准格尔矸石电厂CFB灰中提取冶金级氧化铝工艺研究
摘要
准能矸石电厂流化床灰是新型的固体废弃物,与传统的煤粉炉粉煤灰相比其在化学成分上矸石电厂流化床灰具有相对较高的CaO、SO_3含量;物相组成上流化床灰主要为非晶态,结晶物质相对较少;颗粒形态均为不规则状其颗粒粒度也明显小于煤粉炉粉煤灰。结合以上特点得出准能矸石电厂流化床灰具有高铝、高镓含量的特征。本论文针对其特点提出了通过酸—碱联合法从流化床粉煤灰中提取冶金级氧化铝的生产工艺。从流化床灰中提取冶金级氧化铝工艺主要分两步,即:(1)酸溶除硅→粗氧化铝,酸主要用盐酸;(2)碱溶除铁→冶金级氧化铝(拜耳法)。酸溶实验主要通过添加激发剂让CFB灰与盐酸在一定条件下充分反应,使灰中的活性氧化铝及铁、钛、锰、镓等金属元素溶于盐酸中。通过连续酸溶、渣液分离洗涤后,将渣液浓缩结晶并煅烧得到粗氧化铝。碱溶实验则是将酸溶实验中得到的粗氧化铝粉末与氢氧化钠碱液按一定比例配比成为浆液。参照拜耳法铝土矿的碱溶出条件,使粗氧化铝中的氧化铝与氢反氧化钠应后生成铝酸钠进入到溶液中,经过滤除去铁、锰、钛、钙等的氧化物。再经过种分、煅烧试验从而最终得到了符合国标一级品至二级品标准的冶金级氧化铝产品。
The burning technique of circulating fluidized bed(CFB)is a new technique, which have the advantages of wide adaptability of fuel,high rate of burning,low quantity of NO_x senting out,wide load adjust.With the developing of electric power,the burning technique of CFB will become the main burning technique.At the same time,it will bring the new solid waste,circulating fluidized bed ash.At present,there are a few of reports about comprehensive utilization of circulating fluidized bed ash,especiallly,there is not high technique or high income research. In this paper,in allusion to the comprehensive utilization of circulating fluidized bed ash,we try to find a route of reasonable utilization
The components,structures and properties of circulating fluidized bed ash have been investigated by XRD,laser granularity apparatus and rapid analysis instrument of silicate.The analysis results show that the CaO,SO_3 and burning loss were large for middle temperature burning and adding of limestone as desulfrize reagentat the time of burning,there were no mullite,and the Al and Si were active. For its characteristics,this paper presents a acid-the base of fly ash from fluidized bed extraction metallurgical grade alumina production processes.
Entire experiment is divided into acid-soluble,concentrated crystallization, calcined,alkali-soluble,and then calcined Seed six parts.①acid-soluble aluminum dissolution rate is an important indicator of part of the experiment,which will affect the final product yield,based on past research findings,impact on the rate of acid-soluble ash CFB the principal factors that have temperature,time and acid than ash.Able to associate CFB power plant ash waste as raw materials in the laboratory within the temperature,time and the acid ash than the rate of alumina dissolution test.The results showed that in the CFB gray aluminum dissolution rates increased with temperature increases.However,as the use of laboratory containers for the general dissolution of the glass bottles,not under pressure,and high temperature would lead to serious hydrochloride volatile,so small experimental test the response of the temperature controlled at 95℃within.CFB time on the acid-soluble aluminum gray in the dissolution rate of the acid-soluble time with the increase in dissolution rate also increased in the more than two hours after the time the increase of acid-soluble dissolution rate change has slowed down, and considering the cost factor,the reaction in time to control within two hours. CFB acid gray ash than in the aluminum dissolution rates of the fundamental changes little.This is due to CFB alumina contained in the ash different degrees of activity,increased activity in the good part of the acid dissolution can be sustained, even if the activity of the alumina increased less acid,we can not fully respond. Therefore acid ash than in the control 2.3 can be.CFB ash on the dissolution of the test were to be quasi-rock,ash in the CFB 850℃,950℃,1050℃,1150℃and 1250℃under the roasting conditions,the acid-soluble calcined samples.Grey fixed ratio 2:1 acid,acid temperature 95℃,acid 2 hours.Based on the reaction of alumina content and different temperature roasting CFB XRD patterns of gray,IR spectrum analysis in the acid-soluble ash obtained CFB demonstrated in the course of the activity and its high alumina calcination temperature,850℃Forging burning conditions can be higher dissolution rate of aluminum,more than 850℃aluminum activity will be reduced,when the temperature reached 12.5℃,the Central Plains CFB ash some quality kaolin meet changing nature of the stability of mullite,Al-O bond and the Al-O-Si bond activity will be reduced,leading to the dissolution aluminum.②some of the major concentration is the crystallization of continuous acid-soluble liquid residue after separation after the chloride concentration Qingshi into the tank enrichment crystallization.Concentrator for the enamel pot,ohmic heating.In order to speed up the pace of concentration crystallization using vacuum concentration.Add the condensed liquor buffer cooling tanks,with the temperature drop,crystal aluminum chloride crystal from the beginning,can be filtered crystalline aluminum chloride.Concentrated crystallization conditions:temperature 85 to concentrate 110℃,the vacuum suction 0～-0.06 MPa.