CN102600708B - High-efficiency low-cost purification process of flue gas - Google Patents
High-efficiency low-cost purification process of flue gas Download PDFInfo
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- CN102600708B CN102600708B CN201210058184.8A CN201210058184A CN102600708B CN 102600708 B CN102600708 B CN 102600708B CN 201210058184 A CN201210058184 A CN 201210058184A CN 102600708 B CN102600708 B CN 102600708B
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- heat exchanger
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 239000003546 flue gas Substances 0.000 title claims abstract description 88
- 238000000746 purification Methods 0.000 title abstract 2
- 239000007788 liquid Substances 0.000 claims abstract description 66
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000004140 cleaning Methods 0.000 claims abstract description 60
- 238000000034 method Methods 0.000 claims abstract description 42
- 238000010521 absorption reaction Methods 0.000 claims abstract description 34
- 239000002699 waste material Substances 0.000 claims abstract description 27
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 22
- 239000000126 substance Substances 0.000 claims abstract description 22
- 239000000243 solution Substances 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 11
- 239000012670 alkaline solution Substances 0.000 claims abstract description 3
- 238000005201 scrubbing Methods 0.000 claims description 63
- 239000012530 fluid Substances 0.000 claims description 31
- 238000003860 storage Methods 0.000 claims description 26
- 238000012545 processing Methods 0.000 claims description 20
- 239000000428 dust Substances 0.000 claims description 16
- 239000007791 liquid phase Substances 0.000 claims description 14
- 239000000945 filler Substances 0.000 claims description 13
- 238000012856 packing Methods 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 12
- 231100000614 poison Toxicity 0.000 claims description 11
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 10
- 238000012546 transfer Methods 0.000 claims description 10
- 230000007096 poisonous effect Effects 0.000 claims description 9
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 239000003507 refrigerant Substances 0.000 claims description 7
- 239000007921 spray Substances 0.000 claims description 6
- 239000000292 calcium oxide Substances 0.000 claims description 5
- 235000012255 calcium oxide Nutrition 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 230000007797 corrosion Effects 0.000 claims description 4
- 238000005260 corrosion Methods 0.000 claims description 4
- 150000004820 halides Chemical class 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 239000010808 liquid waste Substances 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 239000000654 additive Substances 0.000 claims description 2
- 230000000996 additive effect Effects 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 239000004568 cement Substances 0.000 claims description 2
- 230000007423 decrease Effects 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 238000009826 distribution Methods 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 238000005245 sintering Methods 0.000 claims description 2
- 239000002893 slag Substances 0.000 claims description 2
- 239000006228 supernatant Substances 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 4
- 239000010802 sludge Substances 0.000 abstract description 4
- 231100000331 toxic Toxicity 0.000 abstract description 2
- 230000002588 toxic effect Effects 0.000 abstract description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract 2
- 238000006386 neutralization reaction Methods 0.000 abstract 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 42
- 239000013618 particulate matter Substances 0.000 description 8
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 6
- 229910001385 heavy metal Inorganic materials 0.000 description 6
- 229910001220 stainless steel Inorganic materials 0.000 description 6
- 239000010935 stainless steel Substances 0.000 description 6
- 230000015556 catabolic process Effects 0.000 description 4
- 239000000356 contaminant Substances 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000002411 adverse Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000002925 chemical effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003500 flue dust Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 230000000704 physical effect Effects 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 230000001376 precipitating effect Effects 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 238000010977 unit operation Methods 0.000 description 3
- 238000004056 waste incineration Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- -1 bioxin Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 241000220010 Rhode Species 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
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- 150000002894 organic compounds Chemical class 0.000 description 1
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- 238000010791 quenching Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention provides a high-efficiency low-cost purification process of flue gas. The process comprises a heat exchange system, a comprehensive cleaning system, a denitration system and a waste liquid treatment system, wherein the comprehensive cleaning system is a comprehensive cleaning tower T1 consisting of 2 to 5 circular cleaning loops, the cleaning solution in the first circular cleaning loop is diluted alkaline solution, and the cleaning solutions in subsequent circular cleaning loops is water, the cleaning solution after cleaning is recycled after neutralization and biochemical treatment, and the sludge generated after treatment is cleaned and detoxified regularly; and the denitration system is a denitrition tower T2 consisting of 2 to 4 circular absorption loops, the circular absorption solution is water, and the absorption solution after NOX is absorbed is diluted nitric acid which can be directly sold or used. The contents of various toxic and harmful substances in the flue gas emitted from the top of the denitration tower T2 can be respectively controlled to be that SOx is less than or equal to 5mg/m<3>, NOx is less than or equal to 50mg/m<3>, HCl is less than or equal to 5mg/m<3>, HF is less than or equal to 1mg/<3>, HBr is less than or equal to 1mg/m<3>, solid particles are less than or equal to 3mg/m<3>, and dioxin (DOX) is less than of equal to 0.001TEQng/m<3>, which are far superior to the emission standard of related flue gas of America, European Union and China.
Description
Technical field
The present invention relates to the process for purifying of flue gas.
Background technology
The world today, coal-burning boiler, incinerator, refuse gasification boiler etc. contain multiple poisonous and harmful substance in its flue gas in the course of the work, as sulfide (SO
2, SO
3deng), halide (HCl, HF, HBr etc.), nitrogen oxide (NOx), CO2, soot dust granule thing, bioxin etc., they are to cause atmosphere pollution principal element.Therefore, industrial smoke must be processed before discharge.Yet, at the international level, there are following two aspect major defects in the method for processing at present industrial smoke: the one, and complex process, the equipment investment of processing procedure are large, chemical consumption is many, disposal cost is high (according to U.S. environment administration report, adopt existing method, as SCR, SNCR, SNCR-SCR etc. are single, process mono-of NOx, its average operation expense cost is just up to 1500-10000USD/t NOx); The 2nd, treatment process can not be integrated, being desulphurization and denitration, dedusting, de-organic pollution mutually can not be supporting as bioxin etc., do things in his own way, even or after integrating, the treatment effeciency of each workshop section is also undesirable, and desulfuration efficiency is only 90% even lower, and denitration efficiency is generally lower than 85%, efficiency of dust collection is more difficult control, and toxic organic compound is generally difficult to remove.
