CN103566746A - External efficient oxidation ammonia desulphurization process and device - Google Patents
External efficient oxidation ammonia desulphurization process and device Download PDFInfo
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Abstract
The invention relates to an external efficient oxidation ammonia desulphurization process and device, in particular to a smoke ammonia desulphurization technique, and belongs to the technical field of electric power, metallurgy, environmental protection and chemical engineering. A desulphurizing tower comprises a crystalizing section, a particulate matter washing and absorbing section, a desulphurizing and ammonia washing section and a demisting section sequentially from bottom to top. The smoke from a boiler dust catcher enters from the crystalizing section at the lower section of the desulphurizing tower, then flows reversely upwards through the particulate matter washing and absorbing section, the desulphurizing and ammonia washing section and the demisting section to remove the dust, sulfur dioxide and part of oxides of nitrogen in the smoke, is subjected to the particulate matter washing operation, the ammonia washing operation and the demisting operation, and then gets out of the desulphurizing tower to be discharged. The operations of crystallization, de-dusting, desulphurization, washing and demisting are all carried out in the same desulphurizing tower, but the ammonium sulfite is oxidized in an external oxidation box, and the very low concentration of ammonium sulfate and an excellent air distribution pipe network are adopted, so that the oxidation efficiency is as high as 2-3 times that of common oxidation, and the problem of difficulty in oxidation in ammonia desulphurization is successfully solved.
Description
Technical field
The present invention relates to a kind of ammonia desulfurizing process and device that adopts external potent oxidation technology, relate in particular to flue gas ammonia method desulfurizing technology, belong to electric power, metallurgy, environmental protection and chemical technology field.
Background technology
The ammonia-process desulfurization technique that utilizes ammonia to remove sulfide in flue gas as raw material has been widely used in the flue gas desulfurization project of electric power, metallurgy and chemical field.
At present, ammonia-process desulfurization technique has the multiple technologies such as single tower, double tower, multitower, wherein double tower ammonia-process desulfurization technique is applied in practical sulphur removal project the earliest, the feature of this technology is that desulfurization, crystallization are carried out respectively in two towers, the flue gas that boiler comes is introduced into a crystallizing tower above, then enters desulfuration absorbing tower below.In crystallizing tower, spray into ammonium sulfate slurries and contact with flue gas downstream (or adverse current), wherein ammonium sulfate slurries are supersaturated ammonium sulfate slurries, and the effect of this tower is mainly crystallization, substantially there is no desulfurizing function; And spray into solution in absorption tower, contact with flue gas adverse current, solution is unsaturated ammonium sulfate, and this tower is substantial desulfurizing tower, and desulfurization performance is high, and in this tower stock tank, be provided with oxidative system is ammonium sulfate by sulfite oxidation simultaneously.The advantage of double tower technology is that two towers are born respectively different effects, and obviously, easily long period operates in the division of labor.And absorption tower is below owing to adopting unsaturated ammonium sulfate as absorbent, desulfuration efficiency is high; Shortcoming be flow process compared with complicated, floor space large, cost is also higher.
In the process of ammonia process technology development, double tower technology also derives multitower technology, and its Typical Representative is that the absorption tower in double tower technology is further divided into again to absorption tower and oxidizing tower.In view of the quantity of tower in this technology is too many, it is excessive to take up an area, conventionally 3 towers are stacked up and down, topmost is absorption tower, and middle part is crystallizing tower, and bottom is oxidizing tower.Such layout has solved this technology and has taken up an area excessive shortcoming, but also causes flow process complicated simultaneously, easily stops up, and device is difficult to long-term operation.
And traditional single tower technology is that desulfurization, oxidation and crystallization are all arranged in same seat tower, flue gas enters from desulfurizing tower middle part, and upwards adverse current is by spraying layer and demister successively, and desulfurizing tower bottom is crystallization, oxidation stock tank.The advantage of this technology be structure and flow process simple, take up an area little, cost is low, shortcoming is because desulfurization, oxidation and crystallization are all in a tower, causing absorbent is supersaturation slurries, causes desulfuration efficiency to decrease, and the solid particle in slurries is easily carried and enters in atmosphere by flue gas.Meanwhile, because the ammonium sulfate content of oxidation slurries is high, oxidation efficiency is low, and oxidation prizes pool volume is large, and oxidation air consumption is large, and energy consumption is also high.
