CN103007710B - Sodium metasilicate tail gas treatment process and treatment facility thereof - Google Patents
Sodium metasilicate tail gas treatment process and treatment facility thereof Download PDFInfo
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- CN103007710B CN103007710B CN201210507766.XA CN201210507766A CN103007710B CN 103007710 B CN103007710 B CN 103007710B CN 201210507766 A CN201210507766 A CN 201210507766A CN 103007710 B CN103007710 B CN 103007710B
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Abstract
The invention discloses a kind of sodium metasilicate tail gas treatment process, belong to chemical industry tail gas processing technology field, comprise described sodium metasilicate tails dedusting and cool, then the circulation fluid in cooled described sodium metasilicate tail gas and some grades of device for absorbing tail gas being carried out reacting until the content of described sodium metasilicate sulfur dioxide in tail gas is up to standard; Also disclose a kind of sodium metasilicate tail gas treatment device simultaneously, comprising the dust arrester, cooling heat exchange device and the some grades of absorption plants that connect successively, in every grade of described absorption plant, being equipped with the shower for being atomized circulation fluid.The present invention effectively removes the sulfur dioxide in sodium metasilicate tail gas, and the content of sulfur dioxide in tail gas is up to standard, can directly be discharged in external environment condition, decreases the adverse effect of exhaust emissions to environment, avoids environmental pollution.
Description
Technical field
The invention belongs to chemical industry tail gas processing technology field, particularly relate to a kind of sodium metasilicate tail gas treatment process and treatment facility thereof.
Background technology
Sodium metasilicate is commonly called as waterglass, sodium silicate, its purposes widely, almost throughout each department of national economy.In chemical industry, be widely used in various silicates products such as manufacturing silica gel, white carbon, zeolite molecular sieve, sodium metasilicate, Ludox, layer silicon and instant powdery sodium silicate, sodium potassium silicate, be the base stock of silicon compound; Being indispensable raw material in the washing agent such as washing powder, soap in light industry, is also water softener, settling agent; For helping dye, bleaching and sizing in textile industry; Casting, emery wheel manufacture and anticolodal etc. are widely used in addition in machinery industry.
Be that sodium metasilicate produced by raw material with soda ash, have that heat waste is large, carbon emission amount large, high in cost of production shortcoming, therefore adopt glauber salt and sodium sulfate instead of soda to be that sodium metasilicate produced by raw material.Significantly reduce because it has cost, carbon emission reduces 95% with first-class advantage simultaneously, is thus widely used.
When glauber salt and quartz sand are raw material production sodium metasilicate, in kiln calcination process, produce a large amount of kiln tail gas and body of heater flue gas, containing sulfur dioxide and dust in tail gas.Adopt bag-type dust collector to carry out desulfurization and dedusting process, although efficiency of dust collection is high, dust qualified discharge in tail gas, the sulfur dioxide in tail gas is without effective process, and sulfur dioxide in tail gas can not realize qualified discharge, can cause severe contamination to environment.
Summary of the invention
Technical problem to be solved by this invention is: provide a kind of sodium metasilicate tail gas treatment process, to solve in sodium metasilicate production process the tail gas produced containing sulfur dioxide, without effective process, to the technical problem of environment.
For solving the problems of the technologies described above, technical scheme of the present invention is: sodium metasilicate tail gas treatment process, comprises the steps:
A, dust removal step;
B, cooling step, be cooled to less than 80 DEG C by the tail gas after dedusting;
C, some grades of tail gas absorption steps, tail gas after cooling is passed into the some grades of absorption plants be cascaded, the shower that concentration is the sodium hydroxide solution of 30% is equipped with in absorption plant described in every one-level, described tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to described shower and continues spray utilization, if the concentration of described sulfur dioxide in tail gas is less than 18mg/m
3, be then discharged into external environment condition from the upper end of described absorption plant, otherwise continue to enter next stage absorption plant;
D, the sodium sulfite solution of absorption plant being positioned at downstream are communicated with the shower of upper level absorption plant with the mixed liquor of sodium hydroxide solution.
Improve as one, the body of heater flue gas collected around boiler passes into second level absorption plant.
Improve as one, first order absorption plant cyclic process sulfite sodium and tail gas continue reaction and generate sodium hydrogensulfite, when the proportion of the sodium hydrogensulfite that first order absorption plant generates is 1.34-1.36, are exported by described sodium hydrogensulfite.