Therefore develop new stack gas cleaning technique very necessary.
For above situation, the present invention proposes a kind of new technology of high efficiency, low cost purifying flue gas, this technique is purifying flue gas fully, can reduce significantly again the unit consumption (processing every cubic metre of cost that flue gas is required) of processing flue gas, flue gas after processing not only reaches China's standard, and can be far superior to relevant international standard.
Summary of the invention
The new technology that the object of this invention is to provide a kind of high efficiency, low cost purifying flue gas.For realizing above-mentioned target, technical scheme of the present invention is as follows:
A high efficiency, low cost stack gas cleaning technique, it is comprised of heat-exchange system, comprehensive washing system, denitrating system and liquid waste treatment system, and as shown in Figure 1, it comprises the following steps its flow process:
(1) by the flue gas of disengaging after steam boiler heat exchange owing to thering is certain temperature (150-600 ℃ not etc.), first pass through afterheat heat exchanger (or waste heat boiler) E0 and carry out heat exchange, prepare hot water, can supplying hot water user use, flue gas is passed in afterheat heat exchanger E0 by pipeline 1, and cold water is walked shell side, flue is made tube side leave with rage, afterheat heat exchanger E0 uprightly installs, so that the flue gas condensate liquid in tube side (wherein comprises the water-soluble poisonous and harmful substance of part, as SO
3hCl, HF, HBr, dust etc.) can be smooth and easy downstream among the temporary storage tank C1 of mixed liquor, after heat exchange, cold water in shell side is heated to after 70-90 ℃, deliver to hot water storage tank, for downstream hot water user, the effluent gas temperature of discharging from afterheat heat exchanger E0 top is reduced to below 100 ℃, enters comprehensive scrubbing tower T1 bottom, comprehensive scrubbing tower T1 is comprised of 2-5 circulation cleaning loop, and each circulation cleaning loop is furnished with respectively comprehensive scrubbing tower heat exchanger and the spray thrower on circulating pump, outer circulation pipeline;
(2) flue gas through afterheat heat exchanger E0 heat exchange enters comprehensive scrubbing tower T1, sig water in uphill process and bottom the comprehensive scrubbing tower T1 entering from sig water pipeline 7 is (in order to reduce reagent cost, be generally the weak solution of calcium hydroxide) fully contact in the first circulation cleaning loop R1 of forming under circulating pump A P1 effect, remove wherein most sulfide (SO
2, SO
3deng), halide (HCl, HF, HBr etc.), dust is with harmful substances such as bioxin, flue gas continues to rise in the second circulation cleaning loop R2 and circulation cleaning loop thereafter afterwards, carry out repeatedly washing operation, thereby make sulfide (SO remaining in flue gas
2, SO
3deng), dust He the harmful substances such as bioxin be substantially eliminated, then, flue gas is discharged from comprehensive scrubbing tower T1 top again, by comprehensive scrubber overhead pipeline 6, enter in air blast F1, after pressurization, enter denitrating tower T2 bottom, at the bottom of cleaning solution drops to tower along comprehensive scrubbing tower T1 under upper, flow to again among the temporary storage tank C1 of mixed liquor, enter down treatment process one;
Wherein: in the first circulation cleaning loop R1, the liquid phase circulating by P1 is sig water, pH value is controlled between 7.2-10, be preferably between 7.5-8.5, can be the alkaline solution of aqua calcis or slag, the temperature of circulation fluid be between 30-70 ℃, is preferably between 35-50 ℃, the temperature of circulation fluid is achieved by the heat exchanger E1 on outer circulation pipeline, and unnecessary heat is removed by heat exchanger E1.
Residue from cinder or waste incineration, gasification all contains Ca in a large number, Mg, and Al, Si, the oxide of Fe, accounts for the more than 60% of total amount, after coming out of the stove, under high temperature, adds water Quench, produces alkaline mixed solution, pH=10-12.Clear liquid wherein can be for the circulation fluid of comprehensive scrubbing tower first paragraph.
Second and circulation cleaning loop R2 and Rn thereafter in, liquid phase by circulating pump B P2 and the circulating pump N Pn circulation in circulation cleaning loop is thereafter light water, the temperature of circulation fluid is between 10-40 ℃, be preferably between 15-35 ℃, second and the temperature of circulation fluid successively by comprehensive scrubbing tower heat exchanger E2 and En on outer circulation pipeline, be achieved respectively, unnecessary heat is removed by comprehensive scrubbing tower heat exchanger E2 and En, the refrigerant of comprehensive scrubbing tower heat exchanger E1, E2 and En is the cold water of 10-32 ℃, or the refrigerant of other low temperature;
According to flue gas actual conditions, the circulation cleaning loop of comprehensive scrubbing tower T1 can arrange 2-5 level, and n=2-5, is preferably 3 grades.
The operating pressure (absolute pressure) of comprehensive scrubbing tower T1 is 0.09-0.11MPa, is preferably 0.095-0.1MPa.
