CN105601075B - 一种污泥热解碳化处理的工艺方法及其装置 - Google Patents
一种污泥热解碳化处理的工艺方法及其装置 Download PDFInfo
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- CN105601075B CN105601075B CN201610177082.6A CN201610177082A CN105601075B CN 105601075 B CN105601075 B CN 105601075B CN 201610177082 A CN201610177082 A CN 201610177082A CN 105601075 B CN105601075 B CN 105601075B
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- sludge
- pyrolysis
- furnace
- rotary kiln
- mixing
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- 239000010802 sludge Substances 0.000 title claims abstract description 98
- 238000003763 carbonization Methods 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000000197 pyrolysis Methods 0.000 claims abstract description 81
- 238000010438 heat treatment Methods 0.000 claims abstract description 73
- 238000002156 mixing Methods 0.000 claims abstract description 72
- 238000001035 drying Methods 0.000 claims abstract description 55
- 239000007789 gas Substances 0.000 claims abstract description 51
- 239000000203 mixture Substances 0.000 claims abstract description 34
- 238000003860 storage Methods 0.000 claims abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 21
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000003546 flue gas Substances 0.000 claims abstract description 8
- 238000000746 purification Methods 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 238000007599 discharging Methods 0.000 claims description 16
- 239000010865 sewage Substances 0.000 claims description 12
- 239000000446 fuel Substances 0.000 claims description 11
- 239000000470 constituent Substances 0.000 claims description 10
- 239000000654 additive Substances 0.000 claims description 6
