CN102305410A - Method and system for carrying out incineration on high N-S-based saliferous organic waste liquor and carrying out purification treatment on tail gas - Google Patents
Method and system for carrying out incineration on high N-S-based saliferous organic waste liquor and carrying out purification treatment on tail gas Download PDFInfo
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- CN102305410A CN102305410A CN201110258076A CN201110258076A CN102305410A CN 102305410 A CN102305410 A CN 102305410A CN 201110258076 A CN201110258076 A CN 201110258076A CN 201110258076 A CN201110258076 A CN 201110258076A CN 102305410 A CN102305410 A CN 102305410A
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- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000011282 treatment Methods 0.000 title claims abstract description 15
- 239000010815 organic waste Substances 0.000 title abstract description 10
- 238000000746 purification Methods 0.000 title abstract description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 78
- 239000003546 flue gas Substances 0.000 claims abstract description 78
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 62
- 230000023556 desulfurization Effects 0.000 claims abstract description 62
- 238000006243 chemical reaction Methods 0.000 claims abstract description 59
- 239000002699 waste material Substances 0.000 claims abstract description 33
- 239000002918 waste heat Substances 0.000 claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000005406 washing Methods 0.000 claims abstract description 10
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 50
- 239000010808 liquid waste Substances 0.000 claims description 36
- 239000003795 chemical substances by application Substances 0.000 claims description 29
- 239000002585 base Substances 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 25
- 239000000428 dust Substances 0.000 claims description 22
- 239000003518 caustics Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 16
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 230000003009 desulfurizing effect Effects 0.000 claims description 14
- 239000003513 alkali Substances 0.000 claims description 13
- 239000002893 slag Substances 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 11
- 238000002347 injection Methods 0.000 claims description 10
- 239000007924 injection Substances 0.000 claims description 10
- 238000003672 processing method Methods 0.000 claims description 10
- 238000005243 fluidization Methods 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 230000003020 moisturizing effect Effects 0.000 claims description 7
- 238000004056 waste incineration Methods 0.000 claims description 7
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 235000019738 Limestone Nutrition 0.000 claims description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 3
- 239000004202 carbamide Substances 0.000 claims description 3
- 230000000977 initiatory effect Effects 0.000 claims description 3
- 239000006028 limestone Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000006227 byproduct Substances 0.000 abstract description 4
- 230000002349 favourable effect Effects 0.000 abstract description 2
- 239000002912 waste gas Substances 0.000 abstract description 2
- 239000000470 constituent Substances 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 description 12
- 150000003839 salts Chemical class 0.000 description 4
- 239000003905 agrochemical Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- DFNYGALUNNFWKJ-UHFFFAOYSA-N aminoacetonitrile Chemical compound NCC#N DFNYGALUNNFWKJ-UHFFFAOYSA-N 0.000 description 2
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 2
- 125000002648 azanetriyl group Chemical group *N(*)* 0.000 description 2
- 230000003851 biochemical process Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000005496 eutectics Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- LTYRAPJYLUPLCI-UHFFFAOYSA-N glycolonitrile Chemical compound OCC#N LTYRAPJYLUPLCI-UHFFFAOYSA-N 0.000 description 2
- BSRDNMMLQYNQQD-UHFFFAOYSA-N iminodiacetonitrile Chemical compound N#CCNCC#N BSRDNMMLQYNQQD-UHFFFAOYSA-N 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- -1 alkali metal salt Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000002147 killing effect Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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- 230000002588 toxic effect Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention relates to a method and a system for carrying out incineration on high N-S-based saliferous organic waste liquor and carrying out purification treatment on tail gas. The system comprises a waste liquor incineration system, a flue gas desulfurization/denitration system, a flue gas dedusting system, a waste heat recovery system and a flue gas washing system which are sequentially connected. High N-S-based organic waste liquor is oxidized in the state of high temperature; after being oxidized completely, the high N-S-based organic waste liquor is fed into a desulfurization/denitration reactor so as to carry out thorough purification on flue gas; then, the purified flue gas is subjected to waste heat recovery. In the invention, an operation of waste liquor incineration and an operation of flue gas purification are performed in a segmented mode, therefore, not only is an incineration temperature required by thoroughly decomposing organic constituents in waste liquor satisfied, but also a favorable condition is created for subsequent desulfurization/denitration reactions. By using the method and system provided by the invention, when waste liquor and waste gas are processed, a great deal of flue gas waste heat is recovered, and a byproduct saturated steam is handled, thereby effectively reducing the operating cost of the incinerator.