③crystalline aluminum chloride burning part of its focus is to determine the complete decomposition of the calcination temperature and the decomposition of hydrogen chloride gas recovery and utilization.Through the examination of crystalline aluminum chloride samples TG-DTA curves of aluminum chloride that crystallization temperature increases gradually with the loss of water,all of the final decomposition of hydrogen chloride gas and produce alumina.In order to determine the crystalline aluminum chloride complete decomposition temperature,we had a different temperature burning test, calcination time for two hours.By analyzing different calcination temperature map of the X-ray crystal aluminum chloride in the calcination temperature of 360 to 600℃,calcination time in a static state for 2 h.④alkali dissolution experiments through from Bayer alkali concentration on the basis of our study focused on the temperature on the rough dissolution rate of alumina,the temperature accordingly alkali-soluble At the same time,the composition of the red mud has done and Phase a focus on.Bayer reference to the dissolution of bauxite alkali conditions, only rough conditions for the dissolution of alumina alkali lye Na2O content concentration of 165g/L,the amount of alumina rough 170g/L,molecular ratio of 1.6,dissolution temperature 210～240℃,the dissolution time is 2 h.Based on the chemical composition of red mud and spirits of alumina in the rough that the process of alkali-soluble Fe2O3 as insoluble exist in red mud,and CaO in the process of alkali-soluble and insoluble alumina from a combination of hydrated calcium aluminate.⑤process is the kind of rough-alumina after the reaction of alkali solution of sodium aluminate solution cooling,making it a supersaturated solution,in this over-saturated solution of aluminum hydroxide added to seed, continuous mixing,a decomposition of sodium aluminate,generated aluminum hydroxide precipitation.Through the kind of aluminum hydroxide at the X-ray diffraction pattems and infrared spectra of the crystal analysis of decomposition conditions:Solution for Al2O3 content concentration 170g/L;seed coefficient of 1.5(390g aluminum hydroxide/L)at the beginning of before temperature is 75℃to terminate 35℃;Seed Time:50 h.⑥aluminum hydroxide will be part of calcined alumina in the high temperature hydrogen from water adsorbing water and structure,and make it crystal changes in the system of metallurgical grade alumina process.Seed will be the aluminum hydroxide in 1000℃,1100℃and 1200℃under calcination temperature conditions.Through the different samples calcined under the conditions of temperature X-ray diffraction and infrared spectra of Fig. We can see that the 1200℃calcined alumina for the crystallization of a well-Al2O3.Bayer has been with the alumina production process,we have identified hydrogen alumina calcination temperature for 1200℃,calcined for 2 h, in this temperature will be sub-species of hydrogen to a number of calcined alumina test finally GB with the goods to one of the two standards for metallurgical grade alumina products.
In conclusion,this study analyzed the characteristics of fly ash CFB proposed acid-the base of fly ash from fluidized bed extraction of a metallurgical grade alumina production process.And the process conditions,product performance to a more in-depth study and discussion,as an important way to provide comprehensive utilization of fly ash
The burning technique of circulating fluidized bed(CFB)is a new technique, which have the advantages of wide adaptability of fuel,high rate of burning,low quantity of NO_x senting out,wide load adjust.With the developing of electric power,the burning technique of CFB will become the main burning technique.At the same time,it will bring the new solid waste,circulating fluidized bed ash.At present,there are a few of reports about comprehensive utilization of circulating fluidized bed ash,especiallly,there is not high technique or high income research. In this paper,in allusion to the comprehensive utilization of circulating fluidized bed ash,we try to find a route of reasonable utilization
The components,structures and properties of circulating fluidized bed ash have been investigated by XRD,laser granularity apparatus and rapid analysis instrument of silicate.The analysis results show that the CaO,SO_3 and burning loss were large for middle temperature burning and adding of limestone as desulfrize reagentat the time of burning,there were no mullite,and the Al and Si were active. For its characteristics,this paper presents a acid-the base of fly ash from fluidized bed extraction metallurgical grade alumina production processes.