- 230000000996 additive Effects 0.000 claims description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium monoxide Chemical group 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- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic Chemical compound 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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Abstract
本发明公开了一种污泥热解碳化处理的工艺方法及其装置，污泥经压榨机压榨、粉碎机粉碎、混合搅拌机混拌、内加热回转窑烘干机内烘干后送入储料仓内后送入热解碳化炉内；污泥在热解碳化炉内发生热解碳化，产物固态碳的混合物输出系统外，产物水蒸气、热解气进入分离提纯塔中进行分离、提纯；提纯后的可燃气送入燃烧器中燃烧为内加热回转窑烘干机输送热源，提纯分离出的重组分送到混合搅拌机与污泥混拌进行二次热解；加热炉产生的烟气排出至热风炉内进行二次烧蚀；整个装置产生的尾气经内加热回转窑烘干机的出口I排出，经过处理后达标排放。本发明具有生产工艺简单、产出物状态稳定、无二次污染的优点，实现了污泥处理的减量化、无害化、资源化。
Description
一种污泥热解碳化处理的工艺方法及其装置
技术领域
[0001] 本发明涉及一种污泥热解碳化处理工艺方法及其装置，特别涉及一种利用热解碳 化工艺及其装置，实现污水厂的污泥减量化、无害化、资源化。
背景技术
[0002] 随着经济发展和人民环保意识的加强，城镇污水处理事业不断发展，污水厂总处 理水量和处理程度将不断扩大和提高，产生的污泥量也日益增加。目前对污泥主要是进行 浓缩、调治、脱水、稳定、干化或焚烧处理。国内外常用的成熟的污泥稳定工艺有:厌氧消化、 好氧消化、热处理、加热干化和加碱稳定;常用的污泥处置是土地利用、焚烧、卫生填埋、堆 月巴、投海等。污泥处理处置的投资和运行费较高，如处置不当，将造成“二次污染”，这已成为 环境保护领域难题，备受关注。
发明内容
[0003] 本发明所要解决的技术问题是针对现有技术中存在的不足，而提供一种污泥热解 碳化处理的工艺方法，用以解决污泥处置不当所造成的二次污染，产物状态稳定，实现了污 泥处理的减量化、无害化、资源化。
[0004] 本发明的目的之二是提供一种污泥热解碳化处理的工艺装置，组装简单，操作简 便。
[0005] 为了实现上述目的，本发明采用如下技术方案：
[0006] —种污泥热解碳化处理的工艺方法，包括以下步骤：
[0007] (1)压榨、粉碎和混拌:将污水厂处理污水后产生的含水率90 %以上的污泥〇V)经 压榨后制备成含水率小于60 %的污泥;将所述的含水率小于60 %的污泥经过粉碎后进行混 拌；
[0008] (2)烘干：将步骤（1)混拌后的混合物进行烘干，至混合物中污泥的含水率低于 30 %后储存备用；
[0009] ⑶热解碳化:将步骤(2)储存的物料进行热解碳化，形成水蒸气、热解气和固态碳 的混合物(C)，将固态碳的混合物排出系统外，将水蒸气和热解气进行分离提纯；
[0010] (4)分离提纯:将步骤(3)制备而成的水蒸气和热解气进行分离提纯，其中所得到 的气体作为燃料为步骤(2)的烘干步骤提供热源，其中所得到的重组分作为原料，与步骤 (1)所述的粉碎后的含水率小于60%的污泥混拌后继续循环进行烘干、热解碳化和分离提 纯。
[0011] 上述技术方案中，所述的工艺方法具体为：