As further improvement, prepare sodium sulfite with the solution of sodium bisulfite that proportion is 1.34-1.36.
After have employed technique scheme, the invention has the beneficial effects as follows: because sodium metasilicate tail gas is through some grades of tail gas absorption, the concentration of sulfur dioxide in tail gas is less than 18mg/m
3, thus the content of sulfur dioxide in tail gas is up to standard, can directly be discharged in external environment condition, decreases the adverse effect of exhaust emissions to environment, avoids environmental pollution; Mixed liquor due to the sodium sulfite solution with sodium hydroxide solution that are positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant, and thus in whole sweetening process, the aqueous solution recycles, completely without waste sludge discharge.
Because the body of heater flue gas collected around boiler passes into second level absorption plant, thus not only prevent body of heater smoke pollution environment, and the sulfur content passed in the absorption plant tail gas of the second level can be increased.
Due to when the proportion of the sodium hydrogensulfite that first order absorption plant generates is 1.34-1.36, described sodium hydrogensulfite is exported, prepare sodium sulfite with the solution of sodium bisulfite that proportion is 1.34-1.36, thus sodium sulfite can be used as accessory substance, increases economic benefit.
This invention also solves another technical problem is: provide a kind of sodium metasilicate tail gas treatment device, to solve in sodium metasilicate production process the tail gas produced containing sulfur dioxide, without effective process, to the technical problem of environment.
For solving the problems of the technologies described above, technical scheme of the present invention is: sodium metasilicate tail gas treatment device, comprise the dust arrester be communicated with described sodium metasilicate tail gas, described dust arrester is communicated with cooling heat exchange device, described cooling heat exchange device is communicated with some grades of absorption plants, the described absorption plant of some levels is cascaded, the shower for being atomized circulation fluid is equipped with in every grade of described absorption plant, the below of described shower arranges agitator tank, discharge gate is provided with bottom described agitator tank, the top of described agitator tank is provided with feeding tube, the sidewall of described agitator tank is provided with fluid pipeline, described fluid pipeline is communicated with described shower by liquor pump, the discharge gate being positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant.
Improve, for collecting the body of heater fume collection pipeline communication second level absorption plant of body of heater flue gas around boiler as one.
Improve as one, the feeding tube of described agitator tank is all communicated with the first liquid caustic soda tank of the sodium hydroxide solution containing concentration being 30%.
Improve as one, the discharge gate of first order absorption plant is communicated with neutralization reaction still.
As further improvement, described neutralization reaction still is communicated with the second liquid caustic soda tank of the sodium hydroxide solution containing concentration being 30%.
After have employed technique scheme, the invention has the beneficial effects as follows: owing to devising some grades of absorption plants, sodium metasilicate tail gas is by the absorption of some grades of absorption plants, and the concentration of sodium metasilicate sulfur dioxide in tail gas is less than 18mg/m
3, thus the content of sulfur dioxide in tail gas is up to standard, can directly be discharged in external environment condition, decreases the adverse effect of exhaust emissions to environment, avoids environmental pollution; Because the discharge gate being positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant, thus in whole sweetening process, the aqueous solution recycles, completely without waste sludge discharge.
Due to the body of heater fume collection pipeline communication second level absorption plant for collecting body of heater flue gas around boiler, thus not only prevent body of heater smoke pollution environment, and the sulfur content passed in the absorption plant tail gas of the second level can be increased.
Because the discharge gate of first order absorption plant is communicated with neutralization reaction still, described neutralization reaction still is communicated with the second liquid caustic soda tank of the sodium hydroxide solution containing concentration being 30%, thus when the proportion of the solution of sodium bisulfite that first order absorption plant generates is 1.34-1.36, be expelled in neutralization reaction still, after sodium hydroxide solution hybrid reaction, generate sodium sulfite as accessory substance, can economic benefit be increased.
Accompanying drawing explanation
Fig. 1 is the structural representation of the embodiment of the present invention;
Fig. 2 is the process chart of the embodiment of the present invention;
In figure, 1, dust arrester, 2, cooling heat exchange device, 3, first order absorption plant, 4, second level absorption plant, 5, third level absorption plant, 6, body of heater fume collection pipeline, 7, shower, 8, agitator tank, 81, discharge gate, 82, feeding tube, 83, fluid pipeline, the 9, first liquid caustic soda tank, 10, liquor pump, 11, neutralization reaction still, the 12, second liquid caustic soda tank, 13, spray column, 14, air inlet, 15, exhaust outlet.
