CN203043822U - Sodium silicate tail gas treatment device - Google Patents
Sodium silicate tail gas treatment device Download PDFInfo
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- CN203043822U CN203043822U CN 201220652984 CN201220652984U CN203043822U CN 203043822 U CN203043822 U CN 203043822U CN 201220652984 CN201220652984 CN 201220652984 CN 201220652984 U CN201220652984 U CN 201220652984U CN 203043822 U CN203043822 U CN 203043822U
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Abstract
The utility model discloses a sodium silicate tail gas treatment device which belongs to the technical field of chemical engineering tail gas treatment. The sodium silicate tail gas treatment device comprises a dust collector which is connected with sodium silicate tail gas, wherein the dust collector is communicated with a cooling heat exchange device which is connected with a plurality of levels of absorption apparatuses, the plurality of levels of absorption apparatuses are connected in series, each level of absorption apparatus is internally provided with a spraying pipe which is used for atomizing a circulating liquid, a stirring tank is arranged below the spraying tank, a discharging port is formed in the bottom of the stirring tank, a liquid outlet pipeline is arranged on the side wall of the stirring tank and is connected with the spraying pipe through a liquid pump, and the discharging port of the absorption apparatus at the low position is connected with the spraying pipe of the upper level of the absorption apparatus. The sodium silicate tail gas treatment device can be used for effectively clearing away sulfur dioxide in the sodium silicate tail gas, so that the tail gas can be directly discharged to external environments after the content of the sulfur dioxide in the tail reaches the standard, the harmful effect of the tail gas on the environments is reduced, and the environmental pollution is avoided.
Description
Technical field
The utility model belongs to the chemical industry tail gas processing technology field, relates in particular to a kind of sodium metasilicate tail gas treatment device.
Background technology
Sodium metasilicate is commonly called as waterglass, bubble flower alkali, and its purposes is very extensive, almost spreads all over each department of national economy.Being widely used in various silicates products such as making silica gel, white carbon, zeolite molecular sieve, sodium metasilicate, Ludox, layer silicon and instant powdery bubble flower alkali, sodium potassium silicate in chemical industry, is the base stock of silicon compound; Being indispensable raw material in the washing agent such as washing powder, soap in light industry, also is water softener, settling agent; In textile industry, be used for helping dye, bleaching and sizing; In mechanical industry, be widely used in casting, emery wheel manufacturing and anticolodal etc. in addition.
Be that raw material is produced sodium metasilicate with soda ash, have big, the shortcomings such as the carbon emission amount is big, cost height of heat waste, therefore adopting glauber salt is that to replace soda ash be that raw material is produced sodium metasilicate to sodium sulphate.Because it has cost and reduces significantly, carbon emission reduces 95% with first-class advantage simultaneously, thereby has obtained using widely.
When glauber salt and quartz sand are raw material production sodium metasilicate, in the kiln calcination process, produce a large amount of kiln tail gas and body of heater flue gas, contain sulfur dioxide and dust in the tail gas.Adopt bag-type dust collector to carry out desulfurization and dedusting and handle, though the efficiency of dust collection height, dust qualified discharge in the tail gas, the sulfur dioxide in the tail gas are without effective processing, and sulfur dioxide can not be realized qualified discharge in the tail gas, can cause severe contamination to environment.
The utility model content
Technical problem to be solved in the utility model is: a kind of sodium metasilicate tail gas treatment device is provided, produces the tail gas that contains sulfur dioxide in the sodium metasilicate production process to solve, and without effective processing, the technical problem that environment is polluted.
For solving the problems of the technologies described above, the technical solution of the utility model is: the sodium metasilicate tail gas treatment device, comprise the dust arrester that is communicated with described sodium metasilicate tail gas, described dust arrester is communicated with the cooling heat transferring device, described cooling heat transferring device is communicated with some grades of absorption plants, the described absorption plant of some levels is cascaded, be equipped with the shower for the atomizing circulation fluid in every grade of described absorption plant, the below of described shower arranges agitator tank, described agitator tank bottom is provided with discharge gate, the top of described agitator tank is provided with feeding tube, the sidewall of described agitator tank is provided with the fluid pipeline, described fluid pipeline is communicated with described shower by the liquid pump, and the discharge gate that is positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant.
As a kind of improvement, be used for collecting the boiler body of heater flue gas collection conduit connection second level absorption plant of body of heater flue gas on every side.
As a kind of improvement, the feeding tube of described agitator tank is that the first liquid caustic soda jar of 30% sodium hydroxide solution is communicated with containing concentration all.
As a kind of improvement, the discharge gate of first order absorption plant is communicated with the neutralization reaction still.
