CN103319024A - Lime-carbon dioxide method nitrate water purification process - Google Patents
Lime-carbon dioxide method nitrate water purification process Download PDFInfo
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- CN103319024A CN103319024A CN2013102230535A CN201310223053A CN103319024A CN 103319024 A CN103319024 A CN 103319024A CN 2013102230535 A CN2013102230535 A CN 2013102230535A CN 201310223053 A CN201310223053 A CN 201310223053A CN 103319024 A CN103319024 A CN 103319024A
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- order reaction
- glass gall
- lime
- solution
- flocculation agent
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Abstract
The invention relates to a lime-carbon dioxide method nitrate water purification process with the following technical steps of: (A) lime milk preparation; (B) primary flocculant solution preparation; (C) primary reaction; (D) carbon dioxide preparation; (E) secondary flocculant solution preparation; and (F) secondary reaction. According to the invention, Ca<2+> and Mg<2+> in nitrate water are removed by using carbon dioxide in quick lime and flue gas, such that steam consumption of nitrate production enterprises is reduced, and carbon dioxide discharge of thermal power plant or boiler room is reduced. Therefore, the novel process method is provided for nitrate water purification.
Description
Technical field
The invention belongs to the glass gall field of purification, particularly remove Ca in the raw material glass gall
2+And Mg
2+Lime-carbon dioxide process glass gall purification process.
Background technology
In the raw material glass gall that Sodium sulfate anhydrous.min(99) (anhydrous sodium sulphate, lower same) manufacturing enterprise adopts, except H
2Outside the O, mainly contain and Na
2SO
4(content range is between 120 ~ 330 g/l), next contains the NaCl(content range between 0 ~ 140 g/l), minor compound is CaSO
4And MgSO
4(content range is all between 0 ~ 4g/l).Ca in the glass gall
2+In evaporation nitre production process processed, can generate CaSO
4Affect quality product, and Mg
2+In evaporative process, can improve the boiling point of solution, not only reduce significantly heat transfer efficiency, also cause heating tube to clean frequent, affect the effective production time of system.
Along with the whole world for the improving constantly of environmental protection requirement, energy-saving and emission-reduction require also more and more higher.By the glass gall purification process, reduce the Ca in the refining glass gall
2+, Mg
2+Concentration, can effectively address this problem, guarantee quality product, improve system's heat transfer property, prolong effective production time.
Traditional glass gall purifying method adopts " caustic soda-soda ash " method.Because caustic soda and soda ash price are significantly soaring in the world, purify cost thereby increased substantially glass gall.But the price of Sodium sulfate anhydrous.min(99) presents descending trend.Therefore, adopting novel method effectively to reduce production costs has great importance.
Summary of the invention
The present invention aims to provide a kind of lime-carbon dioxide process and removes Ca2+ in the raw material glass gall and the purifying method of Mg2+.
Technical scheme of the present invention: lime-carbon dioxide process glass gall purification process, adopt following processing step:
(A) preparation of milk of lime: adopt unslaked lime and glass gall to carry out chemical reaction and make milk of lime, the Ca in the gained solution (OH) 2 content are 10%～15%, the solid-state Ca (OH) 2≤18% in the suspension;
(B) preparation of one-level flocculant solution: add non-ionic group thing flocculation agent in the solution, every cube of glass gall adds 2～3g flocculation agent, and the massfraction of flocculation agent is 0.08%～0.1% in the solution;
(C) first order reaction: the glass gall in the first order reaction bucket adds milk of lime under 20～100r/min mixing speed, add-on is controlled by the pH value, and the scope of pH system is 12.5～13; Continuation is stirred, and reacts to add the one-level flocculant solution in 5 hours afterwards; Stop to stir clarification more than 2 hours, the supernatant liquor of first order reaction changes second order reaction over to, and first order reaction mud pumps into mud disposal system;
(D) preparation of carbonic acid gas: the stack gas that adopts thermoelectric power station or boiler house to produce, CO2 content are between 10% ~ 12%, and stack gas is compressed after lowering the temperature by the washing tower washing;
(E) preparation of secondary flocculant solution: add anionic group thing flocculation agent in the solution, every cube of glass gall adds 2～3g flocculation agent, and the massfraction of flocculation agent is 0.08%～0.1% in the solution;
(F) second order reaction: the glass gall in the second order reaction bucket passes into carbonic acid gas under 20～100r/min mixing speed, add-on is controlled by the pH value, and the scope of pH system is between 11.5 ~ 12; Continue stirring and added the secondary flocculant solution in 2 hours afterwards; Stop to stir clarification more than 2 hours, the supernatant liquor of second order reaction just is refining glass gall, and second order reaction mud pumps into mud disposal system.
