CN104437060A - Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery - Google Patents
Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery Download PDFInfo
- Publication number
- CN104437060A CN104437060A CN201410774822.5A CN201410774822A CN104437060A CN 104437060 A CN104437060 A CN 104437060A CN 201410774822 A CN201410774822 A CN 201410774822A CN 104437060 A CN104437060 A CN 104437060A
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- calcium carbonate
- calcium
- carbon
- storage tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills
Landscapes
- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
The invention discloses method and equipment for recovering, activating and utilizing carbon dioxide from a sugar refinery. The method comprises the following steps: introducing low-content carbon dioxide contained in flue gas of a boiler of the sugar refinery into a carbon dioxide adsorption tower, and reacting the carbon dioxide with lime cream inside the carbon dioxide adsorption tower to form a calcium carbonate solution; introducing a part of the calcium carbonate solution into phosphoric acid to generate calcium dihydrogen phosphate and the carbon dioxide, wherein the calcium dihydrogen phosphate is used for squeezing and secondary phosphorus addition; reacting the other part of the other part of the calcium carbonate solution with the carbon dioxide to generate calcium hydrogen carbonate, and pumping to mixed juice preliming, a floating device overflow pipe and a filtered juice quick-sinking reactor by using a calcium hydrogen carbonate pump. The method disclosed by the invention can be used for generating the calcium carbonate by reacting the low-concentration carbon dioxide contained in the flue gas of the boiler with the lime cream and preparing the calcium hydrogen carbonate and the calcium dihydrogen phosphate as clarifying agents used for the sugar refinery by utilizing the calcium carbonate and the phosphoric acid, thereby achieving the purpose of cane juice clarification by removing a part of colloid and non-sugar components in an adsorbing way, enhancing the CO2 utilization rate and reducing the discharge amount of the carbon dioxide from a chimney of the sugar refinery.
Description
Technical field
The present invention relates to carbon dioxide recovery Application way and equipment, be specially sugar refinery carbon dioxide recovery activation utilization method and apparatus.
Background technology
Cane sugar manufacture production technology has: sulfurous method and carbonatation process two kinds of techniques, wherein: sulfurous method sugar refining technology is due to more difficult removings of non-sugar impurities such as the colloid in syrup, Polyphenols, iron ions, and thus clarifying efficiency is lower than carbonatation process sugar refining technology.So the sugar product quality that the sugar product quality that sulfurous method sugar refining technology is produced is produced than carbonatation process sugar refining technology is slightly poor.
At present, sulfurous method sugar refining technology is all adopt lime and sulfur dioxide as fining agent, by adding the clarifying process that the steps such as ash, stove drying, neutralization, precipitate and separate have been come sugarcane juice and syrup.
Owing to carrying out will using a large amount of sulphur and phosphoric acid in clarifying process to sugarcane juice or syrup, so the sugar product credit rating of producing is lower than carbonatation process, sulfur content is high, not for shelf-stable, and sugar loss is also large.Although have a lot of research to the clarifying process of sugarcane juice and syrup for many years, propose many theories and technique, the change of its basic process is little.Recently, it is also proposed direct boiler flue (low pressure low concentration) carbon dioxide in carbonatation process clarification process of sugar production and make the sugar refining technology of fining agent, owing to being that the boiler combustion instability of fuel brings carbon dioxide in flue gas content not only on the low side but also unstable with bagasse, bring control very unstable to practicing in suitability for industrialized production, and only propose in carbonatation process clarification process of sugar production.
The high situation of low-quality white granulated sugar present situation and white granulated sugar production cost is produced in order to change sulfurous method sugar refining technology as early as possible, the great amount of carbon dioxide contained in cane sugar factory boiler flue being reclaimed and activating is applied in sulfurous method sugar refining technology, Substitute For Partial sulphur, phosphoric acid carry out full charge to sugarcane juice or syrup.And adopt current traditional natural full charge equipment, equipment investment is large, utilization rate of carbon dioxide is not high yet, does not reach the clarifying effect of expection.