[0012] (1)压榨、粉碎和混拌:将污水厂处理污水后产生的含水率90%以上的污泥(A)，输 送至压榨机内进行压榨，压榨成含水率小于60 %的污泥;然后将含水率小于60 %的污泥输 送至粉碎机中进行粉碎，粉碎至粒径为20mm以下;再将粉碎后的污泥输送至混合搅拌机中 进行混拌。
[0013] 所述的压榨机，压榨温度为常温，压榨压力为15〜25MPa，压榨时间为70〜120分 钟；
[0014] 所述的混合搅拌机，混拌的速率为3〜10转/分，混拌温度为40°C〜60°C ;
[0015] (2)烘干:将步骤⑴混合搅拌机内混拌形成的混合物通过螺旋给料机输送至内加 热回转窑烘干机中进行烘干，烘干至混合物中污泥的含水率低于30%;烘干后的产物经内 加热回转窑烘干机的下出料口、通过螺旋输送机I输送至储料仓中进行储存；
[0016] 所述的内加热回转窑烘干机，烘干的温度为80°C〜140°C，烘干时间为45〜60分 钟；
[0017] (3)热解碳化:将步骤(2)中储料仓中的物料通过螺旋输送机II输送至热解碳化炉 中进行热解碳化，热解碳化炉的炉体外部套设有加热炉，加热炉维持热解碳化炉的炉内温 度为700°C〜900°C ;污泥在热解碳化炉内的高温无氧状态下发生热解碳化，主要产物为水 蒸气、热解气和固态碳的混合物(C)，固态碳的混合物排出系统外，水蒸气和热解气进入分 离提纯塔中。在高温作用下，污泥中的重金属被固化在固态碳的混合物中，状态稳定、不会 被水析出、不产生污染。
[0018] (4)分离提纯:将步骤(3)中热解碳化炉内产生的水蒸气、热解气进入分离提纯塔 (17)中进行分离提纯，塔顶的温度为80 °C〜100 °C、压力为50〜60kpa，塔底的温度为350°C 〜400 °C、压力为100〜150kpa;塔顶分离提纯出的气体作为燃料通入热风炉专用的燃烧器 中，塔底分离出的重组分(焦油)输送至步骤（1)所述的混合搅拌机中与粉碎后的污泥混拌 后继续循环进行烘干、热解碳化和分离提纯。
[0019] 上述技术方案中，步骤（1)中，粉碎后的污泥在混合搅拌机中进行混拌时，还可以 加入药物和添加剂;所述的药物为生石灰，用来平衡污泥的酸碱度，同时在反应时放出热 量，为污泥加温，生石灰的添加量为粉碎后污泥重量的2〜3%;所述的添加剂为木肩或煤 粉，用来提高污泥的热值，添加剂的添加量为粉碎后污泥重量的〇〜10% (不是所有的污泥 都加，市政污泥的热值较高，就不用加）。
[0020] 上述技术方案中，步骤⑶中，加热炉加热过程中产生烟气，烟气导入热风炉中，通 过燃烧器在热风炉内燃烧进行二次烧蚀，有害气体在高温作用下被净化，所产生的热风为 内加热回转窑烘干机加热；整个装置产生的尾气由内加热回转窑烘干机的出口 I排出经常 规处理后达标排放，即B。
[0021] 上述技术方案中，步骤⑷中，分离提纯塔分离出的重组分输送至步骤⑴所述的 混合搅拌机中与粉碎后的污泥进行混拌时，重组分与粉碎后的污泥的重量比为1: 450〜 550,优选为 1:500。
[0022] 一种污泥热解碳化处理的工艺装置，包括压榨机、粉碎机、混合搅拌机、螺旋给料 机、内加热回转窑烘干机、储料仓、热解碳化炉、分离提纯塔：
[0023] 所述的压榨机出料口与粉碎机的进料口相连；
[0024] 所述的粉碎机出料口与混合搅拌机的进料口相连；
[0025] 所述的混合搅拌机出料口通过螺旋给料机与内加热回转窑烘干机的进料口相连；
[0026] 所述的内加热回转窑烘干机，下出料口通过螺旋输送机II与储料仓的进料口相连 接;所述的内加热回转窑烘干机的上方设有排出尾气用的出口 I，内加热回转窑烘干机的尾 部配设有热风炉，所述的热风炉的炉尾配设有燃烧器;所述的燃烧器设有燃气进口；
[0027] 所述的储料仓，出料口通过螺旋输送机III与热解碳化炉的进料口相连接；
[0028] 所述的热解碳化炉，出料口与输送固态碳的混合物的螺旋输送机I相连接，将固态 碳的混合物输出装置外;所述的热解碳化炉的上方设有排气口并与分离提纯塔的进料口相 连接；
[0029] 所述的分离提纯塔，出料口与混合搅拌机的进料口相连接，排气口与燃烧器的燃 气进口相连接，提纯后的气体作为燃料供热风炉使用。