The described solution of said process is glass gall; Described unslaked lime content is CaO 〉=60%.
Described flocculation agent is group compound, comprises following two kinds:
(1) non-ionic group thing: such as Polyacrylamide, polyoxyethylene, polyvinyl alcohol etc.
(2) anionic group thing: such as sodium polyacrylate, ammonium polyacrylate etc.
Principle of the present invention:
(1) utilizes Ca (OH)
2With MgSO
4Chemical reaction occurs, and generates Mg (OH)
2Flocks.
(2) utilize Ca (OH)
2With Na
2SO
4Chemical reaction occurs, and generates NaOH.
(3) utilize CO
2With NaOH chemical reaction occuring, generates Na
2CO
3
(4) utilize Ca
2+With Na
2CO
3Chemical reaction occurs, and generates CaCO
3Precipitation.
(5) utilize respectively Mg (OH)
2, CaSO
4And CaCO
3Solubility product in glass gall generates respectively Mg (OH)
2, CaCO
3And CaSO
42H
2The O precipitation.
(6) adding of flocculation agent can be assembled the suspended particulates in the solution to connect forming thick cotton-shaped or agglomerate, is convenient to Mg (OH)
2, CaSO
42H
2O and CaCO
3Sedimentation.
The above-mentioned purifying method of process just can be removed Ca2+ and the Mg2+ in the raw material glass gall, makes refining glass gall, can utilize the laboratory to measure decontamination effect improving.That is: take quantitative different content glass gall to place beaker, reaction and sedimentation certain hour are measured the Ca in the clear liquid
2+And Mg
2+Content.Ca in the clear liquid
2+And Mg
2+Content less, decontamination effect improving is better, on the contrary then decontamination effect improving is poorer.
By the refining glass gall that the inventive method makes, can be used for the raw material that the Sodium sulfate anhydrous.min(99) evaporation is produced, the Ca in the raw material glass gall
2+And Mg
2+Clearance reaches respectively more than 90% and 95%.
Substantive distinguishing features of the present invention and marked improvement are: utilize the Ca in the co 2 removal raw material glass gall in unslaked lime and the stack gas
2+And Mg
2+, reduce the purification cost of Sodium sulfate anhydrous.min(99) manufacturing enterprise, reduced simultaneously the CO2 emissions of thermoelectric power station or boiler house, for purifying, glass gall provides new processing method.
Description of drawings
Fig. 1 is glass gall purification process sketch at intermittence.
Fig. 2 is continuous glass gall purification process sketch.
Embodiment
The below introduces four embodiment.Fig. 1 discontinuous glass gall purification process is identical with processing step and the parameter of continuous glass gall purification process among Fig. 2.Their difference is: intermittently the glass gall purification process be with reaction and clarification be placed on same have in the enough large container carry out; And the glass gall purification process is reaction to be placed on carry out in a certain amount of container continuously, and clarification is placed in a plurality of less containers to be carried out.Embodiment 1 and embodiment 3 adopt the glass gall purification process at intermittence of accompanying drawing 1, and embodiment 2 and embodiment 4 adopt the continuous glass gall purification process of accompanying drawing 2.
Embodiment 1:
Raw material glass gall composition is: H
2O=948.1g/l, Na
2SO
4=245 g/l, NaCl=4 g/l, CaSO
4=2.7 g/l, MgSO
4=0.2 g/l.Get raw material glass gall 1m
3, first order reaction adds 2.65kgCaO and continues stirring reaction and add one-level flocculation agent 2g after 5 hours under 20～100r/min mixing speed, stop to stir clarification 2 hours, the Mg in the measurement clear liquid
2+Be respectively 0.1ppm and 12.9 with pH value; Change the one-level clear liquid over to second order reaction, second order reaction passes into carbonic acid gas 1.90kg under 20～100r/min mixing speed, continues to stir, and adds secondary flocculation agent 2g after 2 hours, stops to stir clarification 2 hours, measures the Ca in the clear liquid
2+, Mg
2+Be respectively 44.7ppm, 0.1ppm and 11.6 with pH value.Clear liquid in the second order reaction bucket just is refining glass gall, and body refuse goes the body refuse treatment system in first order reaction bucket and the second order reaction bucket.Ca
2+And Mg
2+Clearance reaches respectively 94% and 99%, and the amount of carbon dioxide quantity discharged that reduces simultaneously is equivalent to 0.76kg mark coal.