Entire experiment is divided into acid-soluble,concentrated crystallization, calcined,alkali-soluble,and then calcined Seed six parts.①acid-soluble aluminum dissolution rate is an important indicator of part of the experiment,which will affect the final product yield,based on past research findings,impact on the rate of acid-soluble ash CFB the principal factors that have temperature,time and acid than ash.Able to associate CFB power plant ash waste as raw materials in the laboratory within the temperature,time and the acid ash than the rate of alumina dissolution test.The results showed that in the CFB gray aluminum dissolution rates increased with temperature increases.However,as the use of laboratory containers for the general dissolution of the glass bottles,not under pressure,and high temperature would lead to serious hydrochloride volatile,so small experimental test the response of the temperature controlled at 95℃within.CFB time on the acid-soluble aluminum gray in the dissolution rate of the acid-soluble time with the increase in dissolution rate also increased in the more than two hours after the time the increase of acid-soluble dissolution rate change has slowed down, and considering the cost factor,the reaction in time to control within two hours. CFB acid gray ash than in the aluminum dissolution rates of the fundamental changes little.This is due to CFB alumina contained in the ash different degrees of activity,increased activity in the good part of the acid dissolution can be sustained, even if the activity of the alumina increased less acid,we can not fully respond. Therefore acid ash than in the control 2.3 can be.CFB ash on the dissolution of the test were to be quasi-rock,ash in the CFB 850℃,950℃,1050℃,1150℃and 1250℃under the roasting conditions,the acid-soluble calcined samples.Grey fixed ratio 2:1 acid,acid temperature 95℃,acid 2 hours.Based on the reaction of alumina content and different temperature roasting CFB XRD patterns of gray,IR spectrum analysis in the acid-soluble ash obtained CFB demonstrated in the course of the activity and its high alumina calcination temperature,850℃Forging burning conditions can be higher dissolution rate of aluminum,more than 850℃aluminum activity will be reduced,when the temperature reached 12.5℃,the Central Plains CFB ash some quality kaolin meet changing nature of the stability of mullite,Al-O bond and the Al-O-Si bond activity will be reduced,leading to the dissolution aluminum.②some of the major concentration is the crystallization of continuous acid-soluble liquid residue after separation after the chloride concentration Qingshi into the tank enrichment crystallization.Concentrator for the enamel pot,ohmic heating.In order to speed up the pace of concentration crystallization using vacuum concentration.Add the condensed liquor buffer cooling tanks,with the temperature drop,crystal aluminum chloride crystal from the beginning,can be filtered crystalline aluminum chloride.Concentrated crystallization conditions:temperature 85 to concentrate 110℃,the vacuum suction 0～-0.06 MPa.③crystalline aluminum chloride burning part of its focus is to determine the complete decomposition of the calcination temperature and the decomposition of hydrogen chloride gas recovery and utilization.Through the examination of crystalline aluminum chloride samples TG-DTA curves of aluminum chloride that crystallization temperature increases gradually with the loss of water,all of the final decomposition of hydrogen chloride gas and produce alumina.In order to determine the crystalline aluminum chloride complete decomposition temperature,we had a different temperature burning test, calcination time for two hours.By analyzing different calcination temperature map of the X-ray crystal aluminum chloride in the calcination temperature of 360 to 600℃,calcination time in a static state for 2 h.④alkali dissolution experiments through from Bayer alkali concentration on the basis of our study focused on the temperature on the rough dissolution rate of alumina,the temperature accordingly alkali-soluble At the same time,the composition of the red mud has done and Phase a focus on.Bayer reference to the dissolution of bauxite alkali conditions, only rough conditions for the dissolution of alumina alkali lye Na2O content concentration of 165g/L,the amount of alumina rough 170g/L,molecular ratio of 1.6,dissolution temperature 210～240℃,the dissolution time is 2 h.Based on the chemical composition of red mud and spirits of alumina in the rough that the process of alkali-soluble Fe2O3 as insoluble exist in red mud,and CaO in the process of alkali-soluble and insoluble alumina from a combination of hydrated calcium aluminate.