CN210438429U - System for calcium sulfite oxidation modification in semi-dry desulfurization waste ash - Google Patents
System for calcium sulfite oxidation modification in semi-dry desulfurization waste ash Download PDFInfo
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Abstract
The utility model provides a system for calcium sulfite oxidation modification in semidry desulfurization waste ash belongs to environmental engineering technical field. The system comprises a dust remover, a preheating kiln, an oxidation kiln, an external heating furnace and a cooling kiln, wherein the dust remover is arranged at the front end of the preheating kiln, the oxidation kiln is arranged at the rear part of the preheating kiln, the external heating furnace supplies heat for the oxidation kiln, and the cooling kiln is arranged at the rear part of the oxidation kiln. The dust remover comprises a flue gas inlet, a flue gas outlet and an ash discharge port; the preheating kiln comprises a feed inlet, an exhaust port, a discharge port and an air inlet; the oxidation kiln comprises a feed inlet, an exhaust port, an air inlet and a discharge port; the external heating furnace comprises a fuel feeding hole, a combustion-supporting air inlet and a hot flue gas outlet; the cooling kiln comprises a feed inlet, an exhaust port, an air inlet and a discharge port. The system has the advantages of low energy consumption, high oxidation efficiency, large processing capacity and the like, and is suitable for industrial production and application.
Description
Technical Field
The utility model relates to the technical field of environmental engineering, in particular to a system for the oxidation modification of calcium sulfite in semi-dry desulfurization waste ash.
Background
The technologies applied to flue gas desulfurization at home and abroad are mainly divided into wet desulfurization, semi-dry desulfurization and dry desulfurization. Because of the advantages of high desulfurization efficiency of wet desulfurization, mature desulfurization byproduct utilization technology and the like, the application proportion of the wet desulfurization reaches more than 85 percent, but the technology has the problems of gypsum rain, colored smoke plume and the like, along with the continuous improvement of the national environmental protection requirement, various large industrial enterprises gradually tend to adopt a semi-dry flue gas desulfurization technology, the investment and operation cost of the technology is lower than that of the wet desulfurization, and no colored smoke rain exists, so that the application proportion of the wet desulfurization is continuously improved.
With the wide application of the semi-dry desulphurization technology, especially in the steel and electric power industry, a large amount of desulfurized waste ash is generated every year in the production process, and the desulfurized waste ash contains a large amount of calcium sulfite (CaSO)3) The material has poor stability and slow hydration reaction, can not be directly applied to the cement building material industry, and is difficult to carry out resource comprehensive utilization. At present, most of the desulfurization waste ash generated by various large enterprises is in a stockpiling state, occupies a large amount of land, has fine granularity, belongs to alkaline substances, and is very easy to pollute the surrounding environment. Therefore, the key to solve the problem of recycling comprehensive utilization of the desulfurized waste ash lies in how to efficiently and low-consumption convert calcium sulfite in the ash into calcium sulfate (CaSO)4）。
Patent CN 201410380659.4 discloses a dry and semi-dry desulfurization ash two-stage rotary oxygen enrichment plus thermal oxidation process and a device, wherein the heat of air introduced into a kiln comes from the heat exchange of hot flue gas of a heating furnace, the heat exchange efficiency is low, the material preheating effect is poor, and the energy consumption is higher; the kiln head is adopted to feed air, the air and the raw materials flow through the preheating section and the oxidation section in a parallel mode, the effect of preheating the materials is poor, airflow is easy to carry unoxidized particles to the kiln tail, and the unoxidized particles are mixed with finished products, so that the content of finished calcium sulfite is high, and the subsequent building material application is not facilitated; the heat exchange of the finished product by the technology adopts heat pipe indirect heat exchange, the heat exchange efficiency is low, the temperature of the product cannot be effectively reduced, and the subsequent transportation and storage have great problems. The device is influenced by the strength of the rotary drum material, the material processing capacity is limited, and the annual production capacity is only 4 ten thousand tons at most.
ZL201710150077.0 'system and method for treating sintering desulfurization ash', the desulfurization ash is directly added into a slag runner to produce slag, and calcium sulfite in the ash can decompose SO at high temperature2And the atmospheric environment is polluted.