The mass transfer component of comprehensive scrubbing tower T1 inside can be filler, can be also column plate, take structured packing as excellent.The pressure drop of every meter of filler preferably remains on below 100Pa, and full tower pressure drop is preferably controlled at below 2KPa, and the material of filler can be advisable by the material of long-time operation 80 ℃ time again with the corrosion-resistant while;
(3) flue gas after pressurizeing by F1 enters denitrating tower T2 bottom, denitrating tower is comprised of three circulation absorption circuits, each absorption circuit is furnished with respectively denitrating tower heat exchanger E4, E5 and E6 and the spray thrower on circulating pump P4, P5 and P6, outer circulation pipeline, flue gas after pressurization along in tower uphill process successively and circulation absorption circuit R4, in R5 and R6 by circulating pump P4, the NOx absorption liquid (being generally water) of P5 and P6 circulation carries out counter current contacting absorption, NO wherein
2deng the active component with water generation chemical reaction, will finally change nitric acid into, the chemical compositions such as NO with flue gas in excessive oxygen generation oxidation reaction, change NO into
2deng further, can finally by water, be absorbed with the material of water generation chemical reaction, the flue gas by repeatedly circulating after absorbing, rises to denitrating tower T2 top, can pass through the direct emptying in denitrating tower push pipe road 13;
By above-mentioned many circulation cleanings, in flue gas, remove CO
2various water-soluble and reactive materials in addition is almost washed completely and enters in liquid phase, and micro-content organism is wherein as bioxin etc., also can be due to the washing of a large amount of liquid phase circulation and condensation separation effect and the overwhelming majority enters among liquid phase, therefore, after above-mentioned steps, in flue gas, the content of all kinds of poisonous and harmful substances can be controlled in respectively SOx≤5 mg/m
3, NOx≤50 mg/m
3, HCl≤5 mg/m
3, HF≤1 mg/m
3, HBr≤1mg/m
3， bioxin (DOX)≤0.005TEQ ng/m
3, solid particulate matter≤3 mg/m
3, be far superior to the discharge standard of the relevant flue gas in countries in the world;
The absorption liquid (being rare nitric acid) that the drops to T2 bottom circulating pump P4 by the first circulation absorption circuit partially absorbs liquid by pipeline 14 by part and delivers to rare nitric acid product storage tank C2, and rare nitric acid can be used as the raw material use of metal cleaner and configuration intermediate concentration nitric acid.
Above-mentioned three circulation cleaning loop R4, the circulation fluid of R5 and R6 is light water, it is delivered in the liquid distribution trough on T2 with certain speed by top of tower pipeline 8 and 9, be uniformly distributed rear inflow packing layer and decline step by step, its temperature is between 5-20 ℃, be preferably between 8-15 ℃, the temperature of circulation fluid is achieved by three denitrating tower heat exchanger E4, E5 on outer circulation pipeline and E6 respectively, and unnecessary heat is removed by them.
The refrigerant of denitrating tower heat exchanger E4, E5 and E6 is the cold water of 5-12 ℃, in temperature high season, can obtain refrigerant by being equipped with suitable refrigeration machine, because the highest NOx content in flue gas is conventionally lower, between 800-2000ppm, so the heat that course of reaction produces is limited, therefore refrigerating capacity and power consumption are very low.
According to flue gas actual conditions, the circulation cleaning loop of denitrating tower T2 can arrange 2-4 level, is preferably 3 grades.
Denitrating tower T2 is low voltage operated, and operating pressure (absolute pressure) is 0.13-0.2MPa, is preferably 0.15-0.17MPa.
The mass transfer component of denitrating tower T2 inside can be filler, can be also column plate, take structured packing as excellent.The pressure drop of every meter of filler preferably remains on below 100Pa.The material of filler is advisable with resistance to rare nitric acid corrosion material.
(4) at the bottom of the tower of the flue gas condensing liquid in afterheat heat exchanger E0 and comprehensive scrubbing tower T1, cleaning solution enters the temporary storage tank C1 of mixed liquor by pipeline 3 and 4 respectively, and by temporary storage tank C1, by pipeline 5, be delivered to waste liquid pool B1 and carry out preliminary treatment, this processing is generally to add appropriate quick lime to neutralize, or by other more cheap alkaline matter for processing, in waste liquid pool B1, top is supernatant layer, bottom is settle solids layer, the clear liquid on top is delivered to the further biochemical treatment of downstream biochemical treatment tank B2 by pipeline 12, with degraded organic matter wherein, (comprise bioxin, the hypertoxic organic matter such as BaP), and make discharged wastewater met the national standard or recycle, the mud of waste liquid pool B1 bottom can regularly be cleared up and process, its processing mode can be by 1000 ℃ of above high temperature sinterings thoroughly to destroy wherein the poisonous organic residues such as bioxin, or as the additive of cement baking etc. (because this type of technique is comparatively ripe, here no longer describe in detail) use.
PH value general control in waste liquid pool B1, between 7.2-10, is preferably between 7.5-8.5.Part clear liquid in waste liquid pool B1 also can be used as the source of sig water, and saves operation and the equipment of special configuration alkali lye.
The clear liquid on waste liquid pool B1 top, by pipeline 12 overflows or be delivered to biochemical treatment tank B2 by pump and carry out biochemical degradation processing, until up to standard, clear liquid after up to standard (middle water) can be carried respectively to comprehensive scrubbing tower T1 and denitrating tower T2 top as spray liquid by pump P7 and pipeline 9,10,11 by pipeline 8 again, thus water circulation in realizing.
By above 4 steps, can carry out high efficiency low consumption purified treatment to flue gas, and make the flue gas after processing reach discharge standard completely.It is pointed out that above step carries out continuously, under steady working condition, 4 steps are carried out simultaneously, and organically combine, and are not intermittently operated, are just just divided into for convenience 4 steps herein.