[0030] 上述技术方案中，所述的热解碳化炉为外加热式热解碳化炉，炉体外部套设有加 热炉。
[0031] 上述技术方案中，所述的加热炉设有出口 II，所述的热风炉设有入口，所述的出口 II与入口相连接。
[0032] 上述技术方案中，所述的燃烧器为专供热风炉使用的组合式燃烧器。
[0033] 上述技术方案中所述的压榨机，是利用压力栗，将泥浆压入相邻两滤板形成的密 闭滤室中，使滤布两边形成压力差，从而实现固液分离;它将含水率90%以上的污泥压榨成 含水率小于60 %的污泥，供滚筒式内加热干燥炉使用。
[0034] 上述技术方案中所述的粉碎机，它是用来将压榨机压榨后的泥饼粉碎，以便混拌 机更均匀的混拌。
[0035] 上述技术方案中所述的混合搅拌机，它是由带导热夹套的外壳及正反螺旋构成， 对粉碎后的污泥进行前期预热，其热源为采集的余热；同时对污泥加药和添加剂进行混拌， 以便污泥均匀受热。
[0036] 上述技术方案中所述的螺旋给料机，它是用来输送污泥，同时起到密封的作用；以 防止空气进入炉窑，影响热解反应。
[0037] 上述技术方案中所述的内加热回转窑烘干机，它是用来对污泥进行前期烘干，使 污泥水分降至30%以下，便于热解碳化;整个过程是在密闭环境下进行，排放口温度在120 °C〜140°C之间，其成分为水蒸气和粉尘，经处理后排放，对环境不产生污染。
[0038] 上述技术方案中所述的储料仓，它是用来储存干燥后的污泥，对污泥进入外加热 式热解碳化炉之前起到一个缓冲和料封的作用。
[0039] 上述技术方案中所述的热解碳化炉，为外加热式热解碳化炉，它是由外加热炉和 旋转窑构成。其作用是将干燥后的污泥进行热解碳化。外加热炉的燃料为天然气或燃油，通 过燃烧器对旋转窑加温。产生的尾气送入热风炉进行二次烧蚀。当旋转窑内温度达到450°C 以上时，将储料仓的干燥污泥通过下方的螺旋输送机送入旋转窑内进行热解碳化。旋转窑 内始终处于微正压。污泥中的有机成分在高温隔氧状态下，一部分生成气体，经过提纯，作 为燃料供热风炉使用。另一部分生成稳定的碳的混合物，污泥中的重金属被烧结在其中，不 宜被析出。该产物可作为建筑材料或土壤改良剂使用，消除二次污染，实现减量化、无害化、 资源化。
[0040] 上述技术方案中所述的加热炉，它是用来为热解碳化炉的外部加热而设置的。由 于污泥热解是在无氧状态下实现的，所以对热解碳化炉进行外部加热。
[0041] 上述技术方案中所述的分离提纯塔，它是将外加热式热解碳化炉中污泥产生的气 体进行分离、提纯;提纯后的气体作为燃料供热风炉使用;分离出的重组分送到混拌机与新 鲜污泥混拌，进行二次热解。
[0042] 上述技术方案中所述的燃烧器，它是一种供热风炉使用的组合式燃烧器；它可以 单独使用天然气和热解气，也可以同时使用天然气和热解气;装置升温时用天然气，加料后 有热解气产生后，天然气和热解气同时使用；当热解气够量时，关闭天然气，单独使用热解 气。
[0043] 上述技术方案中所述的热风炉，它是用来烧蚀装置中发生的有害气体，同时将产 生的热量直接供给滚筒式内加热干燥窑使用，消除污染，节省能源。
[0044] 本发明所述的压榨机，粉碎机，混合搅拌机，螺旋给料机，内加热回转窑烘干机，加 热炉，外加热式热解碳化炉，螺旋输送机I，螺旋输送机II，储料仓，热风炉，分离提纯塔，燃 烧器，螺旋输送机III均为普通市售产品。
[0045] 本发明技术方案与传统的污泥处理方法相比，具有如下优点和积极效果：
[0046] 1、具有生产工艺简单，产出物状态稳定，无二次污染；
[0047] 2、实现了污泥处理的减量化、无害化、资源化。
附图说明
[0048] 图1:本发明污泥热解碳化处理的工艺方法的流程示意图；
