CN101407327A - Production process for preparing sodium carbonate solution from caustic soda and carbon dioxide - Google Patents
Production process for preparing sodium carbonate solution from caustic soda and carbon dioxide Download PDFInfo
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- CN101407327A CN101407327A CNA2008101581745A CN200810158174A CN101407327A CN 101407327 A CN101407327 A CN 101407327A CN A2008101581745 A CNA2008101581745 A CN A2008101581745A CN 200810158174 A CN200810158174 A CN 200810158174A CN 101407327 A CN101407327 A CN 101407327A
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- soda ash
- packed absorber
- alkali lye
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention discloses a technology for preparing a sodium carbonate solution by using caustic soda and carbon dioxide, which comprises the following steps of: preparing 9%-11% alkali liquor by using 30% caustic soda in a make-up tank; pumping the alkali liquor into a plate-typed heat exchanger through an alkaline pump so as to achieve the object of temperature reduction; conveying the alkali liquor after temperature reduction to a secondary packing absorbing column; after liquid seal, conveying materials in the secondary packing absorbing column to a soda circulation tank at the bottom thereof, starting a soda circulation pump, simultaneously opening an outlet valve of the soda circulation pump so as to transfer the materials to a first packing absorbing column, conveying the carbon dioxide into the first packing absorbing column, dropping down the alkali liquor at the column top through an distributor which is inside the column, through the liquid seal, conveying the reacted liquor into a soda storage tank at the bottom of the first packing absorbing column; and then conveying the alkali liquor to users or into the storage tank. The method realizes the object of being capable of continually providing the sodium carbonate solution to the users directly, thus reducing production cost and labor intensity, eliminating environment pollution and having the advantage of saving energy and the like.
Description
Technical field
The present invention relates to the preparation method of yellow soda ash, is a kind of production technique of producing sodium carbonate solution with caustic soda and carbonic acid gas.
Background technology
The method of producing yellow soda ash has more multiple, and for example: solvay soda process, connection alkaline process etc., the yellow soda ash of producing with these methods re-uses after most number average need be made solution when industrial use.At present, use after solid sodium carbonate made solution, generally be that whole manual methods are finished, the deficiency of this method is: labour intensity is big, severe operational environment, production cost are higher relatively, and can't remove the micro-ammonia that exists in the solid sodium carbonate, use ammoniated sodium carbonate solution easily to influence quality product aborning, jeopardize the chlor-alkali production security of system when serious.
Summary of the invention
The objective of the invention is, provide a kind of and produce the production technique of sodium carbonate solution with caustic soda and carbonic acid gas, it can directly be supplied with the user who needs sodium carbonate solution continuously and use, thereby reduce production costs, improve production security, enhance productivity, improve the quality of products.
The present invention is achieved through the following technical solutions for achieving the above object: a kind ofly produce the production technique of sodium carbonate solution with caustic soda and carbonic acid gas, comprise the steps:
1. in material-compound tank, prepare the alkali lye of 9%-11% with 30% caustic soda;
2. alkali lye is pumped into the purpose that reaches cooling in the plate-type heat exchanger by lye pump;
3. again with the cooling alkali lye with 6.72m
3The flow volume delivery of/h is to the secondary packed absorber;
4. the material in the secondary packed absorber is admitted to through fluid-tight in the soda ash circulation tank of its bottom, when liquid level reaches 1/3-1/2 in the soda ash circulation tank, starts the soda ash recycle pump, opens soda ash circulating-pump outlet valve simultaneously and makes material deliver to the one-level packed absorber;
When 5. material is transported to the one-level packed absorber, in the one-level packed absorber, send into carbonic acid gas, carbonic acid gas is entered by one-level packed absorber bottom, alkali lye falls through sparger in the tower at cat head, carry out chemical absorption at filling surface, reacted liquid enters in the soda ash hold tank of one-level packed absorber bottom through fluid-tight;
6. unabsorbed carbonic acid gas is entered in the secondary packed absorber by one-level packed absorber top, carries out chemical absorption with alkali lye, and the liquid after reaction absorbs forms cycle operation with the operation of step after 3. in fluid-tight enters the soda ash circulation tank of tower bottom;
7. controlling the interior alkali lye pH value of soda ash hold tank is between the 11.89-12.5, at this moment, alkali lye can be delivered in user or the hold-up vessel.
Alkali lye pH value in the control soda ash hold tank, when pH value 〉=12.5, the working condition of the valve of installing on each pipeline is as follows: second valve, the 3rd valve and the 5th valve open, first valve, the 4th valve and the 6th valve closes, solution in the soda ash hold tank is pumped in the one-level packed absorber by soda ash and carries out the cyclic chemical absorption with carbonic acid gas, simultaneously, the carbonic acid gas that has not absorbed that cat head comes out enters in the secondary packed absorber, with the solution formation circulation absorption in the soda ash circulation tank; Close the alkali lye valve that enters the secondary packed absorber by material-compound tank this moment, when pH value≤11.89, alkali lye enters the soda ash circulation tank by the secondary packed absorber, after the alkali lye in the soda ash circulation tank enters the one-level packed absorber, enters in the soda ash hold tank of one-level packed absorber bottom.At this moment, first valve, the 6th valve open, second valve, the 3rd valve, the 4th valve and the 5th valve closes.