Detailed description of the invention
In order to make object of the present invention, technical scheme and advantage clearly understand, below in conjunction with drawings and Examples, the present invention is further elaborated.Should be appreciated that specific embodiment described herein only in order to explain the present invention, be not intended to limit the present invention.
The invention discloses a kind of sodium metasilicate tail gas treatment process, comprise the steps:
A, dust removal step;
B, cooling step, be cooled to less than 80 DEG C by the tail gas after dedusting;
C, some grades of tail gas absorption steps, tail gas after cooling is passed into the some grades of absorption plants be cascaded, the shower that concentration is the sodium hydroxide solution of 30% is equipped with in absorption plant described in every one-level, described tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to described shower and continues spray utilization, if the concentration of described sulfur dioxide in tail gas is less than 18mg/m
3, be then discharged into external environment condition from the upper end of described absorption plant, otherwise continue to enter next stage absorption plant;
D, the sodium sulfite solution of absorption plant being positioned at downstream are communicated with the shower of upper level absorption plant with the mixed liquor of sodium hydroxide solution.
In order to prevent body of heater smoke pollution environment, the body of heater flue gas collected around boiler being passed into second level absorption plant, the sulfur content passed in the absorption plant tail gas of the second level can be increased.
Certainly, first order absorption plant cyclic process sulfite sodium and tail gas continue reaction and generate sodium hydrogensulfite, when the proportion of the sodium hydrogensulfite that first order absorption plant generates is 1.34-1.36, described sodium hydrogensulfite is exported, sodium sulfite is prepared with the solution of sodium bisulfite that proportion is 1.34-1.36, sodium sulfite can be used as accessory substance, increases economic benefit.
The sodium metasilicate tail gas treatment process that the embodiment of the present invention provides, because sodium metasilicate tail gas is through some grades of tail gas absorption, the concentration of sulfur dioxide in tail gas is less than 18mg/m
3, thus the content of sulfur dioxide in tail gas is up to standard, can directly be discharged in external environment condition, decreases the adverse effect of exhaust emissions to environment, avoids environmental pollution; Mixed liquor due to the sodium sulfite solution with sodium hydroxide solution that are positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant, and thus in whole sweetening process, the aqueous solution recycles, completely without waste sludge discharge.
As shown in Figure 1, the invention also discloses a kind of sodium metasilicate tail gas treatment device, comprise the dust arrester 1 be communicated with sodium metasilicate tail gas, dust arrester 1 is bag-type dust collector, dust arrester 1 is communicated with cooling heat exchange device 2, cooling heat exchange device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after heat exchange for the production of and heating, save energy consumption, optimize tail gas parameter for rear road absorption technique simultaneously, cooling heat exchange device 2 is communicated with some grades of absorption plants, some grades of absorption plants are cascaded, the progression of absorption plant is set according to the concentration of sulfur dioxide in tail gas, the concentration of such as kiln sulfur dioxide in tail gas is 31mg/m
3, body of heater sulfur dioxide in flue gas concentration is 100.2mg/m
3, design three grades of absorption plants, cooling heat exchange device 2 is communicated with the first order absorption plant 3 of connecting successively, second level absorption plant 4 and third level absorption plant 5, body of heater fume collection pipeline 6 for collecting body of heater flue gas around boiler is communicated with second level absorption plant 4, not only prevent body of heater smoke pollution environment, and the sulfur content passed in second level absorption plant 4 tail gas can be increased, the shower 7 for being atomized circulation fluid is equipped with in every grade of absorption plant, the below of shower 7 arranges agitator tank 8, discharge gate 81 is provided with bottom agitator tank 8, the top of agitator tank 8 is provided with feeding tube 82, the feeding tube 82 of agitator tank 8 is all communicated with the first liquid caustic soda tank 9 of the sodium hydroxide solution containing concentration being 30%, certainly, the concentration of sodium hydroxide solution also can be 32%, also sodium carbonate liquor can be selected to replace sodium hydroxide solution, the sidewall of agitator tank 8 is provided with fluid pipeline 83, this fluid pipeline 83 is communicated with shower 7 by liquor pump 10, the discharge gate 81 being positioned at the absorption plant in downstream is communicated with the shower 7 of upper level absorption plant, the discharge gate 81 of first order absorption plant 3 is communicated with neutralization reaction still 11, neutralization reaction still 11 is communicated with the second liquid caustic soda tank 12 of the sodium hydroxide solution containing concentration being 30%, when the proportion of the solution of sodium bisulfite that first order absorption plant 3 generates is 1.34-1.36, be expelled in neutralization reaction still 11, after sodium hydroxide solution hybrid reaction, generate sodium sulfite as accessory substance, economic benefit can be increased.