Description
Technical field
The invention belongs to chemical industry saliferous organic liquid waste and handle environmental technology field, be specifically related to a kind of burning and tail gas clean-up processing method and system thereof of high N-S base saliferous organic liquid waste.
Background technology
So-called high N-S organic liquid waste is to be rich in NO
3 -, NH
4 +, SO
4 2-, CN
-Isoionic organic solution, these waste liquid characteristics are the high ((NH of concentration
4)
2SO
4Concentration is up to more than 15%), toxicity is big, calorific value is high and contain sodium salt usually.Adopt conventional processing method to comprise that biochemical process, deep oxidation method and fluidization burning method are all because of existing some drawbacks can't realize industrialization.Therefore, the discharging of such waste water causes very big pressure for the environmental protection of fine chemistry industry industries such as agricultural chemicals, dyestuff, medicine, even threatens the existence of some fine chemistry industry enterprises.
Effect was unsatisfactory when biochemical treatment process was applied to high slat-containing wastewaters such as wastewater from chemical industry such as printing and dyeing, agricultural chemicals and pesticide intermediate.Because salinity is too high in the waste water, can produce growth of microorganism and suppress, the NaCl in waste water surpasses 4000mg/L, Na
2SO
4Content surpasses 2500mg/L, and activated sludge is had stronger inhibitory action, in addition, and toxic component (CN in the waste water
-) microorganism there is killing action, directly influenced the effect of biological treatment, causing biochemical process to handle waste water can't implement.
The organic wastewater that deep oxidation method concentration of treatment is very high is also uneconomical, because the consumption of oxidant increases along with the increase of the concentration of pollutant.And intermediate product that produces in the actual oxidizing process and oxidation product maybe be bigger to the harm of environment.
Adopt the fluidization incinerating method to handle high N-S base organic liquid waste; Because the existence of alkali metal salt in the waste water; Will certainly in bed, form low-melting eutectic (between 635～815 ℃ of the fusing points),, cause the bed material to be reunited and the fluidisation failure the most at last along with the accumulation of molten state eutectic salt.
Summary of the invention
The object of the invention has been to provide a kind of both harmless treatments organic liquid waste has reclaimed the heat energy of waste liquid again, simultaneously high N-S base saliferous organic waste liquid burning and the tail gas clean-up processing method and the system of by-product saturated vapor again.