As further improvement, described neutralization reaction still is that the second liquid caustic soda jar of 30% sodium hydroxide solution is communicated with containing concentration.
After having adopted technique scheme, the beneficial effects of the utility model are: owing to designed some grades of absorption plants, sodium metasilicate tail gas is by the absorption of some grades of absorption plants, and the concentration of sulfur dioxide is less than 18mg/m in the sodium metasilicate tail gas
3, thereby the content of sulfur dioxide is up to standard in the tail gas, can directly be discharged in the external environment condition, has reduced the adverse effect of exhaust emissions to environment, has avoided environmental pollution; Because the discharge gate that is positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant, thereby the aqueous solution is recycling fully in the whole sweetening process, no waste sludge discharge.
Owing to be used for collecting the boiler body of heater flue gas collection conduit connection second level absorption plant of body of heater flue gas on every side, thereby not only prevented body of heater smoke pollution environment, and can increase the sulfur content that feeds in the absorption plant tail gas of the second level.
Because the discharge gate of first order absorption plant is communicated with the neutralization reaction still, described neutralization reaction still is that the second liquid caustic soda jar of 30% sodium hydroxide solution is communicated with containing concentration, thereby the proportion of the solution of sodium bisulfite that generates when first order absorption plant is when being 1.34-1.36, be expelled in the neutralization reaction still, after the sodium hydroxide solution hybrid reaction, generate sodium sulfite as accessory substance, can increase economic benefit.
Description of drawings
Fig. 1 is structural representation of the present utility model;
Among the figure, 1, dust arrester, 2, the cooling heat transferring device, 3, first order absorption plant, 4, second level absorption plant, 5, third level absorption plant, 6, body of heater flue gas collection conduit, 7, shower, 8, agitator tank, 81, discharge gate, 82, feeding tube, 83, the fluid pipeline, 9, the first liquid caustic soda jar, 10, liquid pump, 11, the neutralization reaction still, 12, the second liquid caustic soda jar, 13, spray column, 14, air inlet, 15, exhaust outlet.
The specific embodiment
In order to make the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein only in order to explaining the utility model, and be not used in restriction the utility model.
As shown in Figure 1, the utility model discloses a kind of sodium metasilicate tail gas treatment device, comprise the dust arrester 1 that is communicated with sodium metasilicate tail gas, dust arrester 1 is bag-type dust collector, dust arrester 1 is communicated with cooling heat transferring device 2, cooling heat transferring device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after the heat exchange for the production of and heating, saved energy consumption, optimized the tail gas parameter for back road absorption technique simultaneously, cooling heat transferring device 2 is communicated with some grades of absorption plants, some grades of absorption plants are cascaded, and according to the concentration of sulfur dioxide in the tail gas progression of absorption plant are set, and are 31mg/m such as the concentration of sulfur dioxide in the kiln tail gas
3, body of heater sulfur dioxide in flue gas concentration is 100.2mg/m
3Design three grades of absorption plants, cooling heat transferring device 2 is communicated with the first order absorption plant 3 of series connection successively, second level absorption plant 4 and third level absorption plant 5, be used for collecting the boiler body of heater flue gas collection conduit 6 connection second level absorption plants 4 of body of heater flue gas on every side, not only prevented body of heater smoke pollution environment, and can increase the sulfur content that feeds in absorption plant 4 tail gas of the second level, be equipped with the shower 7 for the atomizing circulation fluid in every grade of absorption plant, the below of shower 7 arranges agitator tank 8, agitator tank 8 bottoms are provided with discharge gate 81, the top of agitator tank 8 is provided with feeding tube 82, the feeding tube 82 of agitator tank 8 is that the first liquid caustic soda jar 9 of 30% sodium hydroxide solution is communicated with containing concentration all, certainly, the concentration of sodium hydroxide solution also can be 32%, also can select for use sodium carbonate liquor 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 liquid pump 10, the discharge gate 81 that is 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 that the second liquid caustic soda jar 12 of 30% sodium hydroxide solution is communicated with containing concentration, when the proportion of the solution of sodium bisulfite that generates when first order absorption plant 3 is 1.34-1.36, be expelled in the neutralization reaction still 11, after the sodium hydroxide solution hybrid reaction, generate sodium sulfite as accessory substance, can increase economic benefit.
For infiltration rate and the uptake of accelerating sulfur dioxide in the sodium metasilicate tail gas, first order absorption plant 3 comprises two spray columns that are arranged in parallel 13, second level absorption plant 4 also comprises two spray columns that are arranged in parallel 13, and third level absorption plant 5 comprises a spray column.