In order to accelerate infiltration rate and the uptake of sodium metasilicate sulfur dioxide in tail gas, first order absorption plant 3 comprises two spray columns be arranged in parallel 13, second level absorption plant 4 also comprises two spray columns be arranged in parallel 13, and third level absorption plant 5 comprises a spray column.
The sodium metasilicate tail gas treatment device that the embodiment of the present invention provides, owing to devising first order absorption plant 3, second level absorption plant 4 and third level absorption plant 5, the desulfurization degree of every grade of absorption plant is greater than 92%, total desulfurization degree of three grades of absorption plants reaches 99.95%, sodium metasilicate tail gas is by the absorption of three grades of absorption plants, and the concentration of sulfur dioxide in tail gas is less than 18mg/m
3, thus the content of sulfur dioxide in tail gas is up to standard, can directly be discharged in external environment condition, decreases the adverse effect of exhaust emissions to environment, avoids environmental pollution; Because the discharge gate 81 being positioned at the absorption plant in downstream is communicated with the shower 7 of upper level absorption plant, thus in whole sweetening process, the aqueous solution recycles, completely without waste sludge discharge.
Embodiment one:
As Fig. 1 and Fig. 2 jointly shown in, produce the tail gas produced in sodium metasilicate process, kiln tail gas generation is 24000m
3/ h, sulfur dioxide concentration is 31g/m
3; Body of heater smoke yields is 5640m
3/ h, sulfur dioxide concentration is 100.2mg/m
3.
A, dust removal step, be that the kiln tail gas of 1100 DEG C passes into flue after dust arrester 1 dedusting by temperature, after flue, kiln exhaust temperature reduces to 400 DEG C;
B, cooling step, kiln tail gas after dedusting is passed into cooling heat exchange device 2 by air-introduced machine, cool to less than 80 DEG C, cooling heat exchange device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after heat exchange for the production of and heating, saved energy consumption, optimized tail gas parameter for rear road absorption technique simultaneously;
C, the first order absorb: the air inlet 14 kiln tail gas after cooling being passed into first order absorption plant 3 by air-introduced machine, the concentration of sulfur dioxide in tail gas is 31g/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in first order absorption plant 3, kiln tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to shower 7 and continues spray utilization, first order absorption plant 3 cyclic process sulfite sodium and tail gas continue reaction and generate sodium hydrogensulfite, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.36, solution of sodium bisulfite is exported to neutralization reaction still 11, with the NaOH hybrid reaction that concentration is 30%, generate sodium sulfite, after fractional crystallization, prepare sodium sulfite finished product, economic benefit can be increased, then the mixed liquor of the sodium sulfite solution in second level absorption plant 4 and sodium hydroxide solution is delivered to the shower 7 of first order absorption plant 3, the absorptivity of the sulfur dioxide of first order absorption plant 3 is greater than 92%, the concentration of kiln sulfur dioxide in tail gas is lower than 2.48g/m
3, kiln tail gas is discharged from the exhaust outlet 15 of first order absorption plant 3,
D, the second level absorb: the kiln tail gas of being discharged by first order absorption plant 3 and body of heater flue gas pass into the air inlet 14 of second level absorption plant 4, and the concentration of kiln sulfur dioxide in tail gas is lower than 2.48g/m
3, body of heater sulfur dioxide in flue gas concentration is 100.2mg/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in second level absorption plant 4, tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to shower 7 and continues spray utilization, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.36, the mixed liquor of the sodium sulfite solution in second level absorption plant 4 and sodium hydroxide solution is delivered to the shower 7 of first order absorption plant 3, then the mixed liquor of the sodium sulfite solution in third level absorption plant 5 and sodium hydroxide solution is delivered to the shower 7 of second level absorption plant 4, the absorptivity of the sulfur dioxide of first order absorption plant 3 is greater than 92%, the concentration of sulfur dioxide in tail gas is lower than 0.206g/m
3, tail gas is discharged from the exhaust outlet 15 of second level absorption plant 4,
E, the third level absorb: the air inlet 14 tail gas that second level absorption plant 4 is discharged being passed into third level absorption plant 5, the concentration of sulfur dioxide in tail gas is lower than 0.206g/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in third level absorption plant 5, tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, sodium sulfite solution and sodium hydroxide solution are circulated to shower 7 and continue spray utilization, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.36, the mixed liquor of the sodium sulfite solution in third level absorption plant 5 and sodium hydroxide solution is delivered to the shower 7 of second level absorption plant 4, the absorptivity of sulfur dioxide in tail gas is greater than 92%, the concentration of sulfur dioxide in tail gas is lower than 16.48mg/m
3, tail gas is discharged into external environment condition from the exhaust outlet 15 of third level absorption plant 5.