Realize the burning and the tail gas clean-up processing method of a kind of high N-S base saliferous organic liquid waste of the object of the invention, it comprises the steps:
(a) high N-S base saliferous organic liquid waste and combustion air burn from the burner that the incinerator top gets in the incinerator simultaneously; Through regulating combustion-supporting air quantity control incinerator interior reaction temperature at 1100～1200 ℃; This high N-S base saliferous organic liquid waste is oxidation Decomposition at high temperature, contains SO in the high-temperature flue gas of generation
2And NO
X
(b) contain SO in the step (a)
2And NO
XHigh-temperature flue gas come out from incinerator bottom to get in the desulfurization and denitrification reaction device from desulfurization and denitrification reaction device bottom through the flue gas injection device; Desulfurizing agent and denitrfying agent get in the desulfurization and denitrification reaction device from the bottom of desulfurization and denitrification reaction device simultaneously, and the atomizing industry water that the promotion desulphurization reaction carries out gets in the desulfurization and denitrification reaction device from the middle and upper part of desulfurization and denitrification reaction device; Adopt the fluidization principle in the desulfurization and denitrification reaction device, reaction temperature is at 850 ℃～950 ℃, and the high-temperature flue gas time of staying, the circulating ratio K of recycle stock was 20～25 at 1.5～2.0 seconds, the SO in the high-temperature flue gas
2And NO
xSame desulfurizing agent, denitrfying agent react and are removed;
(c) step (b) gained removes SO
2Come out from desulfurization and denitrification reaction device top to remove tiny desulfurizing agent and out of stock dose with the high-temperature flue gas of NOx through cyclone dust collectors; Flue gas enters into waste heat boiler and carries out heat exchange then, the water of boiler feedwater pipeline input is heated into behind the saturated vapor output incorporates pipe network into and utilize; This moment, flue-gas temperature was reduced to 240～280 ℃, was cooled to below 180 ℃ through economizer again;
(d) SO of trace is removed in the drip washing of step (c) gained flue gas process caustic wash tower
2, last flue gas directly enters atmosphere through chimney.
The burning and the tail gas clean-up processing method of aforesaid a kind of high N-S base saliferous organic liquid waste, its described desulfurizing agent adopts the powdered lime stone of average grain diameter less than 0.5mm, wherein CaCO
3Content is greater than 90%; Described denitrfying agent adopts urea.
Realize the burning and the tail gas clean-up treatment system of a kind of high N-S base saliferous organic liquid waste of the object of the invention, it comprises liquid waste incineration system, flue gas desulfurization and denitrification system, flue gas dust collecting system, residual neat recovering system and the flue gas washing system that connects successively;
Described liquid waste incineration system comprises incinerator, and waste liquid supply line and combustion air supply line are connected with the top board inlet of incinerator respectively; Described waste liquid supply line initiating terminal connects waste liquid tank, on the waste liquid supply line, also is provided with waste drains pump; Described combustion air supply line is provided with air blast;
Described flue gas desulfurization and denitrification system comprises flue gas injection device, feed bin, desulfurization and denitrification reaction device, separator, material returning device, slag remover and industry water moisturizing pipeline; Wherein, the incinerator outlet at bottom is connected with desulfurization and denitrification reaction device bottom through the flue gas injection device; Desulfurizing agent and denitrfying agent place feed bin, and feed bin is connected with desulfurization and denitrification reaction device bottom through pipeline; Industry water moisturizing pipeline is connected with desulfurization and denitrification reaction device middle and upper part; Desulfurization and denitrification reaction device top exit is connected with separator top inlet; The separator outlet at bottom is connected with material returning device top inlet, and the material returning device centre exit is connected with desulfurization and denitrification reaction device bottom through pipeline, and the material returning device outlet at bottom is connected with the slag remover inlet through pipeline;
Described flue gas dust collecting system comprises cyclone dust collectors and expansion chamber; Wherein, cyclone dust collectors middle and upper part inlet is connected with the separator top exit; The cyclone dust collectors top exit is connected with expansion chamber top inlet; The cyclone dust collectors outlet at bottom is connected with the slag remover inlet through pipeline, and the expansion chamber outlet at bottom is connected with the slag remover inlet through pipeline;
Described residual neat recovering system comprises waste heat boiler, boiler feedwater pipeline, steam output pipe road, economizer; Wherein, the waste heat boiler upper entrance is connected with the outlet of expansion chamber middle and lower part, and the waste heat boiler lower part outlet is connected with the economizer upper entrance; The boiler feedwater pipeline is connected with the water inlet of waste heat boiler middle and lower part through economizer; The steam output pipe road is connected with the venthole on waste heat boiler top;
Described flue gas washing system comprises caustic wash tower, NaOH solution circulating pump, alkali lye storage tank, air-introduced machine, chimney; Described air-introduced machine inlet is connected with the economizer lower part outlet; The air-introduced machine outlet links to each other with caustic wash tower bottom inlet through pipeline; The caustic wash tower outlet at bottom is connected with alkali lye storage tank inlet; The outlet of alkali lye storage tank is connected with the NaOH solution circulating pump inlet; The NaOH solution circulating pump outlet links to each other with caustic wash tower top alkali liquor inlet through pipeline, and caustic wash tower top exhanst gas outlet links to each other with the chimney inlet.