⑤process is the kind of rough-alumina after the reaction of alkali solution of sodium aluminate solution cooling,making it a supersaturated solution,in this over-saturated solution of aluminum hydroxide added to seed, continuous mixing,a decomposition of sodium aluminate,generated aluminum hydroxide precipitation.Through the kind of aluminum hydroxide at the X-ray diffraction pattems and infrared spectra of the crystal analysis of decomposition conditions:Solution for Al2O3 content concentration 170g/L;seed coefficient of 1.5(390g aluminum hydroxide/L)at the beginning of before temperature is 75℃to terminate 35℃;Seed Time:50 h.⑥aluminum hydroxide will be part of calcined alumina in the high temperature hydrogen from water adsorbing water and structure,and make it crystal changes in the system of metallurgical grade alumina process.Seed will be the aluminum hydroxide in 1000℃,1100℃and 1200℃under calcination temperature conditions.Through the different samples calcined under the conditions of temperature X-ray diffraction and infrared spectra of Fig. We can see that the 1200℃calcined alumina for the crystallization of a well-Al2O3.Bayer has been with the alumina production process,we have identified hydrogen alumina calcination temperature for 1200℃,calcined for 2 h, in this temperature will be sub-species of hydrogen to a number of calcined alumina test finally GB with the goods to one of the two standards for metallurgical grade alumina products.
In conclusion,this study analyzed the characteristics of fly ash CFB proposed acid-the base of fly ash from fluidized bed extraction of a metallurgical grade alumina production process.And the process conditions,product performance to a more in-depth study and discussion,as an important way to provide comprehensive utilization of fly ash
引文
[1]边炳鑫,解强,赵由才等,煤系固体废物资源化技术,北京:化学工业出版社,2005.121-125
[2]钱觉时,粉煤灰特性与粉煤灰混凝土,北京:科学出版社,2002.
[3]杨国清,刘康怀,固体废物处理工程,科学出版社,北京:2000,102-110,76-85
[4]曹东,王金南,中国工业污染经济学,北京:中国环境科学出版社,1999.
[5]董金道,国内外粉煤灰综合利用的现状及发展前景,油田节能,2003,14(1):5-10
[6]McCarthy MJ,Dhir PK,Towards maximizing the use of fly ash as a binder in concrete,Cement Concrete Res,1999,78:121-132
[7]Belardi G,Massimila S,Piga L,Crystallization of K-L and K-W zeolites from flyash,Resour Conser Recycl 1998,24:167-181
[8]Miki Inada,Hidenobu Tsujimoto,Yukari Eguchi,et al.Microwave-assisted zeolitesynthesis from coal fly ash in hydrothermal process,Fuel,2005,84:1482-1486
[9]Guo RQ,Rohatgi PK,Opportunities of using fly ash particles for synthesis of composites,Proc Am Power Conf,1997,2:828-833
[10]Saroja Devi M,Murugesan V,Rengarakj K,et al.Utilization of fly ash as filler for unsaturated polyester resin,J Appl Polymer Sci,1998,69:1385-1391
[11]Pickles CA,Mclean A,Alcock CN,et al.Plasma recovery of metal values from fly ash,Can Metal Q,1990,29:193-200
[12]Dasmahaputra GP,Pal TK,Bhattacharya B,Continuous separation of hexavalent chromium in a packed bed of fly ash pellets,Chem Eng Technol,1998,21:89-95
[13]Kuniaki M,Nishikawa K,Ozaki T,et al.Recovery of vanadium,nickel and magnesium from a fly ash of bitumen-in-water emulsion by chlorination and chemical transport,J Alloys Compounds,1998,1-2:156-160
[14]Lin LJ,Malts N,Shinder Y,The complex chemical treatment of alumina-silica containing materials,J Mater Synth Proc,1998,6:27-35
[15]Kalra N,Jain MC,Joshi HC,et al.Fly ash as a soil conditioner and fertilizer,Bioresour Technol,1998,64:163-167
[16]王璐,尹延辉,王斌等,我国粉煤灰综合利用现状、存在问题及其对策,粉煤灰,2004,4:28-31
[17]赵宏,陆胜,解晓斌,用粉煤灰制备高纯超细氧化铝粉的研究,粉煤灰综合利用,2002,6:8-10
[18]Chris C.Y.Chan,Donald W.Kirk,Hilary Marsh,The behavior of Al in MSW incinerator fly ash during thermal treatment,Journal of Hazardous Materials,2000,B76:103-111
[19]陆胜,方荣利,赵红,用石灰烧结自粉化法从粉煤灰中回收高纯超细氧化铝粉的研究,粉煤灰,2003,1:15-17
[20]R.H.Matjie,J.R.Bunt,J.h.P.van Heerdn,Extraction of alumina from coal flyash generated from a selected low rank bituminous South African coal,Minerals Engineering,2005,18:299-310
[21]徐旭常.先进的低污染煤粉燃烧技术[J].煤炭转化,1994,17(3):65-71.