Summary of the invention
In order to overcome the deficiencies in the prior art, the object of this invention is to provide flue gas low content carbon dioxide in a kind of employing absorption boiler and form calcium carbonate soln, in the middle of calcium carbonate soln, interval passes into carbon dioxide again, calcium carbonate part solution is made to change into calcium bicarbonate solution, for sugar refinery carbon dioxide recovery activation utilization method and apparatus of the clarification in the sugar refining technology of sugar refinery.
To achieve these goals, the technical solution used in the present invention is:
Sugar refinery carbon dioxide recovery activation utilization method, its processing step is:
The first step passes in carbon dioxide adsorption tower by the carbon dioxide of flue gas low content in the boiler of sugar refinery, milk of lime in carbon dioxide and tower carries out reaction and forms calcium carbonate soln, the pH value of calcium carbonate soln is 7.5-8.5, with Calcium Carbonate Filtration device, calcium carbonate soln is filtered again, after filtering out impurity and coarse granule, be placed in calcium carbonate storage tank for subsequent use.
Second step passes in carbon-dioxide generator by the calcium carbonate soln part in calcium carbonate storage tank, phosphoric acid again in phosphoric acid storage tank also passes in carbon-dioxide generator, calcium carbonate soln and phosphatase reaction produce biphosphate calcium solution and carbon dioxide, the pH value ﹤ 3 of biphosphate calcium solution, then by biphosphate calcium pump take out calcium dihydrogen phosphate go squeezing and secondary phosphorate; Phosphoric acid is food grade phosphoric acid.
3rd step passes in calcium carbonate activating tank by the calcium carbonate soln another part in calcium carbonate storage tank, the carbon dioxide reaction produced in calcium carbonate soln and carbon-dioxide generator produces calcium bicarbonate solution, and the calcium bicarbonate solution obtained is evacuated to the pre-ash of mixed juice, floating device overflow pipe and filtered juice heavy reactor soon.
The time that milk of lime in described carbon dioxide and tower carries out reacting is 10-20 minute, and temperature is 50-80 DEG C.
Described calcium carbonate soln and the time of phosphatase reaction are 1-5 minute, and temperature is 50-80 DEG C.
The equipment that sugar refinery carbon dioxide recovery activation utilization method adopts, comprise carbon dioxide adsorption tower, calcium carbonate storage tank, calcium carbonate activating tank, carbon-dioxide generator, phosphoric acid storage tank and biphosphate calcium pump, carbon dioxide adsorption tower connects sugar refinery boiler chimney, and carbon dioxide adsorption tower is by the pipeline of water flowing and milk of lime being connected to the Calcium Carbonate Filtration device that calcium carbonate storage tank top is provided with; Calcium carbonate storage tank connects calcium carbonate activating tank by a pipeline, calcium carbonate storage tank is connected to the carbon-dioxide generator being communicated with phosphoric acid storage tank by another pipeline, carbon-dioxide generator connects calcium carbonate activating tank by the pipeline of transport of carbon dioxide, carbon-dioxide generator also connects biphosphate calcium pump calcium dihydrogen phosphate pumped squeezing and secondary and phosphorate by pipeline, pipeline is provided with calcium dihydrogen phosphate pH value detector.
Above-mentioned equipment can realize automatically controlling by computer controller.