Embodiment 2:
Raw material glass gall composition is: H
2O=924.2g/l, Na
2SO
4=268.3 g/l, NaCl=4 .76g/l, CaSO
4=2.78 g/l, MgSO
4=0.42 g/l.Get raw material glass gall 1m
3, first order reaction adds 2.82kgCaO under 20～100r/min continuously stirring rotating speed, and guarantees that the residence time more than 5 hours, changes the one-level clarifying equipment over to, adds simultaneously one-level flocculation agent 2g,, measure the Mg in the one-level clear liquid
2+Be respectively 0.1ppm and 12.9 with pH value; Change the clear liquid of one-level clarifying equipment over to the second order reaction bucket, second order reaction passes into carbonic acid gas 1.95kg under 20～100r/min continuously stirring rotating speed, and guarantees that the residence time more than 2 hours, changes the secondary clarifying equipment over to, add simultaneously secondary flocculation agent 2g, measure the Ca in the clear liquid
2+, Mg
2+Be respectively 36.6ppm, 0.1ppm and 11.6 with pH value.Clear liquid in the secondary clarifying equipment just is refining glass gall, and the body refuse in one-level clarifying equipment and the secondary clarifying equipment goes the body refuse treatment system.Ca
2+And Mg
2+Clearance reaches respectively 95% and 99%.
Embodiment 3:
Raw material glass gall composition is: H
2O=866.7g/l, Na
2SO
4=260g/l, NaCl=30g/l, CaSO
4=1.5g/l, MgSO
4=1.8g/l.Get raw material glass gall 1m
3, first order reaction adds 3.49kgCaO and continues stirring reaction and add one-level flocculation agent 2g after 5 hours under 20～100r/min mixing speed, stop to stir clarification 2 hours, the Mg in the measurement clear liquid
2+Be respectively 0.1ppm and 12.9 with pH value; Change the one-level clear liquid over to second order reaction, second order reaction passes into carbonic acid gas 1.97kg under 20～100r/min mixing speed, continues to stir, and adds secondary flocculation agent 2g after 2 hours, stops to stir clarification 2 hours, measures the Ca in the clear liquid
2+, Mg
2+Be respectively 35.7ppm, 0.1ppm and 11.6 with pH value.Clear liquid in the second order reaction bucket just is refining glass gall, and the body refuse in first order reaction bucket and the second order reaction bucket goes the body refuse treatment system.Ca
2+And Mg
2+Clearance reaches respectively 91.9% and 99%, and the amount of carbon dioxide quantity discharged that reduces simultaneously is equivalent to 0.78kg mark coal.
Embodiment 4:
Raw material glass gall composition is: H
2O=878g/l, Na
2SO
4=295g/l, NaCl=24.9g/l, CaSO
4=2g/l, MgSO
4=0.15g/l.Get raw material glass gall 1m
3, first order reaction adds 2.79kgCaO under 20～100r/min continuously stirring rotating speed, and guarantees that the residence time more than 5 hours, changes the one-level clarifying equipment over to, adds simultaneously one-level flocculation agent 2g,, measure the Mg in the one-level clear liquid
2+Be respectively 0.1ppm and 12.9 with pH value; Change the clear liquid of one-level clarifying equipment over to the second order reaction bucket, second order reaction passes into carbonic acid gas 1.36kg under 20～100r/min continuously stirring rotating speed, and guarantees that the residence time more than 2 hours, changes the secondary clarifying equipment over to, add simultaneously secondary flocculation agent 2g, measure the Ca in the clear liquid
2+, Mg
2+Be respectively 30.8ppm, 0.1ppm and 11.6 with pH value.Clear liquid in the secondary clarifying equipment just is refining glass gall, and the body refuse in one-level clarifying equipment and the secondary clarifying equipment goes the body refuse treatment system.Ca
2+And Mg
2+Clearance reaches respectively 95% and 99%, and the amount of carbon dioxide quantity discharged that reduces simultaneously is equivalent to 0.55kg mark coal.