The burning and the tail gas clean-up treatment system of aforesaid a kind of high N-S base saliferous organic liquid waste, its described incinerator is " L " type, the incinerator interior reaction temperature is 1100～1200 ℃.
Effect of the present invention is:
High N-S base saliferous organic waste liquid burning of the present invention and tail gas clean-up processing method; Be to be directed against of the improvement of the characteristics of this waste water to traditional salt-containing organic wastewater fluidization burning process; It utilizes the smooth combustion of waste water self calorific value; Destroy organic component in the organic liquid waste, and utilization " fluidization " mechanism is come the flue gas after purifying waste burns.In this method with the oxidation under the condition of high temperature of high N-S base organic liquid waste; High-temperature flue gas behind the complete oxidation gets into the desulfurization and denitrification reaction device; In the desulfurization and denitrification reaction device, utilizing the fluid bed principle is that the bed material thoroughly purifies flue gas with the desulfurization denitrification agent, and flue gas after being purified gets into waste-heat recovery device.Disposing waste liquid, in the waste gas, reclaiming a large amount of fume afterheats, the by-product saturated vapor reduces the operating cost of incinerator effectively.Traditional brine waste fluidization burning process has been covered on this environmental-protecting process method mountain peak, be expected to thoroughly to solve fine chemistry industry industries dischargings such as agricultural chemicals, dyestuff, medicine the high concentration sulfur-bearing, contain the bottleneck problem of nitro organic liquid waste environmental protection treatment.
High N-S base saliferous organic waste liquid burning of the present invention and tail gas clean-up treatment system; It adopts liquid waste incineration and gas cleaning segmentation to carry out; Not only satisfy the required incineration temperature of the thorough decomposition of organic component in the waste liquid, and create favorable conditions for follow-up desulfurization and denitrification reaction.High-temperature flue gas purification system after the burning is the basis with the fluid bed principle, makes the repeatedly recirculation in reactor of desulfurizing agent, denitrfying agent, has prolonged the time of contact of desulfurization, denitrfying agent and flue gas, thereby has improved the utilization rate of absorbent greatly.Flue gas purification system of the present invention has been avoided salt bearing liquid wastes to burn effectively and has been caused boiler plugging harm in the back flue gas waste heat recovery process; Realized that successfully salt bearing liquid wastes CIU and heat-energy recovering apparatus are integrated; When disposing waste liquid; Reclaim a large amount of fume afterheats; The by-product saturated vapor reduces the operating cost of incinerator effectively.
Description of drawings
Fig. 1 is a kind of high N-S base saliferous organic waste liquid burning of the present invention and tail gas clean-up treatment system sketch map.
Among the figure: 1. waste liquid tank; 2. waste drains pump; 3. air blast; 4. incinerator; 5. flue gas injection device; 6. feed bin; 7. desulfurization and denitrification reaction device; 8. separator; 9. material returning device; 10. cold slag machine; 11. cyclone dust collectors; 12. expansion chamber; 13. waste heat boiler; 14. economizer; 15. air-introduced machine; 16. caustic wash tower; 17. alkali lye storage tank; 18. NaOH solution circulating pump; 19. boiler feedwater pipeline; 20. steam output pipe road; 21. chimney; 22. industry water moisturizing pipeline.
The specific embodiment
Below in conjunction with accompanying drawing the burning of a kind of high N-S base saliferous organic liquid waste of the present invention and tail gas clean-up processing method thereof and system thereof are further described.