The outstanding advantage of the present invention has following several aspect:
The first, owing to having adopted step (1), its can make on the one hand water vapour in flue gas (conventionally account for flue gas cumulative volume 20-40% not etc.) more than 90% the obtaining condensation in afterheat heat exchanger E0 of total amount and change liquid phase water into, thereby flow into the temporary storage tank C1 of mixed liquor along heat exchanger channel, discharge latent heat simultaneously and can produce hot water as much as possible, make the heat energy in flue gas fully be reclaimed and utilize; On the other hand, along with the condensation of water vapour, the part dust, the SO that in flue gas, are mingled with
3, NO
2, CO
2, HCl, HF and HBr etc., the water that can be condensed absorbs and flows into together the temporary storage tank C1 of mixed liquor; In addition, because most water vapours in flue gas obtain condensation in afterheat heat exchanger E0, the flue gas total amount that enters the comprehensive washing in downstream and denitrating system will significantly reduce, can not reduce in theory 18-35% not etc., thereby significantly reduced processing load and the equipment size of down-stream system, saved processing cost.
The second, owing to having adopted step (2), it not only makes flue gas further be cooled to normal temperature, and has removed the most sulfide (SO in flue gas
2, SO
3deng), the harmful substance such as halide (HCl, HF, HBr etc.), dust and bioxin, make gaseous contaminant change liquid waste water and dregs into, be convenient to further process and removing toxic substances, and even resource.The removal efficiency of its medium sulphide content is up to more than 98%, and dust is removed (comprising denitration workshop section) substantially, and the organic poison removal efficiencies such as bioxin are up to more than 99%.By step (2) and step (3), in flue gas, the content of all kinds of poisonous and harmful substances can be controlled in respectively SOx≤5 mg/m
3, NOx≤50 mg/m
3, HCl≤5 mg/m
3, HF≤1 mg/m
3, HBr≤1mg/m
3， bioxin (DOX)≤0.005TEQ ng/m
3, solid particulate matter≤3 mg/m
3, being far superior to the discharge standard of the relevant flue gas in countries in the world, this is also that other smoke treating method is beyond one's reach.
Three, in step (3), low voltage operated due to what to adopt absolute pressure be 0.15-0.17MPa, this pressure is that common rhodes blower can be realized, rather than the pressure operation more than 0.4MPa conventionally adopting-it must could realize by compressor, so can energy-conservation a large amount of denitration energy resource consumption.
Four, because the present invention does not adopt bag-type dust or electric precipitation, and adopt the wet dedusting technique of multistage washing, so not only the energy consumption of dedusting is significantly saved (10% left and right that is only equivalent to electric precipitation energy consumption), and efficiency of dust collection can be up to more than 99.5%, this is that other all dust collection methods are all incomparable.
Five, owing to having adopted the simplest and the most direct, chemical cost is minimum and energy consumption is minimum process up to now, make comprehensive consumption (energy consumption, material consumption, maintenance and operating cost etc.) that the present invention administers flue gas only for the 20-30%(of other advanced method does not comprise the benefit part that the nitric acid of recovery brings), so have more competitiveness in industrial popularization.
Accompanying drawing explanation
Fig. 1 is the new technological flow schematic diagram of a kind of high efficiency, low cost purifying flue gas of the present invention, wherein: T1 is comprehensive scrubbing tower; T2 is denitrating tower; E0 is afterheat heat exchanger; E1, E2 and E3 are comprehensive scrubbing tower heat exchanger; E4, E5, E6 are denitrating tower heat exchanger; C1 is the temporary storage tank of mixed liquor; C2 is rare nitric acid storage tank; B1 is waste liquid pool; B2 is biochemical treatment tank; F1 is air blast; P1 is circulating pump A; P2 is circulating pump B; P3 is circulating pump C; P4, P5 and P6 are denitrating tower circulating pump; 1,2,13 is flue gas duct; 6 is comprehensive scrubber overhead pipeline; 7 is sig water pipeline; 8,9,10 is fresh water pipeline; 3 and 4 is mixed liquor pipeline, and 5 is that the temporary storage tank mixed liquor of mixed liquor flows out pipeline; 11 is rare nitric acid discharge pipe; Pipeline 12 is waste liquid pool clear liquid outflow pipe material.
The specific embodiment
Below by embodiment, the present invention is specifically described, but can not be interpreted as the restriction to scope of patent protection of the present invention.
Embodiment 1:
Now process certain power plant for self-supply of company flue gas, in volume fraction, it is containing CO
2be 11.2%, O
2be 8.49%, N
2be 54%, H
2o is 24%, SO
2be 1509 mg/m
3, NOx is 1212mg/m
3, all the other are other trace contaminant and flue dust.Flue gas flow is 1124980 m
3/ h, flue-gas temperature is 220 ℃.Adopt above-mentioned process, flue gas enters afterheat heat exchanger E0 by pipeline 1, makes the temperature of flue gas reduce to 115 ℃ by 220 ℃, produces hot water simultaneously, and the 350t/h aqueous water that can obtain temperature and be 88 ℃ enters hot water storage tank, and supplying hot water user uses.Subsequently, flue gas enters comprehensive scrubbing tower T1 bottom from afterheat heat exchanger E0 top by pipeline 2, first circulation fluid the second circulation fluid under with adverse current contacts step by step with the 3rd circulation fluid, and react therein simultaneously, the unit operations such as mass transfer, heat transfer and washing.The diameter of comprehensive scrubbing tower T1 is 11000mm, is highly 28000mm.The first circulation cleaning loop adopts etch-proof plastics random packing, and the second and the 3rd circulation cleaning loop adopts etch-proof stainless steel structured packing.The circulation fluid sprinkle density of first, second, and third filling batch is respectively 30m
3/ m
2.h, 25m
3/ m
2.h, 20m
3/ m
2.h.The pH value of the circulation fluid of the first filling batch is 9.1 left and right, is aqua calcis.The maximum allowable operating temperature (M.A.O.T.) of first, second, and third filling batch is respectively 80 ℃, and 40 ℃ and 20 ℃, and by the cooling water of comprehensive scrubbing tower heat exchanger E1, E2 and E3, implement temperature respectively and control.The pressure at comprehensive scrubbing tower T1 top is 0.0996MPa, and full pressure tower falls and is controlled in 3kPa.After three sections of circulation cleaning circuit operation, enter the SOx containing in the flue gas of comprehensive scrubbing tower T1, HCl, HF, HBr ， bioxin, BaP, and solid particulate matter and heavy metal etc., will be by chemical reaction, chemistry or Physical Absorption, the physical and chemical effects such as washing, dissolving and condensation enter among liquid phase.Therefore, the liquid phase of comprehensive scrubbing tower T1 bottom is chemical composition more than the mixture that contains dust particle, and it enters the temporary storage tank C1 of mixed liquor by the speed by setting with together with condensate liquid in afterheat heat exchanger E0 tube side, and flows into subsequently among waste liquid pool B1.This speed equates with the speed that comprehensive scrubbing tower T1 top clear water adds, is 2t/h.