The invention has the advantages that: it has realized that direct successive provides the purpose of sodium carbonate solution to the user, thereby reduced production cost, and reduced labour intensity, eliminated environmental pollution, simultaneously owing to do not contain ammonia in the sodium carbonate solution, so thoroughly avoided the harm that ammonia is produced the chlor-alkali enterprise security in the solid sodium carbonate, reduce production costs approximately about 30% with comparing with the use of solid sodium carbonate obtain solution, the present invention also has the advantage of save energy etc.
Description of drawings
Accompanying drawing 1 is technological process of production figure of the present invention.
Embodiment
Production technique of the present invention comprises the steps:
1. in material-compound tank 9, prepare the alkali lye of 9%-11% with 30% caustic soda;
2. alkali lye is pumped into the purpose that reaches cooling in the plate-type heat exchanger 7 by lye pump 8;
3. again with the cooling alkali lye with 6.72m
3The flow volume delivery of/h is to secondary packed absorber 2;
4. the material in the secondary packed absorber 2 is admitted in the soda ash circulation tank 4 of its bottom through fluid-tight 17, when liquid level reaches 1/3-1/2 in the soda ash circulation tank 4, start soda ash recycle pump 3, open soda ash circulating-pump outlet valve simultaneously and make material deliver to one-level packed absorber 1;
When 5. material is transported to one-level packed absorber 1, in one-level packed absorber 1, send into carbonic acid gas, carbonic acid gas is entered by one-level packed absorber 1 bottom, alkali lye falls through sparger in the tower at cat head, carry out chemical absorption at filling surface, reacted liquid enters in the soda ash hold tank 6 of one-level packed absorber 1 bottom through fluid-tight 18;
6. unabsorbed carbonic acid gas is entered in the secondary packed absorber 2 by one-level packed absorber 1 top, carry out chemical absorption with alkali lye, liquid after reaction absorbs forms cycle operation with the operation of step after 3. in fluid-tight 17 enters the soda ash circulation tank 4 of tower bottom;
7. controlling soda ash hold tank 6 interior alkali lye pH values is between the 11.89-12.5, at this moment, alkali lye can be delivered in user or the hold-up vessel.
Alkali lye pH value in the control soda ash hold tank 6, adopt valve, realize control automatically by circuit, when pH value 〉=12.5, the working condition of the valve of installing on each pipeline is as follows: second valve 12, the 3rd valve 13 and the 5th valve 15 are opened, first valve 11, the 4th valve 14 and the 6th valve 16 are closed, solution in the soda ash hold tank 6 is sent in the one-level packed absorber 1 by soda ash pump 5 and is carried out the cyclic chemical absorption with carbonic acid gas, simultaneously, the carbonic acid gas that has not absorbed that cat head comes out enters in the secondary packed absorber 2, with the solution formation circulation absorption in the soda ash circulation tank 4; Close the alkali lye valve that enters secondary packed absorber 2 by material-compound tank 9 this moment, when pH value≤11.89, alkali lye enters soda ash circulation tank 4 by secondary packed absorber 2, after alkali lye in the soda ash circulation tank 4 enters one-level packed absorber 1 by pump 3, enter in the soda ash hold tank 6 of one-level packed absorber 1 bottom through fluid-tight 18, at this moment, first valve 11, the 6th valve 16 are opened, and second valve 12, the 3rd valve 13, the 4th valve 14 and the 5th valve 15 are closed.
One-level packed absorber 1 described in the production technique of the present invention and secondary packed absorber 2 are known configurations, wherein used filler is a polyethylene ladder ring, model is 25 * 17.5 * 1.4, packed height is 3.5 meters, plate-type heat exchanger described in the production technique, pump, jar and valve etc. are known technology, its structure and principle of work are repeated no more, various by-pass valve controls are connected with the distribution controlling box by circuit, electric control principle is a known technology, first valve 11 that uses among the embodiment, second valve 12, the 3rd valve 13 and the 5th valve 15 are opened, and the 4th valve 14 and the 6th valve 16 are the ASHL trip valve.