The sodium metasilicate tail gas treatment device that the utility model provides, owing to designed 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 is less than 18mg/m in the tail gas
3, thereby the content of sulfur dioxide is up to standard in the tail gas, can directly be discharged in the external environment condition, has reduced the adverse effect of exhaust emissions to environment, has avoided environmental pollution; Because the discharge gate 81 that is positioned at the absorption plant in downstream is communicated with the shower 7 of upper level absorption plant, thereby the aqueous solution is recycling fully in the whole sweetening process, no waste sludge discharge.
Embodiment one:
Produce the tail gas that produces in the sodium metasilicate process, kiln tail gas generation is 24000m
3/ h, sulfur dioxide concentration are 31g/m
3; Body of heater flue gas generation is 5640m
3/ h, sulfur dioxide concentration are 100.2mg/m
3
A, dust removal step are that 1100 ℃ kiln tail gas feeds flue through after dust arrester 1 dedusting with temperature, reduce to 400 ℃ through kiln exhaust temperature behind the flue;
B, cooling step, kiln tail gas after the dedusting is fed cooling heat transferring device 2 by air-introduced machine, cool to below 80 ℃, cooling heat transferring device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after the heat exchange for the production of and heating, saved energy consumption, optimized the tail gas parameter for back road absorption technique simultaneously;
C, the first order absorb: the kiln tail gas after will cooling is by the air inlet 14 of air-introduced machine feeding first order absorption plant 3, and the concentration of sulfur dioxide is 31g/m in the tail gas
3Be provided with concentration in the first order absorption plant 3 and be the shower 7 of 30% sodium hydroxide solution, 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, sodium sulfite and tail gas continue reaction generation sodium hydrogensulfite in 3 cyclic processes of first order absorption plant, when the proportion of the sodium hydrogensulfite that generates when first order absorption plant 3 is 1.36, export solution of sodium bisulfite to neutralization reaction still 11, with concentration be 30% NaOH hybrid reaction, generate sodium sulfite, behind fractional crystallization, preparation sodium sulfite finished product, can increase economic benefit, then the mixed liquor of the sodium sulfite solution in the 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%, and the concentration of sulfur dioxide is lower than 2.48g/m in the kiln tail gas
3, kiln tail gas is discharged from the exhaust outlet 15 of first order absorption plant 3;
D, the second level absorb: with the kiln tail gas of first order absorption plant 3 discharges and the air inlet 14 of body of heater flue gas feeding second level absorption plant 4, the concentration of sulfur dioxide is lower than 2.48g/m in the kiln tail gas
3, body of heater sulfur dioxide in flue gas concentration is 100.2mg/m
3Be provided with concentration in the second level absorption plant 4 and be the shower 7 of 30% sodium hydroxide solution, 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 generates when first order absorption plant 3 is 1.36, the mixed liquor of the sodium sulfite solution in the 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 the 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%, and the concentration of sulfur dioxide is lower than 0.206g/m in the tail gas
3, tail gas is discharged from the exhaust outlet 15 of second level absorption plant 4;
E, the third level absorb: the tail gas that second level absorption plant 4 is discharged feeds the air inlet 14 of third level absorption plant 5, and the concentration of sulfur dioxide is lower than 0.206g/m in the tail gas
3Be provided with concentration in the third level absorption plant 5 and be the shower 7 of 30% sodium hydroxide solution, 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 generates when first order absorption plant 3 is 1.36, the mixed liquor of the sodium sulfite solution in the 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 is greater than 92% in the tail gas, and the concentration of sulfur dioxide is lower than 16.48mg/m in the tail gas
3, tail gas is discharged into the external environment condition from the exhaust outlet 15 of third level absorption plant 5.