Flue gas from comprehensive scrubbing tower T1 top discharge, through comprehensive scrubber overhead pipeline 6 and after by air blast F1 pressurization, blast denitrating tower T2 bottom, the operating pressure of denitrating tower is 0.18 MPa, temperature is 12 ℃, and the low-temperature cooling water of the denitrating tower heat exchanger by denitrating tower heat exchanger E4, E5 and E6 and the 4th circulation absorption circuit is implemented temperature and controlled respectively.The diameter of denitrating tower T2 is 9000mm, is highly 22000mm.Denitrating tower T2 is comprised of 4 circulation absorption circuits, all fills stainless steel structured packing.The circulation fluid sprinkle density of filling batch is respectively 15m from top to bottom
3/ m
2.h, 15m
3/ m
2.h, 20m
3/ m
2.h and 25m
3/ m
2.h.By pipeline 8, add the clear water flow at denitrating tower T2 top to determine according to the concentration of nitric acid in the absorption liquid of denitrating tower T2 bottom, general control is advisable between 20-40%.By controlling the liquid level of denitrating tower T2 bottom, the absorption liquid of bottom by the speed with certain through pipeline 11 overflows to rare nitric acid storage tank C2, can be used as cleaner for metal, passivating solution is sold, or further be condensed into red fuming nitric acid (RFNA) and sell.
Mixed liquor among inflow waste liquid pool B1, adds CaO with certain flow, and pH value in waste liquid pool is controlled to 8.5 left and right, clarifies and allows clear liquid enter the further degradation treatment of biochemical treatment tank B2 by pipeline 12 overflows, until up to standard.
In the precipitating sludge of waste liquid pool B1 and biochemical treatment tank B2, also may contain multiple harmful substances, comprise heavy metal element, the processing of will regularly clearing up and detoxify.
Pass through aforesaid operations, the flue gas of denitration tower top discharge is learnt after testing, in flue gas, the content of all kinds of poisonous and harmful substances is SOx≤4.2 mg/m3, NOx≤38 mg/m3, HCl≤2 mg/m3, HF≤0.2 mg/m3, HBr≤0.3mg/m3 bioxin (DOX)≤0.0022TEQ ng/m3, solid particulate matter≤2.1 mg/m3.
Embodiment 2:
Now process the flue gas of the consumer waste incineration that certain company's treating capacity is 360t/d, in volume fraction, it is containing CO
2be 12.4%, O
2be 7.63%, N
2be 56.2%, H
2o is that 20.8%, SOx is 1434 mg/m
3, NOx is 1056mg/m
3, all the other are other trace contaminant and flue dust.Flue gas flow is 45080 m
3/ h, flue-gas temperature is 120 ℃ (cooling processing).Adopt above-mentioned process, flue gas enters afterheat heat exchanger E0 by pipeline 1, makes the temperature of flue gas reduce to 85 ℃ by 120 ℃, produces hot water simultaneously, and the 8t/h aqueous water that can obtain temperature and be 64 ℃ enters hot water storage tank, and supplying hot water user uses.Subsequently, flue gas enters comprehensive scrubbing tower T1 bottom from afterheat heat exchanger E0 top by pipeline 2, first circulation fluid the second circulation fluid under with adverse current contacts step by step with the 3rd circulation fluid, and react therein simultaneously, the unit operations such as mass transfer, heat transfer and washing.The diameter of comprehensive scrubbing tower T1 is 2500mm, is highly 26000mm.The first circulation cleaning loop adopts etch-proof plastics random packing, and the second and the 3rd circulation cleaning loop adopts etch-proof stainless steel structured packing.The circulation fluid sprinkle density of the filling batch in first, second, and third circulation cleaning loop is respectively 25m
3/ m
2.h, 20m
3/ m
2.h, 15m
3/ m
2.h.The maximum allowable operating temperature (M.A.O.T.) of first, second, and third filling batch is respectively 55 ℃, and 32 ℃ and 20 ℃, and by the cooling water of comprehensive scrubbing tower heat exchanger E1, E2, E3, implement temperature respectively and control.The pressure at comprehensive scrubbing tower T1 top is 0.0997MPa, and full pressure tower falls and is controlled in 3.2kPa.After three sections of circulation cleaning circuit operation, enter the SOx containing in the flue gas of comprehensive scrubbing tower T1, HCl, HF, HBr ， bioxin, BaP, and solid particulate matter and heavy metal etc., will be by chemical reaction, chemistry or Physical Absorption, the physical and chemical effects such as washing, dissolving and condensation enter among liquid phase.Therefore, the liquid phase of comprehensive scrubbing tower T1 bottom is chemical composition more than the mixture that contains dust particle, and it enters the temporary storage tank C1 of mixed liquor by the speed by setting with together with condensate liquid in afterheat heat exchanger E0 tube side, and flows into subsequently among waste liquid pool B1.This speed equates with the speed that comprehensive scrubbing tower T1 top clear water adds, is 0.5t/h.The pH value of the circulation fluid in the first circulation cleaning loop is 8.9 left and right, is aqua calcis.