Summary of the invention
The technical problem to be solved in the present invention is:
1) to carry ammonium sulfate too much for traditional ammonia process desulfuration tower ubiquity discharge flue gas, causes the problem of secondary pollution; Some desulfurizing tower has adopted filling system, has improved the too much problem of ammonium sulfate of carrying, but because filler is often by obstructions such as flue dust, crystalline sulfuric acid ammoniums, causes the regular unplanned shutdown of desulfurizer.
2) in ammonia desulfurizing process, the oxidation of ammonium sulfite is more difficult, especially the oxidation of high concentration, saturated or supersaturated ammonium sulfate solution (or slurries) difficulty especially.If ammonium sulfite can not be by good oxidation, will cause in absorption liquid ammonium sulfite content too much, absorption efficiency can decline to a great extent on the one hand, also can make on the other hand the crystallization difficulty of ammonium sulfate, and these two aspects all make the operation of desulfurizing tower sharply worsen, discharge flue gas carries the too much problem phenomenon of ammonium sulfate also can be very serious.
For solving the problems of the technologies described above, the technical solution used in the present invention is:
A potent oxidation ammonia desulfurizing process, desulfurizing tower is followed successively by from bottom to top: ammonia section, demist section are washed in crystallized region, particle washing absorption section, desulfurization; Flue gas is entered by desulfurizing tower bottom gas approach, then adverse current successively makes progress, after crystallization, particle washing, ammonia stripping, removal droplet, remove flue dust, sulfur dioxide and part nitrogen oxide in flue gas, and leave desulfurizing tower and form clean flue gas from top discharge; It is characterized in that:
The shared liquid header of ammonia section is washed in the pars infrasegmentalis setting of particle washing absorption and desulfurization, and liquid header is communicated with the outer external oxidation case arranging of desulfurizing tower; In external oxidation case, along casing cross section, oxidation air distribution pipe network is set, oxidation air distribution pipe network is communicated with external oxidation air intlet; External oxidation case is also communicated with outside ammoniacal liquor or ammonia import; Oxidation air distributor pipe side's off the net external oxidation case bottom, arranges respectively two path ，Yi roads and is communicated with the liquid distribution trough of particle washing absorption section through cleaning circulation pump, and the liquid distribution trough that ammonia section is washed through filler circulating pump and desulfurization in another road is communicated with;
Ammonium sulfite, the gravity flow after liquid header is collected of ammonium sulfate mixed solution that ammonia section and the generation of particle washing absorption section are washed in desulfurization enter external oxidation case, by oxidation air distribution pipe network, oxidation air being evenly distributed in external oxidation case slurries, is ammonium sulfate by the sulfurous acid ammoxidation in these slurries; In external oxidation case, pass into ammoniacal liquor or ammonia and control the pH value of slurries simultaneously; After peroxidating forms unsaturated ammonium sulfate from the circulation of two paths to desulfurization being washed to ammonia section and particle washing absorption section is carried out circulated sprinkling, the solubility of described unsaturated ammonium sulfate is 10～25%.
By technique scheme, particle washing absorption section adopts hollow-spraying-tower; The liquid distribution trough below that ammonia section is washed in desulfurization arranges one section or several sections of packing layers and removes sulfur dioxide.
By technique scheme, crystallized region bottom arranges crystallisation cycle pump with stock tank corresponding position, bottom, crystallisation cycle pump be communicated with within the scope of crystallized region bottom stock tank and the crystallized region distributor of gas approach top, by crystallized region distributor, crystallized region is carried out to hollow-spraying-tower, spray liquid is supersaturated ammonium sulfate slurry; The content of the solid suspension of crystallized region supersaturated ammonium sulfate slurry is 3～15%; Absorption tower agitator is arranged in the stock tank of bottom, crystallized region bottom, and tower prime cement liquid is stirred, and accelerates oxidation reaction and prevents that ammonium sulfate crystallization is at tower bottom sediments; Meanwhile, bottom stock tank is constantly inputted the oxidation air that sulfite oxidation needs; Stock tank below, bottom arranges product slurry outlet.