[22]骆仲泱,何宏舟,王勤辉等.循环流化床锅炉技术的现状及发展前景[J].动力工程,2004,24(6):761-767.
[23]岳光溪.循环流化床技术发展与应用[J].节能与环保,2004(1):11-12.
[24]李明富,胡帆.循环流化床锅炉的特点及发展现状[J].环境保护,2001(7):19-20.
[25]RajaramS.Nextgeneration CFBC[J].Chemical Engineering Science,1999(54):5565-5571.
[26]裴亚利,魏存弟,杨殿范等.循环流化床粉煤灰的特征及其综合利用研究[J].粉煤灰综合利用,2006,5:14-16.
[27]李登新,吕俊复,郭庆杰等.循环流化床灰渣利用研究进展[J].热能动力工程,2003,103(18):5-9.
[28]党辉,王洪升,黄红等.循环流化床脱硫灰渣的特性及应用初探[J].国际电力,2004,8(6):55-58.
[29]闫维勇,高廷源,熊仁森.循环流化床锅炉脱硫灰渣综合利用研究[J].洁净煤技术,2000,6(1):31-33.
[30]雒国忠.循环流化床锅炉灰渣物化性能分析[J].电力环境保护,2000,14(7):24-26.
[31]刘德昌.流化床燃烧工业技术应用[M].北京:中国电力出版社,1998,61-64.
[32]田书营.锅炉飞灰回收燃烧实验研究[j].中国能源,1999(5):17-19.
[33]彭涛,田书营,张志宝.内循环流化床锅炉燃烧链条炉飞灰实验研究[j].动力工程,1999(4):250-254.
[34]鲁兴田,冷祯皋.循环流化床锅炉脱硫粉煤灰制砖技术[J].粉煤灰,2005(3):37-38.
[35]岳焕玲,原永涛,朱洪峰.循环流化床锅炉灰渣综合利用[J],锅炉技术,2006,37:36-41.
[36]Thomas Hayden,Alex Kingsbury.Phoenix in the Swamp;Despite the obstacles,there's no shortage of rebuilding plans[J].U.S.News & World Report.Washington:Sep 19,2005.Vol.139,Iss.10;pg.50.
[37]马熹焱,张慧,陈彩云,瞿春艳.脱硫添加剂煅烧特性的试验研究[J].煤炭技术,2007,12期,95-96.
[38]Baoguo Ma,Meng Qi,Jun Peng,et al.The compositions,surface texture,absorption,and binding properties of fly ash in China,Fuel,1999,25:423-432
[39]王祖旭.一水硬铝石拜尔法生产氧化铝脱硅过程[J],铝镁通讯,2006,3期,12-14.
[40]董晓辉,徐宏刚.烧结法氧化铝炉(窑)灰综合利用的研究[J],中国高新技术企业,2007,9期,194-194,196.
[41]艾孟井,程宗浩,张晓风.联合法生产氧化铝的新工艺探讨[J],铝镁通讯,2007,1期,7-9.
[42]杨重愚,氧化铝生产工艺学,北京:冶金工业出版社,1993.
[43]裴亚利,魏存弟,杨殿范等.循环流化床粉煤灰的特征及其综合利用研究[J].粉煤灰综合利用,2006,5:14-16.