In calcium carbonate soln preparation, replace sugarcane juice with the milk of lime that concentration is 8-15 ° of Be and absorb carbon dioxide in flue gas and the byproduct generating decarbonizing process, i.e. calcium carbonate soln (being referred to as full charge).Their chemical equation is:
CO
2+H
2O = H
2CO
3
CaO+ H
2O = Ca(OH)
2
Ca(OH)
2+H
2CO
3= CaCO
3+2H
2O
With sugar phosphoric acid and above part calcium carbonate solution reaction, during control PH ﹤ 3, generation biphosphate calcium solution (another kind of excellent sugar fining agent) and concentration reach the carbon dioxide of more than 90%.Their chemical equation is:
CaCO
3+2H
3PO
4=Ca(H
2PO
4)
2+ H
2O + CO
2↑
With carbon dioxide ejector, the carbon dioxide of high concentration is injected calcium carbonate soln, allow dissolution of calcium carbonate activate as calcium bicarbonate solution.Their chemical equation is:
CaCO
3+ CO
2+H
2O = Ca(HCO
3)
2
The biphosphate calcium solution that above-mentioned decarburization and activation process produce, calcium bicarbonate solution are respectively charged in tank, quantitatively add with the sugarcane juice after the pre-ash of milk of lime with measuring pump, a large amount of newborn calcium carbonate, calcium monohydrogenphosphate and calcium phosphate precipitation particulate will be formed in sugarcane juice and adsorb the non-carbohydrate impurity in removing sugarcane juice.Their chemical equation is:
Ca(HCO
3)
2+ Ca(OH)
2= 2CaCO
3↓+2H
2O
Ca(H
2PO
4)
2+Ca(OH)
2=2CaHPO
4↓+2H
2O
2CaHPO
4+Ca(OH)
2=Ca3(PO
4)
2↓+2H
2O
The present invention utilizes the carbon dioxide of boiler flue low concentration and milk of lime to react and produces calcium carbonate, recycling part calcium carbonate and phosphoric acid prepare the carbon dioxide of calcium dihydrogen phosphate and high concentration, the carbon dioxide of high concentration and remaining calcium carbonate reaction is finally used to produce calcium bicarbonate, utilize calcium dihydrogen phosphate and calcium bicarbonate as the fining agent in sugar refinery, not only adsorptivity removes part colloid and non-sugar, reaches the object of rclarifying cane juice.But also improve CO2 utilization rate, reduce sugar refinery chimney CO2 emissions.
The present invention has the following advantages:
1, change boiler flue and recycle mode, make the CO of low content
2flue gas and milk of lime obtain sufficient blended absorbent and react in tower, greatly improve and absorb full charge effect, reduce CO2 emissions, improve CO
2utilization rate, raises the efficiency more than 20% than traditional full charge equipment;
2, formed brand-new with recovery boiler flue gas low concentration CO both at home and abroad
2as half carbon method process of producing sugar of fining agent;
3, boiler flue in tower through reaction after, the temperature of boiler flue drops to less than 75 DEG C by about 160 DEG C, is disposed to boiler chimney, decreases the discharge of heat.
4, utilize newborn calcium carbonate to have very large specific area and strong adsorption to remove part colloid and non-sugar, reach the object of rclarifying cane juice.
5, improve traditional sulfurous method production process owing to must use the auxiliary material such as a large amount of sulphur, phosphoric acid in process of production, cause the white granulated sugar sulfur content of production higher, quality is on the low side, easily returns the present situation of look, non-for shelf-stable.
6, control carbon method clarification process and produce a large amount of filter muds that cannot recycle, cause the present situation of serious environmental pollution.
7, the equipment adopted, has structure simple, installs, easy to maintenance, reliable, and recovery rate of CO 2 is high, cane juice clarification efficiency high.
Accompanying drawing explanation
Fig. 1 is the structural representation of the equipment that sugar refinery of the present invention carbon dioxide recovery activation utilization method adopts.
Title in figure and sequence number are:
Carbon dioxide adsorption tower 1, Calcium Carbonate Filtration device 2, calcium carbonate storage tank 3, pipeline 4, calcium carbonate activating tank 5, carbon-dioxide generator 6, phosphoric acid storage tank 7, calcium dihydrogen phosphate pH value detector 8, biphosphate calcium pump 9.
Detailed description of the invention
Introduce the present invention in order to more detailed, below in conjunction with accompanying drawing, the present invention will be further described.
Sugar refinery carbon dioxide recovery activation utilization method, its processing step is:
The first step adopts carbon dioxide adsorption tower 1 carbon dioxide separation of flue gas low content in the boiler of sugar refinery to be reclaimed, in carbon dioxide, add milk of lime again carry out reaction formation calcium carbonate soln, the pH value of calcium carbonate soln is 7.5-8.5, with Calcium Carbonate Filtration device 2, calcium carbonate soln is filtered again, after filtering out impurity and coarse granule, be placed in calcium carbonate storage tank 3 for subsequent use.
Second step passes in carbon-dioxide generator 6 by the calcium carbonate soln part in calcium carbonate storage tank 3, phosphoric acid again in phosphoric acid storage tank 7 also passes in carbon-dioxide generator 6, calcium carbonate soln and phosphatase reaction produce biphosphate calcium solution and carbon dioxide, the pH value ﹤ 3 of biphosphate calcium solution, then by biphosphate calcium pump 9 take out calcium dihydrogen phosphate go squeezing and secondary phosphorate; Phosphoric acid is sugar phosphoric acid.