By technique scheme, demist section is positioned at the liquid distribution trough top that ammonia section is washed in desulfurization, adopts one deck or which floor chevron mist eliminator; Below chevron mist eliminator, carry additionally distributor pipe or/and set up up mesh mist eliminator, mesh mist eliminator thickness is 100～300mm, and web material is plastics.
The external potent oxidation ammonia desulfuration equipment that adopts above-mentioned technique, comprises a desulfurizing tower, and desulfurizing tower bottom arranges gas approach, and top is clean exhanst gas outlet; Desulfurizing tower is followed successively by from bottom to top: ammonia section, demist section are washed in crystallized region, particle washing absorption section, desulfurization; It is characterized in that: the shared liquid header of ammonia section is washed in the pars infrasegmentalis setting of particle washing absorption and desulfurization, liquid header is communicated with the outer external oxidation case arranging of desulfurizing tower; In external oxidation case, along casing cross section, oxidation air distribution pipe network is set, oxidation air distribution pipe network is communicated with external oxidation air intlet; External oxidation case is also communicated with outside ammoniacal liquor or ammonia import; Oxidation air distributor pipe side's off the net external oxidation case bottom, arranges respectively two path ，Yi roads and is communicated with the liquid distribution trough of particle washing absorption section through cleaning circulation pump, and the liquid distribution trough that ammonia section is washed through filler circulating pump and desulfurization in another road is communicated with.
By technique scheme, in external oxidation case, add and establish pulsed discharge oxidation unit.
By technique scheme, liquid header top is particle washing absorption section liquid distribution trough; The interval, liquid distribution trough below that ammonia section is washed in desulfurization arranges one section or several sections of packing layers, and interval, packing layer below arranges particle washing absorption section liquid distribution trough.
By technique scheme, crystallized region bottom arranges crystallisation cycle pump with stock tank corresponding position, bottom, crystallisation cycle pump be communicated with within the scope of crystallized region bottom stock tank and the crystallized region distributor of gas approach top; Absorption tower agitator is arranged in the stock tank of bottom, crystallized region bottom; Stock tank place, bottom also arranges oxidation air import and product slurry outlet.
By technique scheme, demist section is positioned at the liquid distribution trough top that ammonia section is washed in desulfurization, adopts one deck or which floor chevron mist eliminator.
By technique scheme, below chevron mist eliminator, carry additionally distributor pipe or/and set up up mesh mist eliminator, mesh mist eliminator thickness is 100～300mm, web material is plastics.
With respect to prior art, the present invention has following beneficial effect:
Adopt grading absorption technique, desulfurizing tower is followed successively by from bottom to top: four sections of ammonia section, demist sections etc. are washed in crystallized region, particle washing absorption section, desulfurization, crystallization, dedusting, desulfurization, washing, demist are carried out in same desulfurizing tower, this structure, when guaranteeing desulfuration efficiency, can successfully solve desulfurizing tower obstruction and discharge flue gas and carry ammonium sulfate problem too much.. crystallized region takes full advantage of flue gas heat, makes the continuous crystal growth of desulfurizing byproduct ammonium sulfate, adopts spray washing not only can prevent that crystal from stopping up, and can also wash away a large amount of flue dust simultaneously.The ammonium sulfate solids particle that particle washing absorption section wash crystallization process generates, simultaneously further remove flue dust, guarantee that follow-up packing layer is not stopped up by flue dust and crystal, make the device can long-term operation, and there is certain desulfurizing function, avoided the regular unplanned shutdown of desulfurizer.Ammonia section is washed in desulfurization: adopt one section or several sections of fillers, this section of loop slurry adopts unsaturated ammonium sulfate, and the solubility of ammonium sulfate is 10～25%, and lower ammonium sulfate concentrations and filler design make desulfurization section have high desulfuration efficiency; Also there is the effect that removes remaining ammonium sulfate dust granules thing simultaneously.
In addition, the oxidation of ammonium sulfite is carried out in external oxidation case, owing to having adopted very low ammonium sulfate concentrations (solubility of ammonium sulfate is 10～25%) and good air-distribution pipe network, oxidation efficiency is very high, be conventional 2～3 times of being oxidized, successfully solved the ammonia process of desulfurization and be oxidized difficult problem.
Accompanying drawing explanation:
Fig. 1 is apparatus structure of the present invention and process flow diagram.