ZL201710123582.6 'a sintering semidry desulfurization ash oxidation modification device and oxidation modification method' and ZL201710123453.7 'a sintering flue gas semidry desulfurization ash acid oxidation modification method', the two methods are feasible in principle, but are not suitable for industrial large-scale production in technology and equipment.
SUMMERY OF THE UTILITY MODEL
The utility model discloses a solve prior art desulfurization waste ash oxidation treatment cost height, produce secondary pollution, oxidation inefficiency scheduling problem, provide the modified system of calcium sulfite oxidation in the semi-dry process desulfurization waste ash for the desulfurization waste ash after the oxidation treatment can be applied to cement, gypsum building materials trade, realizes resourceization, high added value utilization.
The system comprises a dust remover, a preheating kiln, an oxidation kiln, an external heating furnace and a cooling kiln, wherein the dust remover is arranged at the front end of the preheating kiln, the oxidation kiln is arranged at the rear part of the preheating kiln, the external heating furnace supplies heat for the oxidation kiln, and the cooling kiln is arranged at the rear part of the oxidation kiln; wherein, the dust remover includes the flue gas inlet, exhanst gas outlet and ash discharge port, preheat the kiln including preheating the kiln gas vent, preheat the kiln feed inlet, preheat the kiln air inlet and preheat the kiln bin outlet, the oxidation kiln includes oxidation kiln gas vent, oxidation kiln feed inlet, oxidation kiln air inlet and oxidation kiln bin outlet, outer heating furnace includes the nozzle, hot exhanst gas outlet, fuel feed inlet and combustion-supporting wind import, the cooling kiln includes cooling kiln gas vent, cooling kiln feed inlet, cooling kiln air inlet and cooling kiln bin outlet.
The ash discharge port is connected with the preheating kiln feed inlet, the preheating kiln exhaust port is connected with the flue gas inlet, the preheating kiln discharge port is connected with the oxidation kiln feed inlet, the oxidation kiln exhaust port and the hot flue gas outlet are connected with the preheating kiln air inlet, the oxidation kiln discharge port is connected with the cooling kiln feed inlet, and the cooling kiln exhaust port is connected with the oxidation kiln air inlet and the combustion-supporting air inlet.
The outer layers of the preheating kiln and the cooling kiln are steel rollers, heat-insulating materials are built inside the preheating kiln and the cooling kiln, the oxidation kiln is an external heating rotary kiln, and the rollers of the oxidation kiln are made of 310s stainless steel materials.
The cylinders of the preheating kiln, the oxidation kiln and the cooling kiln are internally provided with lifting blades with special structures, the lifting blades are uniformly distributed into a group along the radial direction of the cylinder, a group of lifting blades are arranged at intervals of 20cm along the axial direction of the cylinder, and the rotating angles of the lifting blades sequentially rotate by 10 degrees along the same direction according to the arrangement condition of the upper group of the lifting blades.
The material lifting plate is formed by welding two stainless steel plates which are made of 310s for 90 degrees, the plates fixed with the kiln bodies of the preheating kiln, the oxidation kiln and the cooling kiln are rectangular, the width of the rectangle is 10-20 cm, the length of the rectangle is 20-40 cm, the other plate is a right-angled triangle, the short side of the right-angled triangle is 5-10 cm, and the long side of the right-angled triangle is the same as the length of the rectangular plate.
The burner of the external heating furnace is arranged below the oxidation kiln roller, and the oxidation kiln roller is positioned in the center of the external heating furnace.