3rd step passes in calcium carbonate activating tank 5 by the calcium carbonate soln another part in calcium carbonate storage tank 3, the carbon dioxide reaction produced in calcium carbonate soln and carbon-dioxide generator 6 produces calcium bicarbonate solution, and the calcium bicarbonate solution obtained is evacuated to the pre-ash of mixed juice, floating device overflow pipe and filtered juice heavy reactor soon.
The time that milk of lime in described carbon dioxide and tower carries out reacting is 10-20 minute, and temperature is 50-80 DEG C.
Described calcium carbonate soln and the time of phosphatase reaction are 1-5 minute, and temperature is 50-80 DEG C.
The equipment that sugar refinery carbon dioxide recovery activation utilization method adopts, comprise carbon dioxide adsorption tower 1, calcium carbonate storage tank 3, calcium carbonate activating tank 5, carbon-dioxide generator 6, phosphoric acid storage tank 7 and biphosphate calcium pump 8, carbon dioxide adsorption tower 1 connects sugar refinery boiler chimney, and carbon dioxide adsorption tower 1 is by the pipeline of water flowing and milk of lime being connected to the Calcium Carbonate Filtration device 2 that calcium carbonate storage tank 3 top is provided with; Calcium carbonate storage tank 3 connects calcium carbonate activating tank 5 by a pipeline 4, calcium carbonate storage tank 3 is connected to the carbon-dioxide generator 6 being communicated with phosphoric acid storage tank 7 by another pipeline 4, carbon-dioxide generator 6 connects calcium carbonate activating tank 5 by the pipeline 4 of transport of carbon dioxide, carbon-dioxide generator 6 also connects the biphosphate calcium pump 9 calcium dihydrogen phosphate pumped squeezing and secondary and phosphorate by pipeline 4, pipeline 4 is provided with calcium dihydrogen phosphate pH value detector 8.
Claims (6)
1. sugar refinery carbon dioxide recovery activation utilization method, is characterized in that: its processing step is:
The first step passes in carbon dioxide adsorption tower by the carbon dioxide of flue gas low content in the boiler of sugar refinery, milk of lime in carbon dioxide and tower carries out reaction and forms calcium carbonate soln, with Calcium Carbonate Filtration device, calcium carbonate soln is filtered again, after filtering out impurity and coarse granule, be placed in calcium carbonate storage tank for subsequent use;
Second step passes in carbon-dioxide generator by the calcium carbonate soln part in calcium carbonate storage tank, phosphoric acid in phosphoric acid storage tank also passes in carbon-dioxide generator, calcium carbonate soln and phosphatase reaction produce biphosphate calcium solution and carbon dioxide, the pH value ﹤ 3 of biphosphate calcium solution, then by biphosphate calcium pump take out calcium dihydrogen phosphate go squeezing and secondary phosphorate;
3rd step passes in calcium carbonate activating tank by the calcium carbonate soln another part in calcium carbonate storage tank, the carbon dioxide reaction produced in calcium carbonate soln and carbon-dioxide generator produces calcium bicarbonate solution, and the calcium bicarbonate solution obtained is evacuated to the pre-ash of mixed juice, floating device overflow pipe and filtered juice heavy reactor soon.
2. sugar refinery according to claim 1 carbon dioxide recovery activation utilization method, it is characterized in that: described calcium carbonate soln, its pH value is 7.5-8.5.
3. sugar refinery according to claim 1 carbon dioxide recovery activation utilization method, is characterized in that: the time that the milk of lime in described carbon dioxide and tower carries out reacting is 10-20 minute, and temperature is 50-80 DEG C.
4. sugar refinery according to claim 1 carbon dioxide recovery activation utilization method, it is characterized in that: described calcium carbonate soln and the time of phosphatase reaction are 1-5 minute, temperature is 50-80 DEG C.
