CN106810036A - 一种煤泥、污泥干燥提质装置及工艺 - Google Patents
一种煤泥、污泥干燥提质装置及工艺 Download PDFInfo
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- CN106810036A CN106810036A CN201510848437.5A CN201510848437A CN106810036A CN 106810036 A CN106810036 A CN 106810036A CN 201510848437 A CN201510848437 A CN 201510848437A CN 106810036 A CN106810036 A CN 106810036A
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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000003245 coal Substances 0.000 title claims abstract description 53
- 239000010802 sludge Substances 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000000463 material Substances 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 22
- 239000003517 fume Substances 0.000 claims abstract description 17
- 239000002245 particle Substances 0.000 claims abstract description 14
- 239000000428 dust Substances 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/16—Treatment of sludge; Devices therefor by de-watering, drying or thickening using drying or composting beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/001—Runoff or storm water
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
Abstract
一种煤泥、污泥干燥提质装置及工艺,该装置主要包括烟气发生炉、给料机、干燥管、物料打散装置、旋风分离器、细颗粒输送装置、成品输送装置、除尘器、引风机;由烟气发生炉产生的干燥介质与经过给料机给入的待干燥高水分物料分别进入物料打散装置与干燥管中,高水分物料在物料打散装置内打散及初步干燥,在干燥管实现深度干燥及气力分选,其中粒径不超过设计上限要求的颗粒被气流携带进入分离器中,粒径大于设计上限的煤颗粒落入打散装置被再次打散;由分离器收集的成品经输送装置送入煤场或其它地方;由分离器排出的乏气经除尘器处理后通过引风机排入大气;具有干燥效果更好、运行可靠、系统简单、结构紧凑的特点。
Description
一种煤泥、污泥干燥提质装置及工艺
技术领域
[0001] 本发明涉及干燥提质技术领域,具体涉及一种煤泥、污泥千燥提质装置及工艺。
背景技术
[0002] 选煤生产将伴随着大量的原生煤泥和次生煤泥,因水分较高,产品无销路,只能空 地堆放,不仅易造成资源浪费,且易导致环境污染。即使经过压滤机回收以后,煤泥滤饼粒 度细、水分高、粘度大、品质低,很难实现高效工业应用,以民用地销为主要出路。
[0003] 目前,电力行业仅有少数循环流化床(CFB)锅炉可直接采用掺烧的方式进行压滤 煤泥的利用,掺烧份额基本控制在总燃料量的30%以下。该利用方式不仅需要大功率的 煤泥栗送系统,而且需要将压滤好的煤泥再添加水分以保证其水分达到煤泥栗送系统的要 求,以国内某l〇25t/h CFB锅炉为例,选煤厂供给的煤泥水分在22%〜26%之间,为了满 足煤泥泵送系统输送要求,须将煤泥添加水分至30%左右,从而导致排烟热损失增加,降低 锅炉热效率,降低了煤泥的利用价值。