The method adopting the system comprises the following steps:
s1: preheating materials: mixing desulfurized waste ash and dust removed ash of a dust remover, feeding the mixed material into a preheating kiln, feeding hot flue gas in an oxidation kiln and hot flue gas in an external heating furnace from the tail of the preheating kiln, carrying out countercurrent heat exchange on the flue gas and the material, feeding the flue gas in the kiln into the dust remover after the heat exchange, and discharging the flue gas after dust removal;
s2: material oxidation: the preheated material in the S1 is sent into an oxidation kiln to react with high-temperature air in the oxidation kiln to finish the oxidation process, the high-temperature air in the oxidation kiln is sent from the tail of the oxidation kiln, a material oxidation heat source is from an external heating furnace, fuel and high-temperature combustion-supporting air are combusted to release heat to supply heat for material oxidation, and hot flue gas generated after combustion is sent into the preheating kiln;
s3: cooling materials: and (4) feeding the oxidized material in the S2 into a cooling kiln, carrying out countercurrent heat exchange with cold air fed in from the tail of the cooling kiln, discharging from a discharge port of the cooling kiln at the tail of the cooling kiln, heating the cold air into high-temperature air by the material, and discharging from an exhaust port of the cooling kiln at the front of the cooling kiln to respectively feed into an external heating furnace and the oxidation kiln.
Wherein the retention time of the material in the S1 in the preheating kiln is 60-90 min, the temperature of hot flue gas in the oxidation kiln is 500-550 ℃, and the temperature of flue gas in the external heating furnace is 650-700 ℃.
And S2, controlling the reaction temperature in the oxidation kiln to be 600-650 ℃, and keeping the material in the oxidation kiln for 15-20 min.
The retention time of the oxidized material in the S3 in the cooling kiln is 60-90 min, the temperature is reduced to be below 200 ℃, and the temperature of the high-temperature air after heat exchange in the cooling kiln is 400-450 ℃.
The utility model discloses an above-mentioned technical scheme's beneficial effect as follows:
in the above scheme, preheating, oxidation and cooling functions are respectively completed by adopting three kilns of a preheating kiln, an oxidation kiln and a cooling kiln, parameters such as different kiln sizes and rotating speeds can be designed according to technological parameters of materials in each kiln, the working efficiency of the external heating oxidation kiln can be effectively improved, and the annual treatment capacity of monomer equipment can be improved to 7-8 ten thousand tons.
The utility model discloses the hot waste gas of make full use of oxidation kiln and the hot flue gas high temperature heat of external heating stove carry out direct countercurrent flow heat exchange preheating kiln and material, and heat exchange efficiency is up to 70%, reduces the energy resource consumption of system. The preheating kiln roller is internally insulated, and the diameter and the length of the roller can be enlarged by equipment according to the material preheating requirement so as to ensure sufficient heat exchange time and treatment capacity and improve the material preheating temperature. Furthermore, the temperature rise time of the materials in the oxidation kiln can be reduced, the rotating speed of the oxidation kiln is improved, and the yield is further improved.
The utility model discloses the oxidation kiln adopts the kiln tail to send into 400~450 ℃ high temperature air, with material countercurrent motion, can reduce kiln tail material temperature, avoids because of the reaction is exothermic, and kiln tail material temperature surpasss 670 ℃ and causes CaSO3Decomposition of SO2The problem is re-released. Adopts an external heating mode to prevent CaSO3Decomposition occurs by direct contact with a high temperature flame.
The utility model discloses material cooling adopts the direct heat transfer mode of gas-solid, and heat exchange efficiency is high, can retrieve the product waste heat, and the reduction system energy consumption is more than 20%. Meanwhile, the material discharge temperature is low, which is beneficial to subsequent transportation and storage.
Drawings
FIG. 1 is a schematic structural diagram of a system for oxidation modification of calcium sulfite in semi-dry desulfurization waste ash according to the present invention;
FIG. 2 is a schematic diagram of the distribution of the material raising plates in the kiln;
fig. 3 is the utility model discloses a lifting blade structural schematic diagram, wherein, (a) is the lifting blade elevation, (b) is the lifting blade right-hand member.
Wherein: 1-a dust remover; 2-preheating a kiln; 3-oxidizing kiln; 4-external heating furnace; 5-cooling the kiln; 101-a flue gas inlet; 102-a flue gas outlet; 103-ash discharge port; 201-preheating a kiln exhaust port; 202-preheating a kiln feed inlet; 203-preheating a kiln air inlet; 204-preheating a kiln discharge port; 301-exhaust port of oxidation kiln; 302-the feed inlet of the oxidation kiln; 303-an air inlet of the oxidation kiln; 304-the discharge outlet of the oxidation kiln; 401-hot flue gas outlet; 402-a fuel feed port; 403-combustion-supporting air inlet; 501-cooling a kiln exhaust port; 502-cooling the kiln inlet; 503-cooling kiln air inlet; 504-Cooling the kiln discharge.