Flue gas from comprehensive scrubbing tower T1 top discharge, through comprehensive scrubber overhead pipeline 6 and after by air blast F1 pressurization, blast denitrating tower T2 bottom, the operating pressure of denitrating tower is 0.17 MPa, temperature is 14 ℃, and by the low-temperature cooling water of denitrating tower heat exchanger E4, E5, E6, implements temperature respectively and control.The diameter of denitrating tower T2 is 2000mm, is highly 24000mm.Denitrating tower T2 is comprised of 3 circulation absorption circuits, is stainless steel structured packing.The circulation fluid sprinkle density of filling batch is respectively 12m from top to bottom
3/ m
2.h, 13m
3/ m
2.h, 18m
3/ m
2.h.By pipeline 8, add the clear water flow at denitrating tower T2 top to determine according to the concentration of nitric acid in the absorption liquid of denitrating tower T2 bottom, general control is advisable between 8-15%.By controlling the liquid level of denitrating tower T2 bottom, the absorption liquid of bottom by the speed with certain through pipeline 11 overflows to rare nitric acid storage tank C2, after further concentrated, can be used as the sale of nitric acid product.
Mixed liquor among inflow waste liquid pool B1, adds CaO with certain flow, and the pH value in waste liquid pool B1 is controlled to 9.0 left and right, clarifies and allows clear liquid enter the further degradation treatment of biochemical treatment tank B2 by pipeline 12 overflows, until up to standard.
In the precipitating sludge of waste liquid pool B1 and biochemical treatment tank B2, also may contain multiple harmful substances, comprise heavy metal element, the processing of will regularly clearing up and detoxify.
Pass through aforesaid operations, the flue gas of denitration tower top discharge is learnt after testing, in flue gas, the content of all kinds of poisonous and harmful substances is SOx≤3.8 mg/m3, NOx≤41 mg/m3, HCl≤2.5 mg/m3, HF≤0.21 mg/m3, HBr≤0.29mg/m3 bioxin (DOX)≤0.0026TEQ ng/m3, solid particulate matter≤1.9 mg/m3.
Embodiment 3:
Now process the flue gas of the consumer waste incineration that certain company's treating capacity is 360t/d, in volume fraction, it is containing CO
2be 12.4%, O
2be 7.63%, N
2be 56.2%, H
2o is that 20.8%, SOx is 1434 mg/m
3, NOx is 1056mg/m
3, all the other are other trace contaminant and flue dust.Flue gas flow is 45080 m
3/ h, flue-gas temperature is 120 ℃ (cooling processing).Adopt above-mentioned process, flue gas enters afterheat heat exchanger E0 by pipeline 1, makes the temperature of flue gas reduce to 85 ℃ by 120 ℃, produces hot water simultaneously, and the 8t/h aqueous water that can obtain temperature and be 64 ℃ enters hot water storage tank, and supplying hot water user uses.Subsequently, flue gas enters comprehensive scrubbing tower T1 bottom from afterheat heat exchanger E0 top by pipeline 2, first circulation fluid the second circulation fluid under with adverse current contacts step by step with the 3rd circulation fluid, and react therein simultaneously, the unit operations such as mass transfer, heat transfer and washing.The diameter of comprehensive scrubbing tower T1 is 2500mm, is highly 26000mm.The first circulation cleaning loop adopts etch-proof plastics random packing, and the second and the 3rd circulation cleaning loop adopts etch-proof stainless steel structured packing.The circulation fluid sprinkle density of first, second, and third filling batch is respectively 25m
3/ m
2.h, 20m
3/ m
2.h, 15m
3/ m
2.h.The maximum allowable operating temperature (M.A.O.T.) of first, second, and third filling batch is respectively 55 ℃, and 32 ℃ and 20 ℃, and by the cooling water of comprehensive scrubbing tower heat exchanger E1, E2, E3, implement temperature respectively and control.The pressure at comprehensive scrubbing tower T1 top is 0.0997MPa, and full pressure tower falls and is controlled in 3.2kPa.After three sections of cyclings, enter the SOx containing in the flue gas of comprehensive scrubbing tower T1, HCl, HF, HBr ， bioxin, BaP, and solid particulate matter and heavy metal etc., will be by chemical reaction, chemistry or Physical Absorption, the physical and chemical effects such as washing, dissolving and condensation enter among liquid phase.Therefore, the liquid phase of comprehensive scrubbing tower T1 bottom is chemical composition more than the mixture that contains dust particle, and it enters the temporary storage tank C1 of mixed liquor by the speed by setting with together with condensate liquid in afterheat heat exchanger E0 tube side, and flows into subsequently among waste liquid pool B1.This speed equates to be 0.5t/h with the speed that comprehensive scrubbing tower T1 top clear water adds.The pH value of the circulation fluid in the first circulation cleaning loop is 9.6 left and right, is aqua calcis.
Flue gas from comprehensive scrubbing tower T1 top discharge, through comprehensive scrubber overhead pipeline 6 and after by air blast F1 pressurization, blast denitrating tower T2 bottom, the operating pressure of denitrating tower T2 is 0.17 MPa, temperature is 14 ℃, and by the low-temperature cooling water of denitrating tower heat exchanger E4, E5, E6, implements temperature respectively and control.The diameter of denitrating tower T2 is 2000mm, is highly 30000mm.Denitrating tower T2 is comprised of 3 circulation absorption circuits, all fills stainless steel structured packing.The circulation fluid sprinkle density of filling batch is respectively 12m from top to bottom
3/ m
2.h, 13m
3/ m
2.h, 18m3/ m
2.h.By pipeline 8, add the clear water flow at denitrating tower T2 top to determine according to the concentration of nitric acid in the absorption liquid of denitrating tower T2 bottom, general control is advisable between 8-15%.By controlling the liquid level of denitrating tower T2 bottom, the absorption liquid of bottom by the speed with certain through pipeline 11 overflows to rare nitric acid storage tank C2, after further concentrated, can be used as the sale of nitric acid product.