Embodiment 1
Wait that the high N-S base saliferous organic liquid waste composition that burns purified treatment sees the following form 1:
Table 1
| Sample 1 | Form (wt%) |
| Hydroxyacetonitrile | 7.38％ |
| Glycinonitrile | 0.97％ |
| Iminodiacetonitrile | 13.46％ |
| Nitrilo three acetonitriles | 5.14％ |
| The sulphur ammonium | 16.33％ |
| Moisture | 46.72％ |
| Other organic matter | 10％ |
| Add up to | 100％ |
The step that employing the method for the invention is handled above-mentioned high N-S base saliferous organic liquid waste is following:
(1) high N-S base saliferous organic liquid waste and combustion air get into incinerator from " L " type incinerator 4 tops; At incinerator 4 interior reaction temperatures is 1100～1200 ℃ (for example 1100 ℃, 1150 ℃ or 1200 ℃); Under the condition that has oxygen to exist; Waste liquid is oxidation Decomposition at high temperature, contains a large amount of SO in the high-temperature flue gas of generation
2With little amount of N O
XDeng; Through regulating fire box temperature that combustion air volume controls incinerator 4 at 1100～1200 ℃ (for example 1100 ℃, 1150 ℃ or 1200 ℃).
The burner of delivering to incinerator 4 tops through waste drains pump 2 from high N-S base saliferous organic liquid waste process waste liquid tank 1 back that the factory technics device produces carries out spray burning, in incinerator 4, replenishes excessive combustion air by air blast 3 through pipeline;
(2) high-temperature flue gas in the step (1) comes out from incinerator 4 bottoms to get in the desulfurization and denitrification reaction device 7 from desulfurization and denitrification reaction device 7 bottoms through flue gas injection device 5, and desulfurizing agent (adopts the powdered lime stone of average grain diameter less than 0.5mm, wherein CaCO simultaneously
3Content is greater than 90%) and denitrfying agent (employing urea) get in the desulfurization and denitrification reaction device 7 from the bottom of desulfurization and denitrification reaction device 7, promote atomizing industry water that desulphurization reaction carries out to get in the desulfurization and denitrification reaction device 7 from the middle and upper part of desulfurization and denitrification reaction device 7; Adopt the fluidization principle in the desulfurization and denitrification reaction device 7; Reaction temperature is at 850 ℃～950 ℃ (for example 850 ℃, 900 ℃ or 950 ℃); The high-temperature flue gas time of staying was 1.5～2.0 seconds (for example 1.5 seconds or 2.0 seconds); The circulating ratio K of recycle stock is 20～25 (for example K is 20,22 or 25), the SO in the high-temperature flue gas
2React and be removed with the same desulfurizing agent of NOx, denitrfying agent;
(3) step (2) gained removes SO
2And NO
xHigh-temperature flue gas come out from desulfurization and denitrification reaction device 7 tops through after cyclone dust collectors 11 dedustings; The flue gas of cleaning enters into waste heat boiler and carries out heat exchange; The water of boiler feedwater pipeline 19 input is heated into the saturated vapor of 1.25MPaG, incorporates pipe network into by 20 outputs of steam output pipe road and utilize again; This moment, flue-gas temperature was also correspondingly reduced to about 250 ℃ by about 1100 ℃, was cooled to 180 ℃ through economizer 14 again;
(4) step (3) gained flue gas is removed micro-SO through caustic wash tower 16 washings
2After, directly enter atmosphere through chimney 21.GB16297-1996 " discharge standard of air pollutants " is satisfied in discharging.