Embodiment two:
As Fig. 1 and Fig. 2 jointly shown in, produce the tail gas produced in sodium metasilicate process, kiln tail gas generation is 19355m
3/ h, sulfur dioxide concentration is 25g/m
3; Body of heater smoke yields is 4548m
3/ h, sulfur dioxide concentration is 81mg/m
3.
A, dust removal step, be that the kiln tail gas of 1100 DEG C passes into flue after dust arrester 1 dedusting by temperature, after flue, kiln exhaust temperature reduces to 350 DEG C;
B, cooling step, kiln tail gas after dedusting is passed into cooling heat exchange device 2 by air-introduced machine, cool to less than 80 DEG C, cooling heat exchange device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after heat exchange for the production of and heating, saved energy consumption, optimized tail gas parameter for rear road absorption technique simultaneously;
C, the first order absorb: the air inlet 14 kiln tail gas after cooling being passed into first order absorption plant 3 by air-introduced machine, the concentration of sulfur dioxide in tail gas is 25g/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in first order absorption plant 3, kiln tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to shower 7 and continues spray utilization, first order absorption plant 3 cyclic process sulfite sodium and tail gas continue reaction and generate sodium hydrogensulfite, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.34, solution of sodium bisulfite is exported to neutralization reaction still 11, with the NaOH hybrid reaction that concentration is 30%, generate sodium sulfite, after fractional crystallization, prepare sodium sulfite finished product, economic benefit can be increased, then the mixed liquor of the sodium sulfite solution in second level absorption plant 4 and sodium hydroxide solution is delivered to the shower 7 of first order absorption plant 3, the absorptivity of the sulfur dioxide of first order absorption plant 3 is greater than 92%, the concentration of kiln sulfur dioxide in tail gas is lower than 2g/m
3, kiln tail gas is discharged from the exhaust outlet 15 of first order absorption plant 3,
D, the second level absorb: the kiln tail gas of being discharged by first order absorption plant 3 and body of heater flue gas pass into the air inlet 14 of second level absorption plant 4, and the concentration of kiln sulfur dioxide in tail gas is lower than 2g/m
3, body of heater sulfur dioxide in flue gas concentration is 81mg/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in second level absorption plant 4, tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to shower 7 and continues spray utilization, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.34, the mixed liquor of the sodium sulfite solution in second level absorption plant 4 and sodium hydroxide solution is delivered to the shower 7 of first order absorption plant 3, then the mixed liquor of the sodium sulfite solution in third level absorption plant 5 and sodium hydroxide solution is delivered to the shower 7 of second level absorption plant 4, the absorptivity of the sulfur dioxide of first order absorption plant 3 is greater than 92%, the concentration of sulfur dioxide in tail gas is lower than 0.166g/m
3, tail gas is discharged from the exhaust outlet 15 of second level absorption plant 4,
E, the third level absorb: the air inlet 14 tail gas that second level absorption plant 4 is discharged being passed into third level absorption plant 5, the concentration of sulfur dioxide in tail gas is lower than 0.166g/m
3, the shower 7 that concentration is the sodium hydroxide solution of 30% is provided with in third level absorption plant 5, tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, sodium sulfite solution and sodium hydroxide solution are circulated to shower 7 and continue spray utilization, when the proportion of the sodium hydrogensulfite that first order absorption plant 3 generates is 1.34, the mixed liquor of the sodium sulfite solution in third level absorption plant 5 and sodium hydroxide solution is delivered to the shower 7 of second level absorption plant 4, the absorptivity of sulfur dioxide in tail gas is greater than 92%, now the concentration of sulfur dioxide in tail gas is lower than 13.28mg/m
3, tail gas is discharged into external environment condition from the exhaust outlet 15 of third level absorption plant 5.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, all any amendments done within the spirit and principles in the present invention, equivalent replacement and improvement etc., all should be included within protection scope of the present invention.