Mixed liquor among inflow waste liquid pool B1, adds CaO with certain flow, and the pH value in waste liquid pool is controlled to 9.0 left and right, clarifies and allows clear liquid enter the further degradation treatment of biochemical treatment tank B2 by pipeline 12 overflows, until up to standard.
In the precipitating sludge of waste liquid pool B1 and biochemical treatment tank B2, also may contain multiple harmful substances, comprise heavy metal element, the processing of will regularly clearing up and detoxify.
By aforesaid operations, the flue gas that denitrating tower discharges surely after testing learns, in flue gas, the content of all kinds of poisonous and harmful substances is SOx≤3.8 mg/m
3, NOx≤41 mg/m
3, HCl≤2.5 mg/m
3, HF≤0.21 mg/m
3, HBr≤0.29mg/m
3， bioxin (DOX)≤0.0026TEQ ng/m
3, solid particulate matter≤1.9 mg/m
3.
Claims (8)
1. a high efficiency, low cost stack gas cleaning technique, is characterized in that: it is comprised of heat-exchange system, comprehensive washing system, denitrating system and liquid waste treatment system, and it comprises the following steps:
Step 1, by the flue gas of disengaging after steam boiler heat exchange owing to thering is certain temperature, first pass through afterheat heat exchanger (E0) and carry out heat exchange, flue gas is passed in afterheat heat exchanger (E0) by pipeline (1), cold water is walked shell side, flue is made tube side leave with rage, afterheat heat exchanger (E0) is uprightly installed, so that the flue gas condensate liquid in tube side can be smooth and easy downstream among the temporary storage tank of mixed liquor (C1), after heat exchange, cold water in shell side is heated to after 70-90 ℃, deliver to hot water storage tank, for downstream hot water user, the effluent gas temperature of discharging from afterheat heat exchanger (E0) top is reduced to below 100 ℃, enter comprehensive scrubbing tower (T1) bottom, comprehensive scrubbing tower (T1) is comprised of 2-5 circulation cleaning loop, each circulation cleaning loop is furnished with respectively circulating pump, comprehensive scrubbing tower heat exchanger and spray thrower on outer circulation pipeline,
Step 2, flue gas through afterheat heat exchanger (E0) heat exchange enters comprehensive scrubbing tower (T1), in the first circulation cleaning loop (R1) forming under circulating pump A (P1) effect with the sig water of comprehensive scrubbing tower (T1) bottom entering from sig water pipeline (7) in uphill process, fully contact, remove wherein most sulfide, halide, dust is with bioxin harmful substance, flue gas continues to rise in the second circulation cleaning loop (R2) and circulation cleaning loop thereafter afterwards, carry out repeatedly washing operation, thereby make sulfide remaining in flue gas, dust He bioxin harmful substance be substantially eliminated, then, flue gas is discharged from comprehensive scrubbing tower (T1) top again, by comprehensive scrubber overhead pipeline (6), enter in air blast (F1), after pressurization, enter denitrating tower (T2) bottom, at the bottom of cleaning solution drops to tower from top to bottom along comprehensive scrubbing tower (T1), flow to again among the temporary storage tank of mixed liquor (C1), enter down treatment process one,
Wherein: in the first circulation cleaning loop (R1), liquid phase by circulating pump A (P1) circulation is sig water, pH value is controlled between 7.2-10, the temperature of circulation fluid is between 30-70 ℃, the temperature of circulation fluid is achieved by the comprehensive scrubbing tower heat exchanger of first on outer circulation pipeline (E1), and unnecessary heat is removed by the first comprehensive scrubbing tower heat exchanger (E1);
In second (R2) and circulation cleaning loop (Rn) thereafter, liquid phase by circulating pump B (P2) and circulating pump N (Pn) circulation in circulation cleaning loop is thereafter light water, the temperature of circulation fluid is between 10-40 ℃, second and the temperature of circulation fluid thereafter respectively by the comprehensive scrubbing tower heat exchanger of second on outer circulation pipeline (E2) and thereafter the comprehensive scrubbing tower heat exchanger (En) in circulation cleaning loop be achieved, unnecessary heat is removed by the second comprehensive scrubbing tower heat exchanger (E2) and the comprehensive scrubbing tower heat exchanger of n (En), first, second and the comprehensive scrubbing tower heat exchanger (E1 of n, E2 and En) refrigerant be the cold water of 10-32 ℃, or the refrigerant of other low temperature, the operation absolute pressure of comprehensive scrubbing tower (T1) is 0.09-0.11MPa,
Step 3, by the flue gas after air blast (F1) pressurization, enter denitrating tower (T2) bottom, denitrating tower is comprised of three circulation absorption circuits, each absorption circuit is furnished with respectively the 4th, the the 5th and the 6th circulating pump (P4, P5 and P6), denitrating tower on outer circulation pipeline the 4th, the the 5th and the 6th heat exchanger (E4, E5 and E6) and spray thrower, flue gas after pressurization along in tower uphill process successively with the 4th, the the 5th and the 6th circulation absorption circuit (R4, R5 and R6) in by the 4th, the the 5th and the 6th circulating pump (P4, P5 and P6) circulation NOx absorption liquid carry out counter current contacting absorption, NO wherein
2change nitric acid into water, NO with flue gas in excessive oxygen generation oxidation reaction, change NO into
2and further finally by water, absorbed with water generation chemical reaction, the flue gas by repeatedly circulating after absorbing, rises to denitrating tower (T2) top, by directly emptying of denitrating tower push pipe road (13),
Drop to the absorption liquid of denitrating tower (T2) bottom, i.e. rare nitric acid, the circulating pump (P4) by the first circulation absorption circuit will partially absorb liquid by pipeline (14) and deliver to rare nitric acid product storage tank (C2);