Embodiment two:
Produce the tail gas that produces in the sodium metasilicate process, kiln tail gas generation is 19355m
3/ h, sulfur dioxide concentration are 25g/m
3; Body of heater flue gas generation is 4548m
3/ h, sulfur dioxide concentration are 81mg/m
3
A, dust removal step are that 1100 ℃ kiln tail gas feeds flue through after dust arrester 1 dedusting with temperature, reduce to 350 ℃ through kiln exhaust temperature behind the flue;
B, cooling step, kiln tail gas after the dedusting is fed cooling heat transferring device 2 by air-introduced machine, cool to below 80 ℃, cooling heat transferring device 2 comprises heat exchanger, can cool to high-temperature tail gas fast, hot water after the heat exchange for the production of and heating, saved energy consumption, optimized the tail gas parameter for back road absorption technique simultaneously;
C, the first order absorb: the kiln tail gas after will cooling is by the air inlet 14 of air-introduced machine feeding first order absorption plant 3, and the concentration of sulfur dioxide is 25g/m in the tail gas
3Be provided with concentration in the first order absorption plant 3 and be the shower 7 of 30% sodium hydroxide solution, 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, sodium sulfite and tail gas continue reaction generation sodium hydrogensulfite in 3 cyclic processes of first order absorption plant, when the proportion of the sodium hydrogensulfite that generates when first order absorption plant 3 is 1.34, export solution of sodium bisulfite to neutralization reaction still 11, with concentration be 30% NaOH hybrid reaction, generate sodium sulfite, behind fractional crystallization, preparation sodium sulfite finished product, can increase economic benefit, then the mixed liquor of the sodium sulfite solution in the 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%, and the concentration of sulfur dioxide is lower than 2g/m in the kiln tail gas
3, kiln tail gas is discharged from the exhaust outlet 15 of first order absorption plant 3;
D, the second level absorb: with the kiln tail gas of first order absorption plant 3 discharges and the air inlet 14 of body of heater flue gas feeding second level absorption plant 4, the concentration of sulfur dioxide is lower than 2g/m in the kiln tail gas
3, body of heater sulfur dioxide in flue gas concentration is 81mg/m
3Be provided with concentration in the second level absorption plant 4 and be the shower 7 of 30% sodium hydroxide solution, 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 generates when first order absorption plant 3 is 1.34, the mixed liquor of the sodium sulfite solution in the 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 the 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%, and the concentration of sulfur dioxide is lower than 0.166g/m in the tail gas
3, tail gas is discharged from the exhaust outlet 15 of second level absorption plant 4;
E, the third level absorb: the tail gas that second level absorption plant 4 is discharged feeds the air inlet 14 of third level absorption plant 5, and the concentration of sulfur dioxide is lower than 0.166g/m in the tail gas
3Be provided with concentration in the third level absorption plant 5 and be the shower 7 of 30% sodium hydroxide solution, 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 generates when first order absorption plant 3 is 1.34, the mixed liquor of the sodium sulfite solution in the 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 is greater than 92% in the tail gas, and the concentration of sulfur dioxide is lower than 13.28mg/m in the tail gas at this moment
3, tail gas is discharged into the external environment condition from the exhaust outlet 15 of third level absorption plant 5.
The above only is preferred embodiment of the present utility model; not in order to limit the utility model; all any modifications of within spirit of the present utility model and principle, doing, be equal to and replace and improvement etc., all should be included within the protection domain of the present utility model.
Claims (5)
1. sodium metasilicate tail gas treatment device, comprise the dust arrester that is communicated with described sodium metasilicate tail gas, described dust arrester is communicated with the cooling heat transferring device, described cooling heat transferring device is communicated with some grades of absorption plants, it is characterized in that, the described absorption plant of some levels is cascaded, be equipped with the shower for the atomizing circulation fluid in every grade of described absorption plant, the below of described shower arranges agitator tank, described agitator tank bottom is provided with discharge gate, the top of described agitator tank is provided with feeding tube, the sidewall of described agitator tank is provided with the fluid pipeline, described fluid pipeline is communicated with described shower by the liquid pump, and the discharge gate that is positioned at the absorption plant in downstream is communicated with the shower of upper level absorption plant.
2. sodium metasilicate tail gas treatment device according to claim 1 is characterized in that, is used for collecting the boiler body of heater flue gas collection conduit connection second level absorption plant of body of heater flue gas on every side.
3. sodium metasilicate tail gas treatment device according to claim 1 is characterized in that, the feeding tube of described agitator tank is that the first liquid caustic soda jar of 30% sodium hydroxide solution is communicated with containing concentration all.
4. sodium metasilicate tail gas treatment device according to claim 1 is characterized in that, the discharge gate of first order absorption plant is communicated with the neutralization reaction still.
5. sodium metasilicate tail gas treatment device according to claim 4 is characterized in that, described neutralization reaction still is that the second liquid caustic soda jar of 30% sodium hydroxide solution is communicated with containing concentration.
Priority Applications (1)
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|---|---|---|---|
| CN 201220652984 CN203043822U (en) | 2012-12-01 | 2012-12-01 | Sodium silicate tail gas treatment device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220652984 CN203043822U (en) | 2012-12-01 | 2012-12-01 | Sodium silicate tail gas treatment device |
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| CN203043822U true CN203043822U (en) | 2013-07-10 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007710A (en) * | 2012-12-01 | 2013-04-03 | 昌乐县兴魏化工有限公司 | Sodium silicate tail gas treatment process and treatment device thereof |
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2012
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007710A (en) * | 2012-12-01 | 2013-04-03 | 昌乐县兴魏化工有限公司 | Sodium silicate tail gas treatment process and treatment device thereof |
| CN103007710B (en) * | 2012-12-01 | 2016-02-17 | 昌乐县兴魏化工有限公司 | Sodium metasilicate tail gas treatment process and treatment facility thereof |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130710 Termination date: 20131201 |