[0004] 目前,实际生产中,大量洗选煤泥只能采用掺入洗选后的商品煤等方式进行处理, 由于煤泥中含有大量水分,热值低,降低了成品商品煤的品质和经济价值。
[0005] 近年来随着我国城市污水处理的发展,污泥的产量呈急剧上升趋势,产生了数量 巨大的高水分污泥,由于含有各种病原体、重金属等有毒有害物质,必须要进行处理处置。 [0006] 而日益严峻的土地资源对污泥处理的时间和空间也提出了很高的要求。污泥焚烧 的优点在于能够很大程度地降低污泥的体积,分解污泥中的有毒有机 质,能够回收利用污泥焚烧产生的热能,符合我国可持续发展道路,但污泥的焚烧前需 进行 干燥处理。
[0007]因此,煤泥、污泥等高水分物料经干燥提质加工后,便于实现其有效利用、提高商 业价值、减少占地面积、降低环境污染,为企业增加经济效益。
[0008]目前,应用较为广泛煤泥干燥工艺是煤泥滚筒干燥工艺。该工艺系统主要由热源、 打散装置、带式上料机、进料机、回转滚筒、带式出料机、引风机、卸料器和配电柜构成, 其基本原理是通过滚筒的旋转,使煤泥在缓慢移动过程中被高温热烟气供干。
[0009]煤泥滚筒干燥工艺系统相对较为简单,技术较为成熟,但也存在包括传热系数低、 单套系统处理能力受限、成品粒度品质差、占地面积大等明显缺陷。
发明内容
[0010]为了克服上述现有技术的缺点,本发明的目的是提供一种煤泥、污泥干燥提质装 置及工艺,具有干燥效果更好、运行可靠、系统简单、结构紧凑的特点。
[0011]为了头现上述目的,本发明的技术方案是这样实现的:一种煤泥、污泥干燥提质 装置,包括干燥管3,干燥管3的下端或侧下部与物料打散装置4的出口相连通,干燥管1 的出口与分离器9的进口相连通,其特征在于,干燥管3的出口以下、物料打散装置^的 出口以上的千;):栄管3的中部或上部位置处配置有待千燥高水分物料进口,物料打散装置4 的^气进口布置在物料打散装置4的中部或底部并与烟气发生炉5的烟气出口相连通, 分离器9的尾气出口与除尘器12的进口相连通,分离器9的成品出口与成品输送装置u 相连通,除尘器12的细颗粒出口与细颗粒输送装置10相连通,除尘器12的尾气出口经 引风机13与大气相连通。
[0012] —种煤泥、污泥干燥提质工艺,该干燥提质工艺采用的装置包括干燥管3,干燥管 3的下端或侧下部与物料打散装置4的出口相连通,干燥管3的出口与分离器9的进口 相连通,干燥管3的出口以下、物料打散装置4的出口以上的千燥管3的中部或上部位置 处配置有待干燥高水分物料进口,物料打散装置4的烟气进口布置在物料打散装置4的 中部或底部并与烟气发生炉5的烟气出口相连通,分离器9的尾气出口与除尘器12的进 口 ^连通,分离器9的成品出口与成品输送装置n相连通,除尘器12的细颗粒出口与细 颗粒输送装置10相连通,除尘器12的尾气出口经引风机13与大气相连通其特征在于, 采用烟气发生炉5产生的200〜85(TC高温烟气或空气作为干燥介质,干燥介质由物料 打散装置4的侧部或底部给入,煤泥、污泥由干燥管3的中部或上部的待干燥高水分物料 进口给入,煤泥、污泥在物料打散装置4内被破碎、打散的同时,被干燥介质预干燥;干燥 介质夹带打散和预干燥后的较细颗粒进入干燥管3进行进一步干燥,其中粒径不超过设计 上限要求的颗粒被气^携带进入分离器9中,粒径大于设计上限的颗粒落入物料打散装置 4被再次打散;由分离器9收集的成品经成品输送装置U送入煤场或其它地方,由分离 器9排出的尾气经除尘器12处理后通过引风机13排入大气,除尘器12产生的细颗粒经 细颗粒输送装置10送入煤场或其它地方。
[0013]所说的干燥管3中位于待干燥高水分物料进口之下、物料打散装置4之上的位 置处配置有物料预打散装置14或格栅以控制进入物料打散装置4的物料粒度。
[0014]所说的烟气发生炉5可以是燃煤炉,也可以是燃气炉,燃煤炉可以是链条炉、流化 床炉或煤粉炉。所说的热烟气发生炉5可以单独配置,也可以利用现有锅炉,如电站锅炉, 作为热烟气发生炉,通过在适当位置抽取合适温度的热烟气作为干燥介质。
[0015]所说的物料打散装置4可以采用过风式反击破碎机、过风式锤击破碎机、风扇磨 煤机或类似简化装置。
[°016]所说的干燥管3同时具有气力分选作用,可控制由干燥介质携带离开干燥管的干 燥成品的颗粒粒度和干燥程度。所说的干燥管3内的干燥介质速度在5〜25m/s。所说 的干燥管3截面为圆形、方形或不规则形状,不同高度处截面形状可以发生变化,以改变下 行湿物料与上行f燥气流的混合状况以及大颗粒物料的分选情况。