Claims (2)
1, a kind ofly produces the production technique of sodium carbonate solution, it is characterized in that: comprise the steps: with caustic soda and carbonic acid gas
1. in material-compound tank (9), prepare the alkali lye of 9%-11% with 30% caustic soda;
2. alkali lye is delivered to the purpose that reaches cooling in the plate-type heat exchanger (7) by lye pump (8);
3. the alkali lye after will lowering the temperature again is with 6.72m
3The flow volume delivery of/h is to secondary packed absorber (2);
4. the material in the secondary packed absorber (2) is admitted in the soda ash circulation tank (4) of its bottom through fluid-tight (17), when liquid level reaches 1/3-1/2 in the soda ash circulation tank (4), opens soda ash recycle pump terminal valve, starts soda ash recycle pump (3), with 6.72m
3The flow of/h is delivered to one-level packed absorber (1) with material;
When 5. material is transported to one-level packed absorber (1), in one-level packed absorber (1), send into carbonic acid gas, carbonic acid gas is entered by one-level packed absorber (1) bottom, alkali lye falls through sparger in the tower at cat head, carry out chemical absorption at filling surface, reacted liquid enters in the soda ash hold tank (6) of one-level packed absorber (1) bottom through fluid-tight (18);
6. unabsorbed carbonic acid gas is entered in the secondary packed absorber (2) by one-level packed absorber (1) top, carry out chemical absorption with alkali lye, liquid after reaction absorbs forms cycle operation with the operation of step after 3. in fluid-tight (17) enters the soda ash circulation tank (4) of tower bottom;
7. controlling the interior alkali lye pH value of soda ash hold tank (6) is between the 11.89-12.5, at this moment, alkali lye can be delivered in user or the hold-up vessel.
2, a kind of production technique of producing sodium carbonate solution with caustic soda and carbonic acid gas according to claim 1, it is characterized in that: the interior alkali lye pH value of control soda ash hold tank (6), when pH value 〉=12.5, the working condition of the valve of installing on each pipeline is as follows: second valve (12), the 3rd valve (13) and the 5th valve (15) are opened, first valve (11), the 4th valve (14) and the 6th valve (16) are closed, solution in the soda ash hold tank (6) is sent in the one-level packed absorber (1) by soda ash pump (5) and is carried out the cyclic chemical absorption with carbonic acid gas, simultaneously, the carbonic acid gas that has not absorbed that cat head comes out enters in the secondary packed absorber (2), with the solution formation circulation absorption in the soda ash circulation tank (4); Close the alkali lye valve that enters secondary packed absorber (2) by material-compound tank (9) this moment, when pH value≤11.89, alkali lye enters soda ash circulation tank (4) by secondary packed absorber (2), after alkali lye in the soda ash circulation tank (4) enters one-level packed absorber (1) by pump (3), enter through fluid-tight (18) in the soda ash hold tank (6) of one-level packed absorber (1) bottom, at this moment, first valve (11), the 6th valve (16) are opened, and second valve (12), the 3rd valve (13), the 4th valve (14) and the 5th valve (15) are closed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101581745A CN101407327A (en) | 2008-10-30 | 2008-10-30 | Production process for preparing sodium carbonate solution from caustic soda and carbon dioxide |
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2008101581745A CN101407327A (en) | 2008-10-30 | 2008-10-30 | Production process for preparing sodium carbonate solution from caustic soda and carbon dioxide |
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| CN101407327A true CN101407327A (en) | 2009-04-15 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891256A (en) * | 2010-08-16 | 2010-11-24 | 孙全海 | Production technique of high-purity potassium permanganate and manganese dioxide, and carbon dioxide reaction tower |
| CN106187679A (en) * | 2016-06-29 | 2016-12-07 | 山东聊城中盛蓝瑞化工有限公司 | The recycling system and method for carbon dioxide in a kind of chlorinated hydrocabon hydrolysis tail gas |
| CN107934964A (en) * | 2017-12-18 | 2018-04-20 | 青海盐湖工业股份有限公司 | A kind of carbon dioxide method of comprehensive utilization |
| CN109012089A (en) * | 2018-06-28 | 2018-12-18 | 北京科技大学 | A method of carbon dioxide is trapped using potassium hydroxide and potassium carbonate |
-
2008
- 2008-10-30 CN CNA2008101581745A patent/CN101407327A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891256A (en) * | 2010-08-16 | 2010-11-24 | 孙全海 | Production technique of high-purity potassium permanganate and manganese dioxide, and carbon dioxide reaction tower |
| CN101891256B (en) * | 2010-08-16 | 2011-06-15 | 孙全海 | Production technique of high-purity potassium permanganate and manganese dioxide, and carbon dioxide reaction tower |
| CN106187679A (en) * | 2016-06-29 | 2016-12-07 | 山东聊城中盛蓝瑞化工有限公司 | The recycling system and method for carbon dioxide in a kind of chlorinated hydrocabon hydrolysis tail gas |
| CN107934964A (en) * | 2017-12-18 | 2018-04-20 | 青海盐湖工业股份有限公司 | A kind of carbon dioxide method of comprehensive utilization |
| CN109012089A (en) * | 2018-06-28 | 2018-12-18 | 北京科技大学 | A method of carbon dioxide is trapped using potassium hydroxide and potassium carbonate |
| CN109012089B (en) * | 2018-06-28 | 2021-04-16 | 北京科技大学 | Method for capturing carbon dioxide by using potassium hydroxide and potassium carbonate |
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Open date: 20090415 |