Wherein: 1 desulfurizing tower or absorption tower; 2 absorption tower agitators; 3 packing layers; 4 demisters; 5 crystallisation cycle pumps; 6 external oxidation casees; 7 cleaning circulation pump; 8 filler circulating pumps; 9 liquid headers; 10 liquid distribution troughs; 11 oxidation air distribution pipe networks.
As shown in Figure 1, desulfurizing tower of the present invention or absorption tower 1 are followed successively by from bottom to top: 1.4 4 sections of ammonia section 1.3, demist sections are washed in crystallized region 1.1, particle washing absorption section 1.2, desulfurization.De-front flue gas from boiler dust remover enters from the crystallized region 1.1 of desulfurizing tower 1 hypomere, then upwards adverse current is washed ammonia section 1.3, demist section 1.4 by particle washing absorption section 1.2, desulfurization successively, after particle washing, ammonia stripping, removal droplet, remove flue dust, sulfur dioxide and part nitrogen oxide in flue gas, and leave the clean flue gas of desulfurizing tower 1 formation from top discharge.
1) crystallized region 1.1: crystallized region 1.1 bottoms and stock tank corresponding position, bottom arrange crystallisation cycle pump 5, crystallisation cycle pump 5 be communicated with in crystallized region 1.1 scopes bottom stock tank and de-before the crystallized region distributor of gas approach top, by crystallized region distributor, crystallized region 1.1 is carried out to hollow-spraying-tower, spray liquid is supersaturated ammonium sulfate slurry; The content of the solid suspension of supersaturated ammonium sulfate slurry is 3～15%; Absorption tower agitator 2 is arranged in the stock tank of bottom, crystallized region bottom, and tower prime cement liquid is stirred, and accelerates oxidation reaction and prevents that ammonium sulfate crystallization is at tower bottom sediments; Meanwhile, bottom stock tank is constantly inputted the oxidation air that sulfite oxidation needs; Stock tank below, bottom arranges product slurry outlet.This section takes full advantage of de-front flue gas heat, makes the continuous crystal growth of desulfurizing byproduct ammonium sulfate, and a large amount of flue dust is washed and removes from flue gas in this section simultaneously.The crystallized region slurries that the content that desulfurizing tower 1 bottom output products slurries are solid suspension is 3～15%, remove follow-up ammonium sulfate dehydration after-treatment system.
2) particle washing absorption section 1.2: this section is positioned at desulfurizing tower crystallized region top, particle washing absorption section distributor is set on top equally, utilize particle washing absorption section distributor to adopt hollow-spraying-tower, different from crystallized region 1.1 is that spray liquid adopts unsaturated ammonium sulfate, the solubility of this ammonium sulfate is 10～25%, the Main Function of this section is the ammonium sulfate solids particle that wash crystallization process generates, further remove flue dust, this has just guaranteed that follow-up packing layer 3 is not stopped up by flue dust and crystal, makes the device can long-term operation; In this process, the part sulfur dioxide in flue gas and the ammonia react in spray liquid generate ammonium sulfite and are removed simultaneously; Crystallized region distributor top, particle washing absorption section 1.2 bottoms are provided with desulfurization and wash the shared liquid header of ammonia section 1.3 9, and ammonium sulfite, ammonium sulfate mixed solution that ammonia section 1.3 is washed in particle washing absorption section 1.2, desulfurization utilize high potential difference gravity flow to enter external oxidation case 6 after being collected by liquid header 9.Cleaning circulation pump 7 is communicated with external oxidation case 6 with particle washing absorption section distributor, the unsaturated ammonium sulfate that external oxidation case 6 is produced constantly enters particle washing absorption section 1.2 and carries out hollow-spraying-tower.
3) ammonia section 1.3 is washed in desulfurization: be positioned at particle washing absorption section distributor top, adopt one section or several sections of packing layers 3, the top of packing layer 3 arranges liquid distribution trough 10; The material of packing layer 3 is plastics, and packing layer 3 Main Functions are to remove sulfur dioxide, and the part sulfur dioxide in flue gas and the ammonia react in spray liquid generate ammonium sulfite and be removed; Also there is the effect that removes remaining ammonium sulfate dust granules thing simultaneously.Filler circulating pump 8 is communicated with external oxidation case 6 with liquid distribution trough 10.This section of circulation fluid, for the solubility from external oxidation case 6 is 10～25% unsaturated ammonium sulfates, adopts the dilute ammonium sulfate solution containing ammonia to make desulfurization section have high desulfuration efficiency.