Embodiment 2
As shown in Figure 1, the burning and the tail gas clean-up treatment system thereof of a kind of high N-S base saliferous organic liquid waste of the present invention comprise liquid waste incineration system, flue gas desulfurization and denitrification system, flue gas dust collecting system, residual neat recovering system and the flue gas washing system that connects successively;
Described liquid waste incineration system comprises incinerator 4, and waste liquid supply line and combustion air supply line are connected with the top board inlet of incinerator 4 respectively; Described waste liquid supply line initiating terminal connects waste liquid tank 1, on the waste liquid supply line, also is provided with waste drains pump 2; Described combustion air supply line is provided with air blast 3;
Described flue gas desulfurization and denitrification system comprises flue gas injection device 5, feed bin 6, desulfurization and denitrification reaction device 7, separator 8, material returning device 9, slag remover 10 and industry water moisturizing pipeline 22; Wherein, incinerator 4 outlet at bottoms are connected with desulfurization and denitrification reaction device 7 bottoms through flue gas injection device 5; Desulfurizing agent and denitrfying agent place feed bin 6, and feed bin 6 is connected with desulfurization and denitrification reaction device 7 bottoms through pipeline; Industry water moisturizing pipeline 22 is connected with desulfurization and denitrification reaction device 7 middle and upper parts; Desulfurization and denitrification reaction device 7 top exits are connected with separator 8 tops inlet; Separator 8 outlet at bottoms are connected with material returning device 9 tops inlet, and material returning device 9 centre exits are connected with desulfurization and denitrification reaction device 7 bottoms through pipeline, and material returning device 9 outlet at bottoms are connected with slag remover 10 inlets through pipeline;
Described flue gas dust collecting system comprises cyclone dust collectors 11 and expansion chamber 12; Wherein, cyclone dust collectors 11 middle and upper parts inlet is connected with separator 8 top exits; Cyclone dust collectors 11 top exits are connected with expansion chamber 12 tops inlet; Cyclone dust collectors 11 outlet at bottoms are connected with slag remover 10 inlets through pipeline, and expansion chamber 12 outlet at bottoms are connected with slag remover 10 inlets through pipeline;
Described residual neat recovering system comprises waste heat boiler 13, boiler feedwater pipeline 19, steam output pipe road 20, economizer 14; Wherein, waste heat boiler 13 upper entrances are connected with the outlet of expansion chamber 12 middle and lower parts, and waste heat boiler 13 lower part outlets are connected with economizer 14 upper entrances; Boiler feedwater pipeline 19 is connected with the water inlet of waste heat boiler 13 middle and lower parts through economizer 14; Steam output pipe road 20 is connected with the venthole on waste heat boiler 13 tops;
Described flue gas washing system comprises caustic wash tower 16, NaOH solution circulating pump 18, alkali lye storage tank 17, air-introduced machine 15, chimney 21; Described air-introduced machine 15 inlets are connected with economizer 14 lower part outlets; Air-introduced machine 15 outlets link to each other with caustic wash tower 16 bottoms inlet through pipeline; Caustic wash tower 16 outlet at bottoms are connected with alkali lye storage tank 17 inlets; 17 outlets of alkali lye storage tank are connected with NaOH solution circulating pump 18 inlets; NaOH solution circulating pump 18 outlets link to each other with caustic wash tower 16 top alkali liquor inlets through pipeline, and caustic wash tower 16 top exhanst gas outlets link to each other with the chimney inlet.