Three described circulation absorption circuit (R4, R5 and R6) circulation fluid be water, it is delivered in the liquid distribution trough on denitrating tower (T2) by denitrating tower top duct (9 and 10), be uniformly distributed rear inflow packing layer and decline step by step, its temperature is between 5-20 ℃, the temperature of circulation fluid is achieved by three the denitrating tower heat exchangers (E4, E5 and E6) on outer circulation pipeline respectively, and unnecessary heat is removed by them;
The refrigerant of three denitrating tower heat exchangers (E4, E5 and E6) is the cold water of 5-12 ℃, and denitrating tower (T2) is low voltage operated, and operating pressure absolute pressure is 0.13-0.2MPa;
Step 4, at the bottom of the tower of the flue gas condensing liquid in afterheat heat exchanger (E0) and comprehensive scrubbing tower (T1), cleaning solution enters the temporary storage tank of mixed liquor (C1) by pipeline (3 and 4) respectively, and by temporary storage tank (C1), by pipeline (5), be delivered to waste liquid pool (B1) and carry out preliminary treatment, processing is to add quick lime to neutralize, or by other more cheap alkaline matter for processing, pH value in waste liquid pool (B1) is controlled between 7.2-10, in waste liquid pool (B1), top is supernatant layer, bottom is settle solids layer, the clear liquid on top is delivered to further biochemical treatment of downstream biochemical treatment tank (B2) by pipeline (12), with degraded organic matter wherein, clear liquid after up to standard passes through pipeline (8) again by pump (P7) and pipeline (9, 10, 11) be delivered to respectively comprehensive scrubbing tower (T1) and denitrating tower (T2) top as spray liquid, thereby water circulation in realizing, the mud of waste liquid pool (B1) bottom is regularly cleared up and processes, its processing mode is thoroughly to destroy wherein bioxin and other poisonous organic residues by 1000 ℃ of above high temperature sinterings, or use as the additive of cement baking.
2. high efficiency, low cost stack gas cleaning technique according to claim 1, is characterized in that: the circulation cleaning loop of the comprehensive scrubbing tower (T1) described in step 2 is set to 3 circulation cleaning loops.
3. high efficiency, low cost stack gas cleaning technique according to claim 1, is characterized in that: the circulating cleaning solution in the first circulation cleaning loop (R1) of described comprehensive scrubbing tower (T1) is the alkaline solution of aqua calcis or slag.
4. high efficiency, low cost stack gas cleaning technique according to claim 1, is characterized in that: the operation absolute pressure of described comprehensive scrubbing tower (T1) is 0.095-0.1MPa.
5. high efficiency, low cost stack gas cleaning technique according to claim 1, it is characterized in that: the described inner mass transfer component of comprehensive scrubbing tower (T1) is filler, or column plate, the pressure drop of every meter of filler remains on below 100Pa, full tower pressure drop is controlled at below 2KPa, and the material of filler is the material that the corrosion-resistant while again can long-time operation in the time of 80 ℃.
6. high efficiency, low cost stack gas cleaning technique according to claim 1, is characterized in that: the circulation absorption circuit of the denitrating tower described in step 2 (T2) is set to 2-4 circulation absorption circuit; The operating pressure absolute pressure of denitrating tower is 0.15-0.17MPa, and the NOx absorption liquid of circulating pump (P4, P5 and P6) circulation is water.
7. high efficiency, low cost stack gas cleaning technique according to claim 1, it is characterized in that: the inner mass transfer component of the denitrating tower described in step 2 (T2) is filler, or column plate, when being filler, the pressure drop of every meter of filler remains on below 100Pa, and the material of filler is resistance to rare nitric acid corrosion material.
8. high efficiency, low cost stack gas cleaning technique according to claim 1, it is characterized in that: the pH value in the waste liquid pool described in step 4 (B1) is controlled between 7.5-8.5, part clear liquid in waste liquid pool (B1) is as the source of sig water, and saves operation and the equipment of special configuration alkali lye.
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| CN110772965B (en) * | 2019-11-07 | 2022-01-25 | 合肥学院 | Environment-friendly waste gas treatment process and device thereof |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010082995A2 (en) * | 2009-01-16 | 2010-07-22 | Uop Llc | Heat integration for hot solvent stripping loop in an acid gas removal process |
| CN102059043A (en) * | 2010-10-22 | 2011-05-18 | 惠州市鼎晨实业发展有限公司 | Control method of harmful waste gas generated in recycling of waste electric and electronic products |
| CN102274688A (en) * | 2011-04-10 | 2011-12-14 | 江苏揽山环境科技有限公司 | Multistage spray absorbing device with high efficiency |
| CN102309910A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Fluid catalytic cracking (FCC) flue gas treatment method |
| CN102343201A (en) * | 2011-10-11 | 2012-02-08 | 南京大学 | Process for removing acid gas from flue gas by using residual heat of flue gas |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2010082995A2 (en) * | 2009-01-16 | 2010-07-22 | Uop Llc | Heat integration for hot solvent stripping loop in an acid gas removal process |
| CN102309910A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Fluid catalytic cracking (FCC) flue gas treatment method |
| CN102059043A (en) * | 2010-10-22 | 2011-05-18 | 惠州市鼎晨实业发展有限公司 | Control method of harmful waste gas generated in recycling of waste electric and electronic products |
| CN102274688A (en) * | 2011-04-10 | 2011-12-14 | 江苏揽山环境科技有限公司 | Multistage spray absorbing device with high efficiency |
| CN102343201A (en) * | 2011-10-11 | 2012-02-08 | 南京大学 | Process for removing acid gas from flue gas by using residual heat of flue gas |
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