4) demist section 1.4: be positioned at liquid distribution trough 10 tops, adopt one deck or which floor chevron mist eliminator 4.For further increasing except fog effect, also can below chevron mist eliminator 4, carry additionally distributor pipe or/and set up up mesh mist eliminator, mesh mist eliminator thickness is 100～300mm, web material is plastics.
Through the clean flue gas of above-mentioned 4 sections of processing, at desulfurization tower top discharge.
5) external oxidation case 6: be outside equipped with external oxidation case 6 at desulfurizing tower 1, ammonium sulfite, the gravity flow after liquid header 9 is collected of ammonium sulfate mixed solution that ammonia section 1.3 and 1.2 generations of particle washing absorption section are washed in desulfurization enter external oxidation case 6, and the solubility of this ammonium sulfate is 10～25%; In external oxidation case 6, be provided with oxidation air distribution pipe network 11, oxidation air distribution pipe network 11 is communicated with external oxidation air intlet; By oxidation air distribution pipe network 11, oxidation air being evenly distributed in slurries, is ammonium sulfate by the sulfurous acid ammoxidation in these slurries; In external oxidation case 6, pass into ammoniacal liquor or ammonia and control the pH value of slurries simultaneously.Owing to having adopted very low ammonium sulfate concentrations (10～25%) and good air-distribution pipe network 11, oxidation efficiency is very high, is 2～3 times of conventional oxidation, has successfully solved the ammonia process of desulfurization and has been oxidized difficult problem.Cleaning circulation pump 7 is communicated with the particle washing absorption section 1.2 of external oxidation casees 6 and desulfurizing tower 1, will in external oxidation case 6, containing the unsaturated ammonium sulfate of ammonia, return and be sent to 1.2 pairs of flue gases of particle washing absorption section and process; Filler circulating pump 8 is communicated with external oxidation case 6 and desulfurizing towers 1, will in external oxidation case 6, containing the circulation fluid of ammonia, return and be sent to desulfurization and wash ammonia section 1.3.
The present invention also comprise with oxidation air blower fan corresponding to external oxidation case 6 etc.For further increasing oxidation effectiveness, also can set up pulsed discharge oxidation unit in the interior apolegamy of external oxidation case 6.
Claims (10)
1. an external potent oxidation ammonia desulfurizing process, desulfurizing tower is followed successively by from bottom to top: ammonia section, demist section are washed in crystallized region, particle washing absorption section, desulfurization; Flue gas is entered by desulfurizing tower bottom gas approach, then adverse current successively makes progress, after crystallization, particle washing, ammonia stripping, removal droplet, remove flue dust, sulfur dioxide and part nitrogen oxide in flue gas, and leave desulfurizing tower and form clean flue gas from top discharge; It is characterized in that:
The shared liquid header of ammonia section is washed in the pars infrasegmentalis setting of particle washing absorption and desulfurization, and liquid header is communicated with the outer external oxidation case arranging of desulfurizing tower; In external oxidation case, along casing cross section, oxidation air distribution pipe network is set, oxidation air distribution pipe network is communicated with external oxidation air intlet; External oxidation case is also communicated with outside ammoniacal liquor or ammonia import; Oxidation air distributor pipe side's off the net external oxidation case bottom, arranges respectively two path ，Yi roads and is communicated with the liquid distribution trough of particle washing absorption section through cleaning circulation pump, and the liquid distribution trough that ammonia section is washed through filler circulating pump and desulfurization in another road is communicated with;
Ammonium sulfite, the gravity flow after liquid header is collected of ammonium sulfate mixed solution that ammonia section and the generation of particle washing absorption section are washed in desulfurization enter external oxidation case, by oxidation air distribution pipe network, oxidation air being evenly distributed in external oxidation case slurries, is ammonium sulfate by the sulfurous acid ammoxidation in these slurries; In external oxidation case, pass into ammoniacal liquor or ammonia and control the pH value of slurries simultaneously; After peroxidating forms unsaturated ammonium sulfate from the circulation of two paths to desulfurization being washed to ammonia section and particle washing absorption section is carried out circulated sprinkling, the solubility of described unsaturated ammonium sulfate is 10～25%.
