct below 100 microns is collected in the dust collect plant.
5. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that, in the pipeline of radiation chamber inlet, spray into the overheated ammonia 1-35000 kilogram that is heated to 40-120 ℃/hour, flue gas and overheated ammonia are mixed voluntarily, form mist.
6. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that the flow velocity of mist in radiation chamber is the 0.1-23 meter per second.
7. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that, enter in the wet static dedusting device from 45-75 ℃ the solution of being heated in the solution tank, spray, wash away the byproduct aerosol that dissolving is collected on the electrode and form ammonium sulfate and/or ammonium nitrate solution, its spraying intensity be the 0.1-0.3 ton/square metre.
8. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that, be heated to 45-120 ℃ from heater via in the solution tank after, enter into spray dryer and spray, the cooling, the humidification flue gas, drying byproducts.
9. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that the reaction temperature in radiation chamber is 45-85 ℃.
10. according to a kind of semi-dry fume-purifying linear pulse electron beam method of claim 1, it is characterized in that straight pulse accelerator pulsewidth 10
-4-10
-3Second, dutycycle is greater than 0.002, and less than 0.2, its frequency is 1.2 * 10
5～1.5 * 10
9Hertz.
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| CNB001098497A CN1175918C (en) | 2000-07-11 | 2000-07-11 | Semi-dry fume-purifying linear pulse electron beam method |
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| CNB001098497A CN1175918C (en) | 2000-07-11 | 2000-07-11 | Semi-dry fume-purifying linear pulse electron beam method |
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| CN1175918C CN1175918C (en) | 2004-11-17 |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100361732C (en) * | 2005-04-15 | 2008-01-16 | 中国科学院上海应用物理研究所 | Method for desulfurizing and denitrifying flue gas by electron beam and apparatus thereof |
| CN102091513A (en) * | 2010-09-29 | 2011-06-15 | 上海洁美环保工程有限公司 | Nuclear radiation ammonia method flue gas desulfurization process and equipment |
| CN102814113A (en) * | 2012-08-13 | 2012-12-12 | 河南绿源新星环保设备有限公司 | Novel semi-dry ammonia desulfurization process |
| CN103055649A (en) * | 2013-01-28 | 2013-04-24 | 北京玄路海科技有限公司 | Dust removal, desulfurization and denitrification device of coal-fired power generation boiler |
| CN108136325A (en) * | 2015-10-02 | 2018-06-08 | 达芙妮科技股份公司 | For the device and method of electron irradiation washing |
| CN108480042A (en) * | 2018-03-08 | 2018-09-04 | 马鞍山钢铁股份有限公司 | Fume dust remover and its dust collecting process |
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| CN112370952A (en) * | 2020-09-16 | 2021-02-19 | 江苏汇能环境工程有限公司 | Factory-used waste gas desulfurization and denitrification treatment device |
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| CN100361732C (en) * | 2005-04-15 | 2008-01-16 | 中国科学院上海应用物理研究所 | Method for desulfurizing and denitrifying flue gas by electron beam and apparatus thereof |
| CN102091513A (en) * | 2010-09-29 | 2011-06-15 | 上海洁美环保工程有限公司 | Nuclear radiation ammonia method flue gas desulfurization process and equipment |
| CN102814113A (en) * | 2012-08-13 | 2012-12-12 | 河南绿源新星环保设备有限公司 | Novel semi-dry ammonia desulfurization process |
| CN103055649A (en) * | 2013-01-28 | 2013-04-24 | 北京玄路海科技有限公司 | Dust removal, desulfurization and denitrification device of coal-fired power generation boiler |
| CN103055649B (en) * | 2013-01-28 | 2015-03-11 | 北京玄路海科技有限公司 | Dust removal, desulfurization and denitrification device of coal-fired power generation boiler |
| US11123689B2 (en) | 2015-10-02 | 2021-09-21 | Daphne Technology SA | Apparatus and method for electron irradiation scrubbing |
| CN108136325A (en) * | 2015-10-02 | 2018-06-08 | 达芙妮科技股份公司 | For the device and method of electron irradiation washing |
| CN108480042A (en) * | 2018-03-08 | 2018-09-04 | 马鞍山钢铁股份有限公司 | Fume dust remover and its dust collecting process |
| CN110743338A (en) * | 2019-10-10 | 2020-02-04 | 湖北天佑环保设备有限公司 | Multifunctional waste gas purification tower |
| CN112370952A (en) * | 2020-09-16 | 2021-02-19 | 江苏汇能环境工程有限公司 | Factory-used waste gas desulfurization and denitrification treatment device |
| CN112892145A (en) * | 2021-01-22 | 2021-06-04 | 机械工业第九设计研究院有限公司 | Degradation device in VOC exhaust-gas treatment system of automotive interior processing |
| CN112892145B (en) * | 2021-01-22 | 2022-06-28 | 机械工业第九设计研究院股份有限公司 | Degradation device in VOC exhaust-gas treatment system of automotive interior processing |
| CN115646172A (en) * | 2022-10-31 | 2023-01-31 | 福建龙净环保股份有限公司 | Ammonia gas treatment process and ammonia gas treatment system |
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| CN1175918C (en) | 2004-11-17 |
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Address after: 100084 Beijing 100084-82 mailbox Applicant after: Tsinghua University Co-applicant after: Beijing State Grid Power Technology Co., Ltd. Address before: 100084 Nuclear Power Institute, Tsinghua University, Room 502, Beijing Applicant before: Xu Guang Co-applicant before: Luo Jingyu Co-applicant before: Shi Gen |
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