[0049] 其中，1.压榨机，2.粉碎机，3.混合搅拌机，4.螺旋给料机，5.内加热回转窑烘干机 的出口，6.内加热回转窑烘干机，7.加热炉，8.热解碳化炉，9.螺旋输送机I，10.加热炉的出 口，11.热解碳化炉的排气口，12.内加热回转窑烘干机的下出料口，13.螺旋输送机II，14. 储料仓，15.热风炉，16.热风炉的入口，17.分离提纯塔，18.燃烧器，19.螺旋输送机III; A为 含水率90%以上的污泥，B为排放的达标的尾气，C为固态碳的混合物。
具体实施方式
[0050] 以下对本发明技术方案的具体实施方式详细描述，但本发明并不限于以下描述内 容：
[0051 ] 本发明提供一种污泥热解碳化处理的工艺装置，包括压榨机1、粉碎机2、混合搅拌 机3、螺旋给料机4、内加热回转窑烘干机6、储料仓14、热解碳化炉8、分离提纯塔17:
[0052] 所述的压榨机出料口与粉碎机的进料口相连；
[0053] 所述的粉碎机出料口与混合搅拌机的进料口相连；
[0054] 所述的混合搅拌机出料口通过螺旋给料机4与内加热回转窑烘干机的进料口相 连；
[0055] 所述的内加热回转窑烘干机，下出料口通过螺旋输送机II 13与储料仓的进料口 相连接;所述的内加热回转窑烘干机的上方设有排出尾气用的出口 I 5,内加热回转窑烘干 机的尾部配设有热风炉15,所述的热风炉的炉尾配设有燃烧器18;所述的燃烧器设有燃气 进口；
[0056] 所述的储料仓，出料口通过螺旋输送机III 19与热解碳化炉的进料口相连接；
[0057] 所述的热解碳化炉，出料口与输送固态碳的混合物的螺旋输送机I 9相连接，将固 态碳的混合物输出装置外;所述的热解碳化炉的进料口上方设有排气口 11并与分离提纯塔 的进料口相连接；
[0058] 所述的分离提纯塔，出料口与混合搅拌机的进料口相连接，排气口与燃烧器的燃 气进口相连接，提纯后的气体作为燃料供热风炉使用。
[0059] 所述的热解碳化炉8为外加热式热解碳化炉，炉体外部套设有加热炉7;所述的加 热炉7设有出口 II 10，所述的热风炉15设有入口 16，出口 II与入口相连接。所述的燃烧器18 为供热风炉15使用的组合式燃烧器。
[0060] 本发明所述的压榨机，粉碎机，混合搅拌机，螺旋给料机，内加热回转窑烘干机，加 热炉，外加热式热解碳化炉，螺旋输送机I，螺旋输送机II，储料仓，热风炉，分离提纯塔，燃 烧器，螺旋输送机III均为普通市售设备。
[0061] 本发明提供一种污泥热解碳化处理的工艺方法，流程图如图1所示，包括以下步 骤：
[0062] (1)压榨、粉碎和混拌:将污水厂处理污水后产生的含水率90%以上的污泥A，输送 至压榨机1内进行压榨，压榨成含水率小于60%的污泥;然后将含水率小于60%的污泥输送 至粉碎机2中进行粉碎，再将粉碎后的污泥输送至混合搅拌机3中进行混拌。
[0063] (2)烘干:将步骤（1)混合搅拌机内混拌形成的混合物通过螺旋给料机4输送至内 加热回转窑烘干机6中进行烘干，烘干至混合物中污泥的含水率低于30%;烘干后的产物经 内加热回转窑烘干机的下出料口 12、通过螺旋输送机I 13输送至储料仓14中进行储存；
[0064] (3)热解碳化:将步骤(2)中储料仓中的物料通过储料仓下方的螺旋输送机II 19 输送至热解碳化炉8中进行热解碳化，污泥在热解碳化炉内的高温无氧状态下发生热解碳 化，主要产物为水蒸气、热解气和固态碳的混合物C，固态碳的混合物通过螺旋输送机I 9排 出，水蒸气和热解气由热解碳化炉8的排气口 11排出、经管路进入分离提纯塔17中；
[0065] (4)分离提纯:将步骤(3)中热解碳化炉内产生的水蒸气、热解气进入分离提纯塔 中进行分离提纯，塔顶分离提纯出的气体作为燃料通入热风炉专用的燃烧器18中，通过热 风炉15为内加热回转窑烘干机输送热源;塔底分离出的重组分输送至步骤（1)所述的混合 搅拌机中与粉碎后的污泥进行混拌进行二次热解。
[0066] 热解碳化炉8的炉体外部套设有加热炉7，加热炉7产生的烟气由出口 10排出，通过 热风炉15的入口 16进入热风炉15内进行二次烧蚀;整个装置产生的尾气经内加热回转窑烘 干机6的出口 5排出，经过处理后达标排放。
[0067] 下面结合具体的实施例对本发明方法和装置进行具体的描述：