[0017]待千燥高水分物料进口布置在干燥管3中的中部或上部,因此,给入高水分物料 因重力作用下行掉入物料打散装置4过程中,与热烟气流动方向呈逆流流向,使进入物料 打散装置4的湿物料进行初步干燥和分选,以减轻物料打散装置的工作负荷和发生粘堵的 可能性。干燥管3出口可设置惯性分离装置,以加强对出料粒度的分选控制。
[0018] 本发明具有以下优点: 1、采用对流干燥方式,烟气与待干燥高水分物料传热传质强烈,既可加快待干燥高水 分物料中水分扩散速率,又可大幅提高单套设备和系统的处理能力,单套设备可实现处理 能力基本在150t/h以上; 2、 米用物枓玎戒装置和干燥官组合布置的方式,有效解决了高水分物料干燥过程中的 防粘堵问题; 3、 采用空间高度方向为主^置方式,整个工艺系统占地面积小; 4、 通过气流分选和惯性分离以及干燥管的特殊设计,可以实现对成品粒度的有效控 制,保证干燥提质产品的品质; 5、 通过选择和控制干燥介质初温并设置高效除尘设备,可以保证最终排入大气的乏气 满足国家和地方环保排放标准,不污染环境。
[0019] 6、系统阻力小,电耗低。
附图说明
[0020] 图1是本发明的实施例1的结构示意图。
[0021]图2是本发明的实施例2的结构示意图。
[0022]图3是本发明的实施例3的结构示意图。
具体实施方式
[0023]下面结合附图和实施例对本发明做更详细的说明。
[00241…参见图h该实施例1的干燥管3采用等截面结构,待干燥高水分物料进口配置 在干的出口以下、物料打散装置4的出口以上的干燥管3的中部,实现中部给料; 待干燥高水分物料进口与给料机2的出料口相连通,给料机2的进料口与料仓1相连通, 给料机2为煤泥旋切机,物料打散装置4的烟气进口布置在物料打散装置4的底部并与 烟气发生炉5的烟气出口相连通,采用物料打散装置4底部给入烟气的方式,烟气发生炉 5为链条炉。另外,图1中,6为送风机;7为给煤机;8为煤仓;9为旋风分离器;除尘器 12为布袋除尘器。
[0025]。〜参见图2,该实施例2的干燥管3采用变截面结构,待干燥高水分物料进口配置 ^干3的出口以下、物料打散装置4的出口以上的干燥管3的上部,实现上部给料; 燥高水分物料进口与给料机2的出料口相连通,给料机2的进料口与料仓1相连通, 给料机2为煤泥破碎机,物料打散装置4的烟气进口布置在物料打散装置4的上部并与 烟气发生炉5的烟气出口相连通,采用物料打散装置4上部给入烟气的方式,烟气发生 5为链条炉。 另外,图2中,6为送风机;7为给煤机;8为煤仓;分离器9为旋风分离器滁 =^12为布袋除尘器;14为配置在干燥管3中的位于物料打散装置4之上的物料预打 政装置。 参见图3,该实細3的干燥管3采用等截面结构,待千燥高水分物料进口配置 的出口以下、物料打散装置4的出口以上的干燥管3的中部,实现中部给料; 咼水分物料进口与给料机2的出料口相连通,给料机2的进料口与料仓1相连通, 为煤泥旋切机,物料打散装置4的烟气进口布置在物料打散装置4的底部并与 S 的烟气出口相连通,采用物料打散装置4底部给入烟气的方式,烟气发生炉 士床烟气发生炉。另外,图3中,6为送风机;7为给煤机;8为煤仓;分离器9为 惯性分罔器;除尘器12为布袋除尘器。 L〇〇28」压漶后的爪分M刀州%、外观尺寸约为400mm的煤泥滤饼经皮带送入给料机2 破^成粒度不大于5〇mm的煤泥颗粒团并送入干燥管3 ;在重力的作用下,大块煤泥颗粒团 下落进入物料预打散装置14、物料打散装置4或直接进入物料打散装置七细颗粒煤泥随 烟气上升;由发热量低于3000kCal/kg燃用劣质煤的烟气发生炉产生的47CTC左右的烟气 从物料^散装置4的中部或底部给入后,将从干燥管3落入物料打散装置4的大颗粒煤 泥^干燥,在此过程中完成煤泥团的打散,使煤泥粒度满足要求;满足要求的细颗粒煤泥随 文因,上升进入干燥管3,进一步干燥后进入干燥管3出口的分离器9被分离后,经成品输 送装置11输送至成品仓库;由分离器9排出的低温烟气经除尘器12除尘处理后,通过引 ^机13被排入大气;除尘器12产生的细颗粒经细颗粒输送装置10送入煤场或其它地 方。
Claims (8)