Claims (1)
1. lime-carbon dioxide process glass gall purification process is characterized in that adopting following processing step:
(A) preparation of milk of lime: adopt unslaked lime and glass gall to carry out chemical reaction and make milk of lime, the Ca in the gained solution (OH) 2 content are 10%～15%, the solid-state Ca (OH) 2≤18% in the suspension;
(B) preparation of one-level flocculant solution: add non-ionic group thing flocculation agent in the solution, every cube of glass gall adds 2～3g flocculation agent, and the massfraction of flocculation agent is 0.08%～0.1% in the solution;
(C) first order reaction: the glass gall in the first order reaction bucket adds milk of lime under 20～100r/min mixing speed, add-on is controlled by the pH value, and the scope of pH system is 12.5～13; Continuation is stirred, and reacts to add the one-level flocculant solution in 5 hours afterwards; Stop to stir clarification more than 2 hours, the supernatant liquor of first order reaction changes second order reaction over to, and first order reaction mud pumps into mud disposal system;
(D) preparation of carbonic acid gas: the stack gas that adopts thermoelectric power station or boiler house to produce, CO2 content are between 10% ~ 12%, and stack gas is compressed after lowering the temperature by the washing tower washing;
(E) preparation of secondary flocculant solution: add anionic group thing flocculation agent in the solution, every cube of glass gall adds 2～3g flocculation agent, and the massfraction of flocculation agent is 0.08%～0.1% in the solution;
(F) second order reaction: the glass gall in the second order reaction bucket passes into carbonic acid gas under 20～100r/min mixing speed, add-on is controlled by the pH value, and the scope of pH system is between 11.5 ~ 12; Continue stirring and added the secondary flocculant solution in 2 hours afterwards; Stop to stir clarification more than 2 hours, the supernatant liquor of second order reaction just is refining glass gall, and second order reaction mud pumps into mud disposal system.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103693780A (en) * | 2013-12-20 | 2014-04-02 | 四川省洪雅青衣江元明粉有限公司 | Method and device for nitrified water purification used for comprehensive utilization of energy conservation and emission reduction |
| CN106986356A (en) * | 2017-05-12 | 2017-07-28 | 江西晶昊盐化有限公司 | A kind of lime-flue gas bittern purifying method |
| CN114261978A (en) * | 2021-12-22 | 2022-04-01 | 四川省洪雅青衣江元明粉有限公司 | Efficient purification method of saltpeter water |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102424403A (en) * | 2011-09-20 | 2012-04-25 | 四川同庆南风有限责任公司 | Removal of calcium and magnesium in anhydrous sodium sulfate flue gas and continuous feeding method |
-
2013
- 2013-06-06 CN CN2013102230535A patent/CN103319024A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102424403A (en) * | 2011-09-20 | 2012-04-25 | 四川同庆南风有限责任公司 | Removal of calcium and magnesium in anhydrous sodium sulfate flue gas and continuous feeding method |
Non-Patent Citations (7)
| Title |
|---|
| 《中国井矿盐》 19881231 黄觉民 石灰-(芒硝)-二氧化碳法处理硫酸钠型卤水 13-16 1 , 第5期 * |
| 《中国井矿盐》 20061231 邹志刚 浅谈石灰--二氧化碳法卤水净化工艺 1 第37卷, 第6期 * |
| 代承志 等: "硝水除钙镁新工艺", 《中国井矿盐》, no. 3, 31 December 1990 (1990-12-31) * |
| 段克明 等: "对硝水除钙镁生产工艺的研究", 《山西化工》, no. 1, 31 December 1998 (1998-12-31), pages 22 - 24 * |
| 胡西纯 等: "硝水采用石灰碳铵法除钙镁在我厂的研究与应用", 《中国井矿盐》, no. 6, 31 December 1994 (1994-12-31), pages 28 - 31 * |
| 邹志刚: "浅谈石灰——二氧化碳法卤水净化工艺", 《中国井矿盐》, vol. 37, no. 6, 31 December 2006 (2006-12-31) * |
| 黄觉民: "石灰—(芒硝)—二氧化碳法处理硫酸钠型卤水", 《中国井矿盐》, no. 5, 31 December 1988 (1988-12-31), pages 13 - 16 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103693780A (en) * | 2013-12-20 | 2014-04-02 | 四川省洪雅青衣江元明粉有限公司 | Method and device for nitrified water purification used for comprehensive utilization of energy conservation and emission reduction |
| CN106986356A (en) * | 2017-05-12 | 2017-07-28 | 江西晶昊盐化有限公司 | A kind of lime-flue gas bittern purifying method |
| CN106986356B (en) * | 2017-05-12 | 2018-03-20 | 江西晶昊盐化有限公司 | A kind of lime-flue gas bittern purifying method |
| CN114261978A (en) * | 2021-12-22 | 2022-04-01 | 四川省洪雅青衣江元明粉有限公司 | Efficient purification method of saltpeter water |
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Application publication date: 20130925 |