[0068] 实施例1:
[0069] 该实施例中所用的压榨机型号为WGL— 11，粉碎机型号为LSF30—2，混合搅拌机型 号为LSB600，螺旋给料机型号为LSJ28—2.5，内加热回转窑烘干机型号为LSGl200—12，加 热炉型号为LSL6,外加热式热解碳化炉型号为LSR800—10,螺旋输送机I型号为LSJ28—3， 螺旋输送机Π型号为LSJ30—3,储料仓型号为LSC1，热风炉型号为LSR12000,分离提纯塔型 号为LST500—3，燃烧器型号为STAR—500，螺旋输送机III型号为LSJ30—3。
[0070] 处理的污泥为北京市顺义新城生态调水中心和顺义区金马开发区污水处理厂处 理污水后形成的污泥，其中污泥的含水率85〜90 %，有毒重金属铜、锌、铅、镉、镍、铬、砷、汞 的含量分别为 73.7mg/kg、544mg/kg、〈9mg/kg、〈5mg/kg、96 · 9mg/kg、123mg/kg、12.4mg/kg、 0.499mg/kg，（如表I所示)经本发明下述方法进行处理：
[0071] (1)压榨、粉碎和混拌:将污泥输送至压榨机1内进行压榨，压榨成含水率小于60% 的污泥;然后将含水率小于60 %的污泥输送至粉碎机2中进行粉碎，粉碎至粒径为20mm以 下;再将粉碎后的污泥输送至混合搅拌机3中进行混拌。
[0072] 所述的压榨机，压榨温度为常温、压力20MPa、压榨时间约为90分钟；
[0073] 所述的混合搅拌机，混拌的速率为6转/分，混拌温度为50°C〜55°C ;
[0074] (2)烘干:步骤（1)混合搅拌机内混拌形成的混合物通过螺旋给料机4输送至内加 热回转窑烘干机6中进行烘干，烘干至混合物中污泥的含水率低于30%;烘干后的产物经内 加热回转窑烘干机的下出料口 12、通过螺旋输送机I 13输送至储料仓14中进行储存；
[0075] 所述的内加热回转窑烘干机，烘干的温度为105〜IHTC，烘干时间约为52分钟；
[0076] (3)热解碳化:步骤(2)中储料仓中的物料通过螺旋输送机II (19)输送至热解碳化 炉8中进行热解碳化，热解碳化炉8的炉体外部套设有加热炉7,加热炉维持热解碳化炉的炉 内温度为790〜810°C;污泥在热解碳化炉内的高温无氧状态下发生热解碳化，主要产物为 水蒸气、热解气和固态碳的混合物C，固态碳的混合物排出系统外，水蒸气和热解气进入分 离提纯塔17中。
[0077] (4)分离提纯:步骤(3)中热解碳化炉内产生的水蒸气、热解气进入分离提纯塔17 中进行分离提纯，塔顶的温度为80〜85°C、压力为55kpa，塔底的温度为370〜380°C、压力为 125kpa;塔顶分离提纯出的气体作为燃料通入热风炉专用的燃烧器18中，塔底分离出的重 组分输送至步骤（1)所述的混合搅拌机中与粉碎后的污泥进行混拌进行二次热解，重组分 与粉碎后的污泥的重量比为1:500。
[0078] 步骤⑶中，加热炉7加热过程中产生烟气，烟气导入热风炉15中，通过燃烧器18在 热风炉内燃烧进行二次烧蚀，有害气体在高温作用下被净化，所产生的热风为内加热回转 窑烘干机加热；整个装置产生的尾气由内加热回转窑烘干机的出口 I排出经常规处理后达 标排放，即B。
[0079] 尾气按《危险废物焚烧大气污染物排放标准》DBl 1/503—2007检测；固态碳的混合 物C按《危险废物鉴别标准浸出毒性鉴别》GB5085.3—2007和《固体废物总汞的测定冷原子 吸收分光光度法》GB/T15555.1—1995检测，其值如表1所示：
[0080] 表1:本发明方法处理重金属的效果
[0081]
[0082]由表1可知，用本发明方法及装置处理污泥，污泥中的重金属被固化在固态碳的混 合物中，状态稳定、不会被水析出、不产生污染。
[0083]上述实例只是为说明本发明的技术构思以及技术特点，并不能以此限制本发明的 保护范围。凡根据本发明的实质所做的等效变换或修饰，都应该涵盖在本发明的保护范围 之内。
Claims (6)