5. sugar refinery according to claim 1 carbon dioxide recovery activation utilization method, it is characterized in that: the equipment adopted comprises carbon dioxide adsorption tower, calcium carbonate storage tank, calcium carbonate activating tank, carbon-dioxide generator, phosphoric acid storage tank and biphosphate calcium pump, carbon dioxide adsorption tower connects sugar refinery boiler chimney, and carbon dioxide adsorption tower is by the pipeline of water flowing and milk of lime being connected to the Calcium Carbonate Filtration device that calcium carbonate storage tank top is provided with; Calcium carbonate storage tank connects calcium carbonate activating tank by a pipeline, calcium carbonate storage tank is connected to the carbon-dioxide generator being communicated with phosphoric acid storage tank by another pipeline, carbon-dioxide generator connects calcium carbonate activating tank by the pipeline of transport of carbon dioxide, carbon-dioxide generator also connects biphosphate calcium pump calcium dihydrogen phosphate pumped squeezing and secondary and phosphorate by pipeline, pipeline is provided with calcium dihydrogen phosphate pH value detector.
6. sugar refinery according to claim 1 carbon dioxide recovery activation utilization method, is characterized in that: described phosphoric acid is food grade phosphoric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410774822.5A CN104437060A (en) | 2014-12-16 | 2014-12-16 | Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410774822.5A CN104437060A (en) | 2014-12-16 | 2014-12-16 | Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104437060A true CN104437060A (en) | 2015-03-25 |
Family
ID=52884274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410774822.5A Pending CN104437060A (en) | 2014-12-16 | 2014-12-16 | Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104437060A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107010739A (en) * | 2017-05-10 | 2017-08-04 | 烟台大学 | A kind of calcium hardness reduction method of nonferrous metallurgy acid waste water recycle-water |
| WO2020125459A1 (en) * | 2018-12-18 | 2020-06-25 | 浙江华康药业股份有限公司 | Xylose mother liquor continuous carbonation and impurity-removal device and method therefor |
| JP2021512640A (en) * | 2018-12-04 | 2021-05-20 | 浙江▲華▼康葯▲業▼股▲フン▼有限公司Ｚｈｅｊｉａｎｇ Ｈｕａｋａｎｇ Ｐｈａｒｍａｃｅｕｔｉｃａｌ Ｃｏ．， Ｌｔｄ． | Systems and methods for continuously hydrolyzing hemicellulose to prepare a xylose solution |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1654682A (en) * | 2005-01-21 | 2005-08-17 | 华南理工大学 | Sugar production process using boiler flue gas as clarificant |
| CN101457261A (en) * | 2008-12-26 | 2009-06-17 | 营口北方糖业有限公司 | Tail gas recovery and reuse device and process of sugar production carbonating tank by carbonic acid method |
| CN101538620A (en) * | 2009-04-30 | 2009-09-23 | 广西大学 | Improved process for clarifying sugar juice by carbonation method |
| CN103007727A (en) * | 2012-11-15 | 2013-04-03 | 广西南宁华鑫糖业技术有限责任公司 | Method for absorbing and activating carbon dioxide in boiler flue gas and application of method |
| CN103773902A (en) * | 2014-01-15 | 2014-05-07 | 广西大新县雷平永鑫糖业有限公司 | Filtered juice clarification method by saturated filling of flue gas |
-
2014
- 2014-12-16 CN CN201410774822.5A patent/CN104437060A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1654682A (en) * | 2005-01-21 | 2005-08-17 | 华南理工大学 | Sugar production process using boiler flue gas as clarificant |
| CN101457261A (en) * | 2008-12-26 | 2009-06-17 | 营口北方糖业有限公司 | Tail gas recovery and reuse device and process of sugar production carbonating tank by carbonic acid method |
| CN101538620A (en) * | 2009-04-30 | 2009-09-23 | 广西大学 | Improved process for clarifying sugar juice by carbonation method |
| CN103007727A (en) * | 2012-11-15 | 2013-04-03 | 广西南宁华鑫糖业技术有限责任公司 | Method for absorbing and activating carbon dioxide in boiler flue gas and application of method |
| CN103773902A (en) * | 2014-01-15 | 2014-05-07 | 广西大新县雷平永鑫糖业有限公司 | Filtered juice clarification method by saturated filling of flue gas |