[44]王文静,韩作振,程建光,酸法提取粉煤灰中氧化铝的条件选择,能源环 境保护,2003,17(4):17-19
[45]Merem Seferinoglu,Mehtap Paul,Ake Sandstrom,Acid leaching of coal and coal-ashes,Fuel,2003,82 1721-1734
[46]H.C.Park,Y.J.Park,R.Stevens,Synthesis of alumina from high purity alum derived from coal fly ash,Materials Science and Engineering A 2004,367,166-170
[47]杨敦顺.浅谈氯化氢尾气水吸收工艺的改进[J].中国氯碱,1998,4期,15-16
[48]林开建.结晶氯化铝生产的腐蚀特点及主要换热设备的材料选择[J].福建化工,2005,5期,14-16.
[49]沈钧,裘俊红,王定海.高浓氯化氢气体吸收的若干问题探讨[J].浙江化工,2004,5期,17-19.
[50]Kanaka T A,The adiabatic absorption of hydrogen chloride.Transactions of the Institution ofChemical Engineers,1954.32:236-243
[51]杨世杰.苹果铝厂赤泥的物相分析[J].中南工业大学报,1996,27(5):570-572.
[52]徐明瑛.铝土矿的供求现状[J].海运情报,2007,12期,15-16.
[2]钱觉时,粉煤灰特性与粉煤灰混凝土,北京:科学出版社,2002.
[3]杨国清,刘康怀,固体废物处理工程,科学出版社,北京:2000,102-110,76-85
[4]曹东,王金南,中国工业污染经济学,北京:中国环境科学出版社,1999.
[5]董金道,国内外粉煤灰综合利用的现状及发展前景,油田节能,2003,14(1):5-10
[6]McCarthy MJ,Dhir PK,Towards maximizing the use of fly ash as a binder in concrete,Cement Concrete Res,1999,78:121-132
[7]Belardi G,Massimila S,Piga L,Crystallization of K-L and K-W zeolites from flyash,Resour Conser Recycl 1998,24:167-181
[8]Miki Inada,Hidenobu Tsujimoto,Yukari Eguchi,et al.Microwave-assisted zeolitesynthesis from coal fly ash in hydrothermal process,Fuel,2005,84:1482-1486
[9]Guo RQ,Rohatgi PK,Opportunities of using fly ash particles for synthesis of composites,Proc Am Power Conf,1997,2:828-833
[10]Saroja Devi M,Murugesan V,Rengarakj K,et al.Utilization of fly ash as filler for unsaturated polyester resin,J Appl Polymer Sci,1998,69:1385-1391
[11]Pickles CA,Mclean A,Alcock CN,et al.Plasma recovery of metal values from fly ash,Can Metal Q,1990,29:193-200
[12]Dasmahaputra GP,Pal TK,Bhattacharya B,Continuous separation of hexavalent chromium in a packed bed of fly ash pellets,Chem Eng Technol,1998,21:89-95
[13]Kuniaki M,Nishikawa K,Ozaki T,et al.Recovery of vanadium,nickel and magnesium from a fly ash of bitumen-in-water emulsion by chlorination and chemical transport,J Alloys Compounds,1998,1-2:156-160
[14]Lin LJ,Malts N,Shinder Y,The complex chemical treatment of alumina-silica containing materials,J Mater Synth Proc,1998,6:27-35
[15]Kalra N,Jain MC,Joshi HC,et al.Fly ash as a soil conditioner and fertilizer,Bioresour Technol,1998,64:163-167
[16]王璐,尹延辉,王斌等,我国粉煤灰综合利用现状、存在问题及其对策,粉煤灰,2004,4:28-31
[17]赵宏,陆胜,解晓斌,用粉煤灰制备高纯超细氧化铝粉的研究,粉煤灰综合利用,2002,6:8-10
[18]Chris C.Y.Chan,Donald W.Kirk,Hilary Marsh,The behavior of Al in MSW incinerator fly ash during thermal treatment,Journal of Hazardous Materials,2000,B76:103-111
[19]陆胜,方荣利,赵红,用石灰烧结自粉化法从粉煤灰中回收高纯超细氧化铝粉的研究,粉煤灰,2003,1:15-17
[20]R.H.Matjie,J.R.Bunt,J.h.P.van Heerdn,Extraction of alumina from coal flyash generated from a selected low rank bituminous South African coal,Minerals Engineering,2005,18:299-310
[21]徐旭常.先进的低污染煤粉燃烧技术[J].煤炭转化,1994,17(3):65-71.
[22]骆仲泱,何宏舟,王勤辉等.循环流化床锅炉技术的现状及发展前景[J].动力工程,2004,24(6):761-767.