Detailed Description
In order to make the technical problems, technical solutions and advantages to be solved by the present invention clearer, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
The utility model provides a calcium sulfite oxidation modified system in semi-dry desulfurization waste ash.
As shown in figure 1, the system comprises a dust remover 1, a preheating kiln 2, an oxidation kiln 3, an external heating furnace 4 and a cooling kiln 5, wherein the dust remover 1 is arranged at the front end of the preheating kiln 2, the oxidation kiln 3 is arranged at the rear part of the preheating kiln 2, the external heating furnace 4 supplies heat for the oxidation kiln 3, and the cooling kiln 5 is arranged at the rear part of the oxidation kiln 3;
the dust remover 1 comprises a flue gas inlet 101, a flue gas outlet 102 and an ash discharge port 103, and is used for removing dust in flue gas discharged from the preheating kiln 2, and the generated dust and the desulfurization waste ash are mixed and then enter the preheating kiln 2.
Preheating kiln 2 is including preheating kiln gas vent 201, preheating kiln feed inlet 202, preheating kiln air inlet 203 and preheating kiln bin outlet 204, preheats in the kiln 2 material and the mixed flue gas that the kiln tail sent into and carries out gas-solid countercurrent flow, for the heat exchange efficiency who increases the material, the utility model discloses the lifting blade that sets up in the kiln can make the material form even stable material curtain in the kiln, promotes material drying and preheats, and material temperature rises to 350~400 ℃, and dwell time is 60~90min in preheating kiln 2. After heat exchange, the flue gas in the kiln enters a dust remover 1, and the flue gas after dust removal is discharged outside. The temperature of hot flue gas in the oxidation kiln 3 is 500-550 ℃, and the temperature of hot flue gas in the external heating furnace 4 is 650-700 ℃.
The oxidation kiln 3 comprises an oxidation kiln exhaust port 301, an oxidation kiln feed inlet 302, an oxidation kiln air inlet 303 and an oxidation kiln discharge port 304, and the preheated desulfurization waste ash is fed into the oxidation kiln 3 to react with high-temperature air to complete the oxidation process. The reaction temperature in the oxidation kiln 3 is controlled to be 600-650 ℃, and the residence time of the materials in the kiln is 15-20 min.
The external heating furnace 4 comprises a burner, a hot flue gas outlet 401, a fuel feeding hole 402 and a combustion-supporting air inlet 403, and hot flue gas generated by fuel combustion of the external heating furnace enters the preheating kiln 2 to preheat materials. The burner is arranged below the oxidation kiln roller, and the oxidation kiln roller is positioned in the center of the external heating furnace.
The cooling kiln 5 comprises a cooling kiln exhaust port 501, a cooling kiln feed port 502, a cooling kiln air inlet 503 and a cooling kiln discharge port 504, finished product ash with the temperature of 500-550 ℃ after oxidation is sent into the cooling kiln, countercurrent heat exchange is carried out on the finished product ash and cold air sent in from the kiln tail, the product ash stays in the kiln for 60-90 min, the temperature is reduced to below 200 ℃, and the finished product ash is discharged from a discharge end cover at the tail of the cooling kiln. Wherein the temperature of the high-temperature air is 400-450 ℃.
As shown in FIG. 1, an ash discharge port 103 is connected with a preheating kiln feed inlet 202, a preheating kiln exhaust port 201 is connected with a flue gas inlet 101, a preheating kiln exhaust port 204 is connected with an oxidation kiln feed inlet 302, an oxidation kiln exhaust port 301 and a hot flue gas outlet 401 are connected with a preheating kiln air inlet 203, an oxidation kiln exhaust port 304 is connected with a cooling kiln feed inlet 502, and a cooling kiln exhaust port 501 is connected with an oxidation kiln air inlet 303 and a combustion-supporting air inlet 403.