Claims (5)
1. sodium metasilicate tail gas treatment process, is characterized in that, comprises the steps:
A, dust removal step;
B, cooling step, be cooled to less than 80 DEG C by the tail gas after dedusting;
C, some grades of tail gas absorption steps, tail gas after cooling is passed into the some grades of absorption plants be cascaded, the shower that concentration is the sodium hydroxide solution of 30% is equipped with in absorption plant described in every one-level, described tail gas and sodium hydroxide solution countercurrent reaction, countercurrent reaction generates sodium sulfite solution, the mixed liquor of sodium sulfite solution and sodium hydroxide solution is circulated to described shower and continues spray utilization, if the concentration of described sulfur dioxide in tail gas is less than 18mg/m
3, be then discharged into external environment condition from the upper end of described absorption plant, otherwise continue to enter next stage absorption plant;
D, the sodium sulfite solution of absorption plant being positioned at downstream are communicated with the shower of upper level absorption plant with the mixed liquor of sodium hydroxide solution; The body of heater flue gas collected around boiler passes into second level absorption plant.
2. sodium metasilicate tail gas treatment process according to claim 1, it is characterized in that, first order absorption plant cyclic process sulfite sodium and tail gas continue reaction and generate sodium hydrogensulfite, when the proportion of the sodium hydrogensulfite that first order absorption plant generates is 1.34-1.36, described sodium hydrogensulfite is exported.
3. sodium metasilicate tail gas treatment process according to claim 2, is characterized in that, prepares sodium sulfite with the solution of sodium bisulfite that proportion is 1.34-1.36.
4. sodium metasilicate tail gas treatment device, comprise the dust arrester be communicated with described sodium metasilicate tail gas, described dust arrester is communicated with cooling heat exchange device, described cooling heat exchange device is communicated with some grades of absorption plants, it is characterized in that, the described absorption plant of some levels is cascaded, the shower for being atomized circulation fluid is equipped with in every grade of described absorption plant, the below of described shower arranges agitator tank, discharge gate is provided with bottom described agitator tank, the top of described agitator tank is provided with feeding tube, the sidewall of described agitator tank is provided with fluid pipeline, described fluid pipeline is communicated with described shower by liquor pump, the discharge gate being positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant, for collecting the body of heater fume collection pipeline communication second level absorption plant of body of heater flue gas around boiler, the feeding tube of described agitator tank is all communicated with the first liquid caustic soda tank of the sodium hydroxide solution containing concentration being 30%, the discharge gate of first order absorption plant is communicated with neutralization reaction still.
5. sodium metasilicate tail gas treatment device according to claim 4, is characterized in that, described neutralization reaction still is communicated with the second liquid caustic soda tank of the sodium hydroxide solution containing concentration being 30%.
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| CN106745086A (en) * | 2016-12-30 | 2017-05-31 | 耒阳市焱鑫有色金属有限公司 | One kind Ca (OH)2And SO2Multi-stage countercurrent continuously reduces Na2SO4Generation Na2SO3Reaction tower |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4207299A (en) * | 1977-02-16 | 1980-06-10 | Davy Powergas, Inc. | Sulphur dioxide removal process |
| CN101982405A (en) * | 2010-11-10 | 2011-03-02 | 白银有色集团股份有限公司 | Method for preparing sulphurous acid by utilizing pyrite |
| CN102583452A (en) * | 2011-01-07 | 2012-07-18 | 北京柯兰富尔过滤技术有限公司 | Method and equipment for directly producing sodium sulfite by using sulfuric acid-containing gas |
| CN203043822U (en) * | 2012-12-01 | 2013-07-10 | 昌乐县兴魏化工有限公司 | Sodium silicate tail gas treatment device |
-
2012
- 2012-12-01 CN CN201210507766.XA patent/CN103007710B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4207299A (en) * | 1977-02-16 | 1980-06-10 | Davy Powergas, Inc. | Sulphur dioxide removal process |
| CN101982405A (en) * | 2010-11-10 | 2011-03-02 | 白银有色集团股份有限公司 | Method for preparing sulphurous acid by utilizing pyrite |
| CN102583452A (en) * | 2011-01-07 | 2012-07-18 | 北京柯兰富尔过滤技术有限公司 | Method and equipment for directly producing sodium sulfite by using sulfuric acid-containing gas |
| CN203043822U (en) * | 2012-12-01 | 2013-07-10 | 昌乐县兴魏化工有限公司 | Sodium silicate tail gas treatment device |
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