2. external potent oxidation ammonia desulfurizing process according to claim 1, is characterized in that: particle washing absorption section adopts hollow-spraying-tower; The liquid distribution trough below that ammonia section is washed in desulfurization arranges one section or several sections of packing layers and removes sulfur dioxide.
3. external potent oxidation ammonia desulfurizing process according to claim 1 and 2, it is characterized in that: crystallized region bottom arranges crystallisation cycle pump with stock tank corresponding position, bottom, crystallisation cycle pump be communicated with within the scope of crystallized region bottom stock tank and the crystallized region distributor of gas approach top, by crystallized region distributor, crystallized region is carried out to hollow-spraying-tower, spray liquid is supersaturated ammonium sulfate slurry; The content of the solid suspension of crystallized region supersaturated ammonium sulfate slurry is 3～15%; Absorption tower agitator is arranged in the stock tank of bottom, crystallized region bottom, and tower prime cement liquid is stirred, and accelerates oxidation reaction and prevents that ammonium sulfate crystallization is at tower bottom sediments; Meanwhile, bottom stock tank is constantly inputted the oxidation air that sulfite oxidation needs; Stock tank below, bottom arranges product slurry outlet.
4. external potent oxidation ammonia desulfurizing process according to claim 3, is characterized in that: demist section is positioned at the liquid distribution trough top that ammonia section is washed in desulfurization, adopts one deck or which floor chevron mist eliminator; Below chevron mist eliminator, carry additionally distributor pipe or/and set up up mesh mist eliminator, mesh mist eliminator thickness is 100～300mm, and web material is plastics.
5. adopt the external potent oxidation ammonia desulfuration equipment of one of the claims described technique, comprise a desulfurizing tower, desulfurizing tower bottom arranges gas approach, and top is clean exhanst gas outlet; Desulfurizing tower is followed successively by from bottom to top: ammonia section, demist section are washed in crystallized region, particle washing absorption section, desulfurization; It is characterized in that: the shared liquid header of ammonia section is washed in the pars infrasegmentalis setting of particle washing absorption and desulfurization, liquid header is communicated with the outer external oxidation case arranging of desulfurizing tower; In external oxidation case, along casing cross section, oxidation air distribution pipe network is set, oxidation air distribution pipe network is communicated with external oxidation air intlet; External oxidation case is also communicated with outside ammoniacal liquor or ammonia import; Oxidation air distributor pipe side's off the net external oxidation case bottom, arranges respectively two path ，Yi roads and is communicated with the liquid distribution trough of particle washing absorption section through cleaning circulation pump, and the liquid distribution trough that ammonia section is washed through filler circulating pump and desulfurization in another road is communicated with.
6. external potent oxidation ammonia desulfurizing process according to claim 5, is characterized in that: in external oxidation case, add and establish pulsed discharge oxidation unit.
7. according to the external potent oxidation ammonia desulfurizing process described in claim 5 or 6, it is characterized in that: liquid header top is particle washing absorption section liquid distribution trough; The interval, liquid distribution trough below that ammonia section is washed in desulfurization arranges one section or several sections of packing layers, and interval, packing layer below arranges particle washing absorption section liquid distribution trough.
8. external potent oxidation ammonia desulfurizing process according to claim 7, it is characterized in that: crystallized region bottom arranges crystallisation cycle pump with stock tank corresponding position, bottom, crystallisation cycle pump be communicated with within the scope of crystallized region bottom stock tank and the crystallized region distributor of gas approach top; Absorption tower agitator is arranged in the stock tank of bottom, crystallized region bottom; Stock tank place, bottom also arranges oxidation air import and product slurry outlet.
9. according to the external potent oxidation ammonia desulfurizing process described in claim 5 or 6 or 8, it is characterized in that: demist section is positioned at the liquid distribution trough top that ammonia section is washed in desulfurization, adopts one deck or which floor chevron mist eliminator.