Non-Patent Citations (1)
| Title |
|---|
| 何华柱等: ""烟道气CO2饱充，蔗汁渣沫分离"技术在亚硫酸法糖厂澄清工艺的应用与探讨", 《广西蔗糖》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107010739A (en) * | 2017-05-10 | 2017-08-04 | 烟台大学 | A kind of calcium hardness reduction method of nonferrous metallurgy acid waste water recycle-water |
| JP2021512640A (en) * | 2018-12-04 | 2021-05-20 | 浙江▲華▼康葯▲業▼股▲フン▼有限公司Ｚｈｅｊｉａｎｇ Ｈｕａｋａｎｇ Ｐｈａｒｍａｃｅｕｔｉｃａｌ Ｃｏ．， Ｌｔｄ． | Systems and methods for continuously hydrolyzing hemicellulose to prepare a xylose solution |
| WO2020125459A1 (en) * | 2018-12-18 | 2020-06-25 | 浙江华康药业股份有限公司 | Xylose mother liquor continuous carbonation and impurity-removal device and method therefor |
| JP2021512639A (en) * | 2018-12-18 | 2021-05-20 | 浙江▲華▼康葯▲業▼股▲フン▼有限公司Ｚｈｅｊｉａｎｇ Ｈｕａｋａｎｇ Ｐｈａｒｍａｃｅｕｔｉｃａｌ Ｃｏ．， Ｌｔｄ． | Equipment and methods for continuously saturate-filling xylose mother liquor to remove impurities |
| US11795517B2 (en) | 2018-12-18 | 2023-10-24 | Zhejiang Huakang Pharmaceutical Co., Ltd. | Device and method for performing continuous carbonation and impurity removal for xylose mother liquor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102114383B (en) | Ammonia-chemical-chain-cycle-based carbon dioxide capture and conversion method | |
| CN103007727B (en) | Method for absorbing and activating carbon dioxide in boiler flue gas and application of method | |
| CN104437061A (en) | Method and equipment for activating calcium carbonate from sugar refinery | |
| CN103007721B (en) | Ammonia circulation-based method and device for carbonating fixation of CO2 in coal-fired flue gas | |
| CN103990370B (en) | Thermal power generation flue gas CO 2reduce discharging by-product superfine nano CaCO 3method | |
| CN104437060A (en) | Method and equipment for recovering, activating and utilizing carbon dioxide from sugar refinery | |
| CN109095578A (en) | A kind of method of oxalate precipitation method recycling power plant desulfurization wastewater calcium and magnesium | |
| CN108821308B (en) | Method and device for preparing high-concentration ammonia water by using coking residual ammonia water | |
| CN104803425B (en) | Method for removing hydrogen sulfide from high-sulfur oilfield produced water | |
| CN101805804A (en) | Method for preparing CO2-N2 mixed gas from boiler flue gas to be used for clarification process of sugar production | |
| CN102275955B (en) | Method for preparing mirabilite by using sulfonated end gas absorption solution, and apparatus thereof | |
| CN204320082U (en) | Sugar refinery calcium carbonate activation equipment | |
| CN102225312A (en) | Process for enhancing dual alkali desulfurization | |
| CN104353337B (en) | A kind of ammonia-contaminated gas recovery and processing system and processing method thereof | |
| CN111760457A (en) | Method and equipment for regenerating waste salt generated in flue gas desulfurization | |
| CN204320081U (en) | Sugar refinery carbon dioxide recovery activation utilization device | |
| CN104511228B (en) | A kind of process system of flue gas combined desulfurization decarburization and method | |
| CN107930399A (en) | The removal methods of foreign ion in a kind of organic amine desulfuration solution | |
| CN104016382B (en) | Flue gas is carried out the method that desulfurization produces sodium sulfite by a kind of Dual alkali | |
| CN103638808B (en) | Utilize the method that carbonic anhydrase catalysis lime cream is enriched with sugar refinery carbon dioxide in flue gas | |
| CN216550293U (en) | Vertical square furnace coal gas heat carrier pyrolysis system | |
| CN212492410U (en) | Flue gas desulfurization waste salt regeneration equipment | |
| CN209974511U (en) | Desulfurization water zero release comprehensive utilization device | |
| CN104962322B (en) | Coke oven gas purification system | |
| CN205115045U (en) | Improve ore deposit or smelt device of sour low temperature heat recovery of flue gas sulfur production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150325 |