CN202494120U - High N-S based saliferous organic waste liquid incineration and tail gas purification processing system - Google Patents
High N-S based saliferous organic waste liquid incineration and tail gas purification processing system Download PDFInfo
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- CN202494120U CN202494120U CN2011203278858U CN201120327885U CN202494120U CN 202494120 U CN202494120 U CN 202494120U CN 2011203278858 U CN2011203278858 U CN 2011203278858U CN 201120327885 U CN201120327885 U CN 201120327885U CN 202494120 U CN202494120 U CN 202494120U
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Abstract
The utility model relates to a high N-S based saliferous organic waste liquid incineration and tail gas purification processing system, which comprises a waste liquid incineration system, a flue gas desulphurization and denitration system, a flue gas dedusting system, a waste heat recovery system and a flue gas washing system which are connected in order. A high N-S based organic waste liquid is oxidized at a high-temperature state; high-temperature flue gas obtained after complete oxidation enters a desulphurization and denitration reactor so as to thoroughly purify the flue gas; and the purified flue gas undergoes waste heat recovery. According to the processing system provided by the utility model, waste liquid incineration and flue gas purification are carried out in stages, thus satisfying the incineration temperature for thorough decomposition of organic components in the waste liquid and creating favorable conditions for subsequent desulphurization and denitration reaction. According to the utility model, while the waste liquid and the exhaust gas are processed, a lot of flue gas waste heat is recovered, a by-product saturated vapor is generated, and operation cost of an incineration device is effectively reduced.
Description
Technical field
The utility model belongs to chemical industry saliferous organic liquid waste and handles environmental technology field, is specifically related to a kind of burning and tail gas clean-up treatment 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 -, NH4
+, SO
4 2-, CN
-Isoionic organic solution, these waste liquid characteristics are concentration high ((NH4)
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 utility model purpose has been to provide a kind of both harmless treatments organic liquid waste has reclaimed the heat energy of waste liquid again, simultaneously the high N-S base saliferous organic waste liquid burning and the tail gas clean-up treatment system of by-product saturated vapor again.
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 utility model purpose, 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 ℃.
The burning and the tail gas clean-up treatment system of aforesaid a kind of high N-S base saliferous organic liquid waste, 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.
The effect of the utility model is:
Described high N-S base saliferous organic waste liquid burning of the utility model 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.The flue gas purification system of the utility model 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 described a kind of high N-S base saliferous organic waste liquid burning of the utility model 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
Further describe below in conjunction with the burning and the tail gas clean-up treatment system thereof of accompanying drawing the described a kind of high N-S base saliferous organic liquid waste of the utility model.
As shown in Figure 1, the burning and the tail gas clean-up treatment system thereof of the described a kind of high N-S base saliferous organic liquid waste of the utility model 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 1:
Table 1
| 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％ |
Deliver to incinerator 4 tops from high N-S base saliferous organic liquid waste process waste liquid tank 1 back that the factory technics device produces through waste drains pump 2 and carry out spray burning, in incinerator 4, replenish excessive combustion air through pipeline by air blast 3; Through regulating fire box temperature that combustion air volume controls incinerator 4 between 1100～1200 ℃; The flue gas of the high temperature in the incinerator 4 gets into desulfurization and denitrification reaction device 7 through flue gas injection device 5; In desulfurization and denitrification reaction device 7 and separator 8, accomplish the desulfurization and denitrification reaction of flue gas, reaction temperature is controlled at 850 ℃～950 ℃, and gas residence time is more than 1.5s; And the circulating ratio K of recycle stock gets more than 20; Flue gas behind the desulphurization denitration gets into cyclone dust collectors 11, remove a small amount of desulfurizing agent that flue gas carries after, pure high-temperature flue gas gets into waste heat boilers 13 through expansion chamber 12.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 utility model 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 utility model is directed against the improvement of the characteristics of this waste water to traditional salt-containing organic wastewater fluidization burning process, and it utilizes the smooth combustion of waste water self calorific value, destroys organic component in the organic liquid waste, and utilization " fluidization " mechanism is come the flue gas after purifying waste burns.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.
The above; Be merely the best specific embodiment of the utility model; But the protection domain of the utility model is not limited thereto; Any technical staff who is familiar with the present technique field is in the technical scope that the utility model discloses, and the variation that can expect easily or replacement all should be encompassed within the protection domain of the utility model.
Claims (2)
1. 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.
2. 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 1, it is characterized in that: described incinerator (4) is " L " type, and the incinerator interior reaction temperature is 1100～1200 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203278858U CN202494120U (en) | 2011-09-02 | 2011-09-02 | High N-S based saliferous organic waste liquid incineration and tail gas purification processing system |
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|---|---|---|---|
| CN2011203278858U CN202494120U (en) | 2011-09-02 | 2011-09-02 | High N-S based saliferous organic waste liquid incineration and tail gas purification processing system |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102305410A (en) * | 2011-09-02 | 2012-01-04 | 北京航天动力研究所 | Method and system for carrying out incineration on high N-S-based saliferous organic waste liquor and carrying out purification treatment on tail gas |
| CN103438466A (en) * | 2013-09-09 | 2013-12-11 | 北京航天动力研究所 | Method and device for producing sodium pyrophosphate by forging glyphosate mother liquor at constant temperature |
| CN106196097A (en) * | 2016-08-30 | 2016-12-07 | 安徽今朝环保科技有限公司 | Industrial slag salt bubbling fluidized bed burns harmless treatment device and method |
| CN111735065A (en) * | 2020-06-23 | 2020-10-02 | 山东同智创新能源科技股份有限公司 | Comprehensive treatment system for realizing ultra-clean emission of waste gas liquid resource in coal-to-ethylene glycol process |
| CN110160063B (en) * | 2018-02-11 | 2020-12-08 | 阮氏化工（常熟）有限公司 | Combustion treatment process for mixed waste acid containing organic matters and heavy metals |
-
2011
- 2011-09-02 CN CN2011203278858U patent/CN202494120U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102305410A (en) * | 2011-09-02 | 2012-01-04 | 北京航天动力研究所 | Method and system for carrying out incineration on high N-S-based saliferous organic waste liquor and carrying out purification treatment on tail gas |
| CN103438466A (en) * | 2013-09-09 | 2013-12-11 | 北京航天动力研究所 | Method and device for producing sodium pyrophosphate by forging glyphosate mother liquor at constant temperature |
| CN103438466B (en) * | 2013-09-09 | 2015-11-25 | 北京航天动力研究所 | A kind of method and device utilizing glyphosate mother solution calcining at constant temperature production sodium pyrophosphate |
| CN106196097A (en) * | 2016-08-30 | 2016-12-07 | 安徽今朝环保科技有限公司 | Industrial slag salt bubbling fluidized bed burns harmless treatment device and method |
| CN110160063B (en) * | 2018-02-11 | 2020-12-08 | 阮氏化工（常熟）有限公司 | Combustion treatment process for mixed waste acid containing organic matters and heavy metals |
| CN111735065A (en) * | 2020-06-23 | 2020-10-02 | 山东同智创新能源科技股份有限公司 | Comprehensive treatment system for realizing ultra-clean emission of waste gas liquid resource in coal-to-ethylene glycol process |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20121017 Effective date of abandoning: 20130522 |
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| RGAV | Abandon patent right to avoid regrant |