Adopt the high N-S base saliferous organic liquid waste shown in the said system processing list 2:
Table 2
| Sample | Form (wt%) |
| Hydroxyacetonitrile | 8.30％ |
| Glycinonitrile | 0.93％ |
| Iminodiacetonitrile | 8.29％ |
| Nitrilo three acetonitriles | 3.04％ |
| The sulphur ammonium | 14.14％ |
| Moisture | 53.30％ |
| Other organic matter | 12％ |
| Add up to | 100％ |
Arising from the plant process units high salinity organic waste NS group 1 after passing through the waste tank waste incinerators pump 2 to 4 Top atomization combustion air blower 3 by the incinerator 4 through pipelines to replenish the excess combustion air; By adjusting the amount of combustion air to control the furnace temperature incinerator 4 in between 1100 ~ 1200 ℃, high temperature incinerator flue gas within four gas injectors 5 through into the desulfurization and denitration reactor 7, the desulfurization and denitrification reactor 7 and the separator 8 is completed desulfurization and denitrification of flue gas, the reaction temperature is controlled at 850 ℃ ~ 950 ℃, gas residence time of more than 1.5s, and the loop material recycling rate K is 20 or more, after the flue gas desulfurization and denitrification into cyclone 11 to remove a small amount of flue gas desulfurization agent carries after pure high temperature flue gas settling chamber 12 into the waste heat boiler 13.High-temperature flue gas is through carrying out heat exchange with waste heat boiler 13; The water of boiler feedwater pipeline 19 inputs is heated into the saturated vapor of 1.25MPaG; Thereby make a large amount of heat recovery that contain in the high-temperature flue gas after the burning; Flue-gas temperature is also correspondingly reduced to about 250 ℃ by about 1100 ℃, is cooled to 180 ℃ through economizer again; Gained steam is incorporated pipe network into by 20 outputs of steam output pipe road and is utilized.Flue gas after the cooling enters atmosphere by chimney after air-introduced machine 15 causes caustic wash tower 16 sprays.
The operating pressure of a whole set of process system of the present invention fixes on expansion chamber zero point, and is malleation before the expansion chamber, is negative pressure state after the expansion chamber, and discharge tail gas meets the GB16297-1996 standard.
The above; Only be the best specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, any technical staff who is familiar with the present technique field is in the technical scope that the present invention discloses; The variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.
Claims (4)
1. the burning and the tail gas clean-up processing method of one kind high N-S base saliferous organic liquid waste, it is characterized in that: this method comprises the steps:
(a) high N-S base saliferous organic liquid waste and combustion air burn from the burner that incinerator (4) top gets in the incinerator (4) simultaneously; Through regulating combustion-supporting air quantity control incinerator (4) interior reaction temperature at 1100～1200 ℃; This high N-S base saliferous organic liquid waste is oxidation Decomposition at high temperature, contains SO in the high-temperature flue gas of generation
2And NO
X
(b) contain SO in the step (a)
2And NO
XHigh-temperature flue gas come out from incinerator (4) bottom to get in the desulfurization and denitrification reaction device (7) from desulfurization and denitrification reaction device (7) bottom through flue gas injection device (5); Desulfurizing agent and denitrfying agent get in the desulfurization and denitrification reaction device (7) from the bottom of desulfurization and denitrification reaction device (7) simultaneously, and the atomizing industry water that the promotion desulphurization reaction carries out gets in the desulfurization and denitrification reaction device (7) from the middle and upper part of desulfurization and denitrification reaction device (7); Adopt the fluidization principle in the desulfurization and denitrification reaction device (7), reaction temperature is at 850 ℃～950 ℃, and the high-temperature flue gas time of staying, the circulating ratio K of recycle stock was 20～25 at 1.5～2.0 seconds, the SO in the high-temperature flue gas
2And NO
xSame desulfurizing agent, denitrfying agent react and are removed;
(c) step (b) gained removes SO
2Come out from desulfurization and denitrification reaction device (7) top to remove tiny desulfurizing agent and out of stock dose with the high-temperature flue gas of NOx through cyclone dust collectors (11); Flue gas enters into waste heat boiler (13) and carries out heat exchange then, the water of boiler feedwater pipeline (19) input is heated into behind the saturated vapor output incorporates pipe network into and utilize; This moment, flue-gas temperature was reduced to 240～280 ℃, passed through economizer (14) again and was cooled to below 180 ℃;
(d) SO of trace is removed in the drip washing of step (c) gained flue gas process caustic wash tower (16)
2, last flue gas directly enters atmosphere through chimney (21).