10. external potent oxidation ammonia desulfurizing process according to claim 9, is characterized in that: below chevron mist eliminator, carry additionally distributor pipe or/and set up up mesh mist eliminator, mesh mist eliminator thickness is 100～300mm, and web material is plastics.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104353344A (en) * | 2014-11-05 | 2015-02-18 | 朱忠良 | Method for removing sulfide from steel gas |
| CN104492243A (en) * | 2015-01-08 | 2015-04-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Flue gas desulphurization system and flue gas desulphurization process |
| CN105013313A (en) * | 2015-08-03 | 2015-11-04 | 中石化南京工程有限公司 | Flue gas desulfurization device based on ammonia-ammonium sulfate method |
| CN105056669A (en) * | 2015-09-14 | 2015-11-18 | 叶宏 | Water curtain type special dust remover for biomass |
| CN106621768A (en) * | 2016-12-20 | 2017-05-10 | 亚太环保股份有限公司 | Ammonia process of desulfurization integral purification device and method for acid gas sulfur recovery tail gas |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6063352A (en) * | 1997-07-19 | 2000-05-16 | Lurgi Lentjes Bischoff Gmbh | Method of removing sulfur dioxide from flue gases, especially power plant flue gases and flue gases from garbage incinerator plants |
| CN201669054U (en) * | 2010-05-17 | 2010-12-15 | 上海申川环保科技有限公司 | Flue-gas desulphurization device with external oxidation pool |
| CN102698584A (en) * | 2012-06-29 | 2012-10-03 | 武汉凯迪电力环保有限公司 | Sectional absorption ammonia desulfurization process and device |
-
2013
- 2013-11-26 CN CN201310606822.XA patent/CN103566746A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6063352A (en) * | 1997-07-19 | 2000-05-16 | Lurgi Lentjes Bischoff Gmbh | Method of removing sulfur dioxide from flue gases, especially power plant flue gases and flue gases from garbage incinerator plants |
| CN201669054U (en) * | 2010-05-17 | 2010-12-15 | 上海申川环保科技有限公司 | Flue-gas desulphurization device with external oxidation pool |
| CN102698584A (en) * | 2012-06-29 | 2012-10-03 | 武汉凯迪电力环保有限公司 | Sectional absorption ammonia desulfurization process and device |
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|---|---|---|---|---|
| CN104353344A (en) * | 2014-11-05 | 2015-02-18 | 朱忠良 | Method for removing sulfide from steel gas |
| CN104353344B (en) * | 2014-11-05 | 2016-08-24 | 朱忠良 | The method removing iron and steel sulfide in flue gas |
| CN104492243A (en) * | 2015-01-08 | 2015-04-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Flue gas desulphurization system and flue gas desulphurization process |
| CN105013313B (en) * | 2015-08-03 | 2017-03-08 | 中石化南京工程有限公司 | A kind of ammoniacal ammonium sulphate method flue gas desulfurization device |
| CN105013313A (en) * | 2015-08-03 | 2015-11-04 | 中石化南京工程有限公司 | Flue gas desulfurization device based on ammonia-ammonium sulfate method |
| CN105056669A (en) * | 2015-09-14 | 2015-11-18 | 叶宏 | Water curtain type special dust remover for biomass |
| CN105056669B (en) * | 2015-09-14 | 2017-01-25 | 叶宏 | Water curtain type special dust remover for biomass |
| CN106621768A (en) * | 2016-12-20 | 2017-05-10 | 亚太环保股份有限公司 | Ammonia process of desulfurization integral purification device and method for acid gas sulfur recovery tail gas |
| CN109173680A (en) * | 2018-11-14 | 2019-01-11 | 冷应杰 | A kind of high efficiency industrial fumes energy-saving and purifying technique |
| CN109173680B (en) * | 2018-11-14 | 2021-04-13 | 加中联合(北京)环境科技有限公司 | High-efficiency energy-saving industrial smoke purifying process |
| CN109432995A (en) * | 2018-12-14 | 2019-03-08 | 四川金象赛瑞化工股份有限公司 | The processing method and processing unit of chemical industry tail gas |
| CN110523261A (en) * | 2019-09-29 | 2019-12-03 | 中冶沈勘秦皇岛工程设计研究总院有限公司 | Flue gas desulphurization system |
| CN110523261B (en) * | 2019-09-29 | 2024-07-05 | 中冶沈勘秦皇岛工程设计研究总院有限公司 | Flue gas desulfurization system |
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Application publication date: 20140212 |