1.一种煤泥、污泥干燥提质装置,包括干燥管(3),干燥管(3)的下端或侧下部与物料 装置(4)的出口相连通,干燥管(3)的出口与分离器(9)的进口相连通,其特征在于,干 燥菅(3 it出口以下、物料打散装置(4)的出口以上的干燥管(3)的中部或上部位置处配置 有待y燥尚水分物料进口,物料打散装置(4)的烟气进口布置在物料打散装置(4)的上部 或底部并与烟丨气发生炉(5)的烟气出口相连通,分离器(9)的尾气出口与除尘器(12)的进 口相连^,分、呙器(9)的成品出口与成品输送装置(丨丨)相连通,除尘器(12)的细颗粒出口 与细^2输送装置(10)相连通,除尘器(12)的尾气出口经引风机(13)与大气相连通,所说 的=燥管(3、)中位于待干燥高水分物料进口之下、物料打散装置(4)之上的位置处配置有 物料预打散装置⑽或格栅,所说的干燥管⑶截面为圆形或方形,不同高度处截面形状 相同或不同。
2.根据权利要求1所述的装置,其特征在于,所说的烟气发生炉(5)是燃煤炉或燃气 炉。
3.根据权利要求2所述的装置,其特征在于,所说的燃煤炉是链条炉、流化床炉或煤 粉炉。
4.根据权利要求1所述的装置,其特征在于,所说的物料打散装置(4)为过风式反击 式破碎机、过风式锤击式破碎机或风扇磨煤机。
5.—种煤泥、污泥干燥提质工艺,该干燥提质工艺采用的装置包括干燥管(3 ),干燥管 (3)的下端或侧下部与物料打散装置(4)的出口相连通,干燥管(3)的出口与分离器(9)的 进口相连通,干燥管(3)的出口以下、物料打散装置(4)的出口以上的干燥管(3)的中部或 上部位置处配置有待干燥高水分物料进口,物料打散装置(4)的烟气进口布置在物料打散 装置(4)的上部或底部并与烟气发生炉(5 )的烟气出口相连通,分离器(9 )的尾气出口与除 尘器(12)的进口相连通,分离器(9)的成品出口与成品输送装置(11)相连通,除尘器(12) 的细颗粒出口与细颗粒输送装置(10)相连通,除尘器(丨2)的尾气出口经引风机(13)与大 气相连通,其特征在于,采用烟气发生炉(5)产生的200〜85(TC高温烟气或空气作为干 燥介质,干燥介质由物料打散装置(4)的侧部或底部给入,煤泥、污泥由干燥管(3)的中部 或上部的待干燥高水分物料进口给入,煤泥、污泥在物料打散装置(4)内被破碎、打散的同 时,被干燥介质预干燥;干燥介质夹带打散和预干燥后的较细颗粒进入干燥管(3)进行进 一步干燥,其中粒径不超过设计上限要求的颗粒被气流携带进入分离器(9)中,粒径大于设 计上限的颗粒落入物料打散装置(4)被再次打散;由分离器(g)收集的成品经成品输送装 置(11)送入煤场或其它地方,由分离器(9)排出的尾气经除尘器(12)处理后通过引风机 (13)排入大气,除尘器(m产生的细颗粒经细颗粒输送装置(10)送入煤场或其它地方。
6.根据权利要求5所述的工艺,其特征在于,所说的干燥管(3)同时具有气力分选作 用,能够控制由干燥介质携带离开干燥管的干燥成品的颗粒粒度和干燥程度。
7. 根据权利要求5所述的工艺,其特征在于,所说的干燥管(3)内的干燥介质速度在 5 〜25m/s〇
8. 根据权利要求5所述的工艺,其特征在于,所说的热烟气发生炉(5)为单独配置, 或利用现有锅炉作为热烟气发生炉,通过抽取合适温度的热烟气作为干燥介质。
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CN107285597A (zh) * | 2017-07-21 | 2017-10-24 | 北京中科领向环保研究院有限公司 | 一种利用陶瓷厂废气余热进行污泥烘干的方法及系统 |
CN107285596A (zh) * | 2017-07-21 | 2017-10-24 | 北京中科领向环保研究院有限公司 | 一种利用铝型材厂废气余热进行污泥烘干的方法及系统 |
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CN107285597A (zh) * | 2017-07-21 | 2017-10-24 | 北京中科领向环保研究院有限公司 | 一种利用陶瓷厂废气余热进行污泥烘干的方法及系统 |
CN107285596A (zh) * | 2017-07-21 | 2017-10-24 | 北京中科领向环保研究院有限公司 | 一种利用铝型材厂废气余热进行污泥烘干的方法及系统 |
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