Fig. 2 is the utility model discloses a lifting blade in preheating kiln 2, oxidation kiln 3 and cooling kiln 5 sets up the schematic structure. 12 raising plates are uniformly distributed in the radial direction of the roller to form a group, a group of raising plates are arranged at intervals of 20cm along the axial direction of the roller, and the rotating angle sequentially rotates by 10 degrees along the same direction according to the arrangement condition of the upper group of raising plates. As shown in figure 3, the material raising plate is formed by welding two stainless steel plates made of 310s at 90 degrees, the height of the material raising plate and a kiln body fixing plate is 10-20 cm, and the length of the material raising plate is 20-40 cm. The other side plate is a right triangle, the short side of the other side plate is 5-10 cm, and the length of the long side of the other side plate is consistent with that of the rectangular plate.
The following description is given with reference to specific examples.
Example 1
In this example, the system shown in FIG. 1 was used to oxidize desulfurized fly ash. In this example, desulfurized fly ash, CaSO, was treated339% of CaSO4The content is 15 percent, and the rest is CaCO3、Ca(OH)2。
The specific treatment process is as follows:
preheating: and (3) introducing the desulfurized waste ash into a preheating kiln, introducing 550 ℃ mixed flue gas into the kiln tail to heat the material, and heating the material to 350 ℃ when the material moves to the kiln tail, wherein the residence time in the kiln is 60 min.
And (3) oxidation: heating to 350 deg.C, and introducing the desulfurized waste ash into an oxidation kiln, wherein the reaction temperature in the kiln is 650 deg.C, the oxidation process is completed during the movement toward the tail of the kiln, and the residence time in the kiln is 15 min.
And (3) cooling: and feeding the oxidized finished product ash with the temperature of 550 ℃ into the cooling kiln, performing countercurrent heat exchange with cold air fed from the tail of the kiln, allowing the product ash to stay in the kiln for 60min, reducing the temperature to 200 ℃, and discharging from a discharge end cover at the tail of the cooling kiln. The temperature of the high-temperature air after heat exchange is 400 ℃.
The oxidized product ash is detected by a GB/T5484-3Content of 1.8%, CaSO4The content was 55.3%.
Example 2
In this example, the system shown in FIG. 1 was used to oxidize desulfurized fly ash. In this example, desulfurized fly ash, CaSO, was treated339% of CaSO4The content is 15 percent, and the rest is CaCO3、Ca(OH)2。
The specific treatment process is as follows:
preheating: and (3) introducing the desulfurized waste ash into a preheating kiln, introducing 650 ℃ mixed flue gas into the kiln tail to heat the material, and heating the material to 400 ℃ when the material moves to the kiln tail, wherein the retention time in the kiln is 90 min.
And (3) oxidation: heating to 400 ℃, and feeding the desulfurized waste ash into an oxidation kiln, wherein the reaction temperature in the kiln is 610 ℃, the oxidation process is completed in the process of moving to the tail of the kiln, and the residence time in the kiln is 20 min.
And (3) cooling: and feeding the oxidized finished product ash with the temperature of 520 ℃ into the cooling kiln, performing countercurrent heat exchange with cold air fed from the tail of the kiln, allowing the product ash to stay in the kiln for 90min, reducing the temperature to 150 ℃, and discharging from a discharge end cover at the tail of the cooling kiln. The temperature of the high-temperature air after heat exchange is 410 ℃.
The oxidized product ash is detected by a GB/T5484-3Content of 1.7%, CaSO4The content was 55.6%.
The foregoing is a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the principle of the present invention, and these improvements and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. A system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash is characterized in that: the device comprises a dust remover (1), a preheating kiln (2), an oxidation kiln (3), an external heating furnace (4) and a cooling kiln (5), wherein the dust remover (1) is arranged at the front end of the preheating kiln (2), the oxidation kiln (3) is arranged at the rear part of the preheating kiln (2), the external heating furnace (4) supplies heat for the oxidation kiln (3), and the cooling kiln (5) is arranged at the rear part of the oxidation kiln (3); wherein, dust remover (1) includes flue gas inlet (101), exhanst gas outlet (102) and ash discharge port (103), preheat kiln (2) including preheating kiln gas vent (201), preheat kiln feed inlet (202), preheat kiln air inlet (203) and preheat kiln bin outlet (204), oxidation kiln (3) are including oxidation kiln gas vent (301), oxidation kiln feed inlet (302), oxidation kiln air inlet (303) and oxidation kiln bin outlet (304), outer heating furnace (4) are including the nozzle, hot exhanst gas outlet (401), fuel feed inlet (402) and combustion-supporting wind import (403), cooling kiln (5) are including cooling kiln gas vent (501), cooling kiln feed inlet (502), cooling kiln air inlet (503) and cooling kiln bin outlet (504).