2. the burning and the tail gas clean-up processing method of a kind of high N-S base saliferous organic liquid waste according to claim 1, it is characterized in that: described desulfurizing agent adopts the powdered lime stone of average grain diameter less than 0.5mm, wherein CaCO
3Content is greater than 90%; Described denitrfying agent adopts urea.
3. the burning and the tail gas clean-up treatment system of one kind high N-S base saliferous organic liquid waste, it is characterized in that: this system comprises liquid waste incineration system, flue gas desulfurization and denitrification system, flue gas dust collecting system, residual neat recovering system and the flue gas washing system that connects successively;
Described liquid waste incineration system comprises incinerator (4), and waste liquid supply line and combustion air supply line are connected with the top board inlet of incinerator (4) respectively; Described waste liquid supply line initiating terminal connects waste liquid tank (1), on the waste liquid supply line, also is provided with waste drains pump (2); Described combustion air supply line is provided with air blast (3);
Described flue gas desulfurization and denitrification system comprises flue gas injection device (5), feed bin (6), desulfurization and denitrification reaction device (7), separator (8), material returning device (9), slag remover (10) and industry water moisturizing pipeline (22); Wherein, incinerator (4) outlet at bottom is connected with desulfurization and denitrification reaction device (7) bottom through flue gas injection device (5); Desulfurizing agent and denitrfying agent place feed bin (6), and feed bin (6) is connected with desulfurization and denitrification reaction device (7) bottom through pipeline; Industry water moisturizing pipeline (22) is connected with desulfurization and denitrification reaction device (7) middle and upper part; Desulfurization and denitrification reaction device (7) top exit is connected with separator (8) top inlet; Separator (8) outlet at bottom is connected with material returning device (9) top inlet, and material returning device (9) centre exit is connected with desulfurization and denitrification reaction device (7) bottom through pipeline, and material returning device (9) outlet at bottom is connected with slag remover (10) inlet through pipeline;
Described flue gas dust collecting system comprises cyclone dust collectors (11) and expansion chamber (12); Wherein, cyclone dust collectors (11) middle and upper part inlet is connected with separator (8) top exit; Cyclone dust collectors (11) top exit is connected with expansion chamber (12) top inlet; Cyclone dust collectors (11) outlet at bottom is connected with slag remover (10) inlet through pipeline, and expansion chamber (12) outlet at bottom is connected with slag remover (10) inlet through pipeline;
Described residual neat recovering system comprises waste heat boiler (13), boiler feedwater pipeline (19), steam output pipe road (20), economizer (14); Wherein, waste heat boiler (13) upper entrance is connected with the outlet of expansion chamber (12) middle and lower part, and waste heat boiler (13) lower part outlet is connected with economizer (14) upper entrance; Boiler feedwater pipeline (19) is connected with the water inlet of waste heat boiler (13) middle and lower part through economizer (14); Steam output pipe road (20) is connected with the venthole on waste heat boiler (13) top;
Described flue gas washing system comprises caustic wash tower (16), NaOH solution circulating pump (18), alkali lye storage tank (17), air-introduced machine (15), chimney (21); Described air-introduced machine (15) inlet is connected with economizer (14) lower part outlet; Air-introduced machine (15) outlet links to each other with caustic wash tower (16) bottom inlet through pipeline; Caustic wash tower (16) outlet at bottom is connected with alkali lye storage tank (17) inlet; Alkali lye storage tank (17) outlet is connected with NaOH solution circulating pump (18) inlet; NaOH solution circulating pump (18) outlet links to each other with caustic wash tower (16) top alkali liquor inlet through pipeline, and caustic wash tower (16) top exhanst gas outlet links to each other with the chimney inlet.
4. the burning and the tail gas clean-up treatment system of a kind of high N-S base saliferous organic liquid waste according to claim 4, it is characterized in that: described incinerator (4) is " L " type, and the incinerator interior reaction temperature is 1100～1200 ℃.
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