[23]岳光溪.循环流化床技术发展与应用[J].节能与环保,2004(1):11-12.
[24]李明富,胡帆.循环流化床锅炉的特点及发展现状[J].环境保护,2001(7):19-20.
[25]RajaramS.Nextgeneration CFBC[J].Chemical Engineering Science,1999(54):5565-5571.
[26]裴亚利,魏存弟,杨殿范等.循环流化床粉煤灰的特征及其综合利用研究[J].粉煤灰综合利用,2006,5:14-16.
[27]李登新,吕俊复,郭庆杰等.循环流化床灰渣利用研究进展[J].热能动力工程,2003,103(18):5-9.
[28]党辉,王洪升,黄红等.循环流化床脱硫灰渣的特性及应用初探[J].国际电力,2004,8(6):55-58.
[29]闫维勇,高廷源,熊仁森.循环流化床锅炉脱硫灰渣综合利用研究[J].洁净煤技术,2000,6(1):31-33.
[30]雒国忠.循环流化床锅炉灰渣物化性能分析[J].电力环境保护,2000,14(7):24-26.
[31]刘德昌.流化床燃烧工业技术应用[M].北京:中国电力出版社,1998,61-64.
[32]田书营.锅炉飞灰回收燃烧实验研究[j].中国能源,1999(5):17-19.
[33]彭涛,田书营,张志宝.内循环流化床锅炉燃烧链条炉飞灰实验研究[j].动力工程,1999(4):250-254.
[34]鲁兴田,冷祯皋.循环流化床锅炉脱硫粉煤灰制砖技术[J].粉煤灰,2005(3):37-38.
[35]岳焕玲,原永涛,朱洪峰.循环流化床锅炉灰渣综合利用[J],锅炉技术,2006,37:36-41.
[36]Thomas Hayden,Alex Kingsbury.Phoenix in the Swamp;Despite the obstacles,there's no shortage of rebuilding plans[J].U.S.News & World Report.Washington:Sep 19,2005.Vol.139,Iss.10;pg.50.
[37]马熹焱,张慧,陈彩云,瞿春艳.脱硫添加剂煅烧特性的试验研究[J].煤炭技术,2007,12期,95-96.
[38]Baoguo Ma,Meng Qi,Jun Peng,et al.The compositions,surface texture,absorption,and binding properties of fly ash in China,Fuel,1999,25:423-432
[39]王祖旭.一水硬铝石拜尔法生产氧化铝脱硅过程[J],铝镁通讯,2006,3期,12-14.
[40]董晓辉,徐宏刚.烧结法氧化铝炉(窑)灰综合利用的研究[J],中国高新技术企业,2007,9期,194-194,196.
[41]艾孟井,程宗浩,张晓风.联合法生产氧化铝的新工艺探讨[J],铝镁通讯,2007,1期,7-9.
[42]杨重愚,氧化铝生产工艺学,北京:冶金工业出版社,1993.
[43]裴亚利,魏存弟,杨殿范等.循环流化床粉煤灰的特征及其综合利用研究[J].粉煤灰综合利用,2006,5:14-16.
[44]王文静,韩作振,程建光,酸法提取粉煤灰中氧化铝的条件选择,能源环 境保护,2003,17(4):17-19
[45]Merem Seferinoglu,Mehtap Paul,Ake Sandstrom,Acid leaching of coal and coal-ashes,Fuel,2003,82 1721-1734
[46]H.C.Park,Y.J.Park,R.Stevens,Synthesis of alumina from high purity alum derived from coal fly ash,Materials Science and Engineering A 2004,367,166-170
[47]杨敦顺.浅谈氯化氢尾气水吸收工艺的改进[J].中国氯碱,1998,4期,15-16
[48]林开建.结晶氯化铝生产的腐蚀特点及主要换热设备的材料选择[J].福建化工,2005,5期,14-16.
[49]沈钧,裘俊红,王定海.高浓氯化氢气体吸收的若干问题探讨[J].浙江化工,2004,5期,17-19.
[50]Kanaka T A,The adiabatic absorption of hydrogen chloride.Transactions of the Institution ofChemical Engineers,1954.32:236-243
[51]杨世杰.苹果铝厂赤泥的物相分析[J].中南工业大学报,1996,27(5):570-572.
[52]徐明瑛.铝土矿的供求现状[J].海运情报,2007,12期,15-16.