2. The system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash according to claim 1, characterized in that: the connection of ash discharge opening (103) preheats kiln feed inlet (202), preheats kiln gas vent (201) and connects flue gas inlet (101), preheats kiln bin outlet (204) and connects oxidation kiln feed inlet (302), and oxidation kiln gas vent (301) and hot flue gas outlet (401) are connected and are preheated kiln air inlet (203), and cooling kiln feed inlet (502) are connected in oxidation kiln bin outlet (304), and oxidation kiln air inlet (303) and combustion-supporting wind import (403) are connected in cooling kiln gas vent (501).
3. The system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash according to claim 1, characterized in that: the outer layers of the preheating kiln (2) and the cooling kiln (5) are steel rollers, heat-insulating materials are built inside the preheating kiln and the cooling kiln, the oxidation kiln (3) is an external heating rotary kiln, and the rollers of the oxidation kiln (3) are made of 310s stainless steel materials.
4. The system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash according to claim 1, characterized in that: the preheating kiln (2), the oxidation kiln (3) and the cooling kiln (5) are internally provided with lifting plates, 12 lifting plates are uniformly distributed in a group along the radial direction of the roller, a group of lifting plates are arranged at intervals of 20cm along the axial direction of the roller, and the rotating angles of the lifting plates rotate by 10 degrees along the same direction according to the arrangement condition of the lifting plates.
5. The system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash according to claim 4, characterized in that: the material raising plate is formed by welding two stainless steel plates which are made of 310s for 90 degrees, the plates fixed with the kiln bodies of the preheating kiln (2), the oxidation kiln (3) and the cooling kiln (5) are rectangular, the width of each rectangular plate is 10-20 cm, the length of each rectangular plate is 20-40 cm, the other plate is a right-angled triangle, the short side of each right-angled triangle is 5-10 cm, and the long side of each right-angled triangle is as long as the rectangular plate.
6. The system for oxidizing and modifying calcium sulfite in semi-dry desulfurization waste ash according to claim 1, characterized in that: and the burner of the external heating furnace (4) is arranged below the roller of the oxidation kiln (3), and the roller of the oxidation kiln (3) is positioned in the center of the external heating furnace (4).
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110065962A (en) * | 2019-04-16 | 2019-07-30 | 北京北科环境工程有限公司 | A kind of energy-efficient oxidative system of the useless ash of desulfurization and method |
| CN112028102A (en) * | 2020-07-31 | 2020-12-04 | 马鞍山钢铁股份有限公司 | Treatment method and system for efficiently converting calcium sulfite in calcium-based desulfurized fly ash into calcium sulfate |
| CN112939495A (en) * | 2021-02-05 | 2021-06-11 | 北京北科环境工程有限公司 | Production process for processing plastering gypsum by using semidry desulfurization ash |
-
2019
- 2019-04-16 CN CN201920513803.5U patent/CN210438429U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110065962A (en) * | 2019-04-16 | 2019-07-30 | 北京北科环境工程有限公司 | A kind of energy-efficient oxidative system of the useless ash of desulfurization and method |
| CN112028102A (en) * | 2020-07-31 | 2020-12-04 | 马鞍山钢铁股份有限公司 | Treatment method and system for efficiently converting calcium sulfite in calcium-based desulfurized fly ash into calcium sulfate |
| CN112028102B (en) * | 2020-07-31 | 2023-03-03 | 马鞍山钢铁股份有限公司 | Treatment method and system for efficiently converting calcium sulfite in calcium-based desulfurized fly ash into calcium sulfate |
| CN112939495A (en) * | 2021-02-05 | 2021-06-11 | 北京北科环境工程有限公司 | Production process for processing plastering gypsum by using semidry desulfurization ash |
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