1. 一种污泥热解碳化处理的工艺方法，其特征在于，包括以下步骤： (1) 压榨、粉碎和混拌:将污水厂处理污水后产生的含水率90%以上的污泥输送至压榨 机(1)内进行压榨，压榨成含水率小于60%的污泥;然后将含水率小于60%的污泥输送至粉碎 机(2)中进行粉碎，粉碎至粒径为20mm以下;再将粉碎后的污泥输送至混合搅拌机(3)中进 行混拌； 所述的压榨机，压榨温度为常温，压榨压力为15〜25 MPa，压榨时间为70〜120分钟； 所述的混合搅拌机，混拌的速率为3〜10转/分，混拌温度为40°C〜60°C ; (2) 烘干:将步骤（1)混合搅拌机内混拌形成的混合物通过螺旋给料机(4)输送至内加 热回转窑烘干机(6)中进行烘干，烘干至混合物中污泥的含水率低于30%;烘干后的产物经 内加热回转窑烘干机的下出料口（12)、通过螺旋输送机I (13)输送至储料仓（14)中进行储 存； 所述的内加热回转窑烘干机，烘干的温度为80°C〜140°C，烘干时间为45〜60分钟； (3) 热解碳化:将步骤(2)中储料仓中的物料通过螺旋输送机II (19)输送至热解碳化炉 (8)中进行热解碳化，热解碳化炉(8)的炉体外部套设有加热炉(7)，加热炉维持热解碳化炉 的炉内温度为700°C〜900°C;污泥在热解碳化炉内的高温无氧状态下发生热解碳化，主要产 物为水蒸气、热解气和固态碳的混合物，固态碳的混合物排出系统外，水蒸气和热解气进入 分离提纯塔(17)中； (4) 分离提纯:将步骤(3)中热解碳化炉内产生的水蒸气、热解气进入分离提纯塔（17) 中进行分离提纯，塔顶的温度为80°C〜100°C、压力为50〜60kpa，塔底的温度为350°C〜400°C、 压力为100〜150kpa;塔顶分离提纯出的气体作为燃料通入热风炉专用的燃烧器（18)中，塔 底分离出的重组分输送至步骤(1)所述的混合搅拌机中与粉碎后的污泥进行混拌进行二次 热解。
2. 根据权利要求1所述的工艺方法，其特征在于，步骤（1)中，粉碎后的污泥在混合搅 拌机中进行混拌时，还可以加入药物和添加剂;所述的药物为生石灰，添加量为粉碎后污泥 重量的2〜3%;所述的添加剂为木肩或煤粉，添加量为粉碎后污泥重量的0〜10%。
3. 根据权利要求1所述的工艺方法，其特征在于，步骤(3)中，加热炉（7)加热过程中产 生烟气，烟气导入热风炉（15)中，通过燃烧器（18)在热风炉内燃烧，有害气体在高温作用下 被净化，所产生的热风为内加热回转窑烘干机(6)加热;整个工艺装置产生的尾气由内加热 回转窑烘干机的出口 I排出、经常规处理后达标排放。
4. 根据权利要求1所述的工艺方法，其特征在于，步骤(4)中，分离提纯塔（17)分离出的 重组分输送至步骤（1)所述的混合搅拌机中与粉碎后的污泥混拌时，重组分与粉碎后的污 泥的重量比为1:450〜550。
5. 根据权利要求1所述的工艺方法，其特征在于，重组分与粉碎后的污泥的重量比为1: 500 〇
6. —种污泥热解碳化处理的工艺装置，包括压榨机（1)、粉碎机(2)、混合搅拌机(3)、螺 旋给料机(4)、内加热回转窑烘干机(6)、储料仓（14)、热解碳化炉(8)、分离提纯塔（17)，其 特征在于： 所述的压榨机出料口与粉碎机的进料口相连； 所述的粉碎机出料口与混合搅拌机的进料口相连； 所述的混合搅拌机出料口通过螺旋给料机与内加热回转窑烘干机的进料口相连； 所述的内加热回转窑烘干机下出料口通过螺旋输送机II (13)与储料仓的进料口相连 接;所述的内加热回转窑烘干机的上方设有排出尾气用的出口 I (5)，内加热回转窑烘干机 的尾部配设有热风炉（15)，所述的热风炉的炉尾配设有燃烧器（18);所述的燃烧器设有燃 气进口； 所述的储料仓出料口通过螺旋输送机III (19)与热解碳化炉的进料口相连接； 所述的热解碳化炉出料口与输送固态碳的混合物的螺旋输送机I (9)相连接，将固态碳 的混合物输出装置外;所述的热解碳化炉的上方设有排气口（11)并与分离提纯塔的进料口 相连接； 所述的分离提纯塔底部出料口与混合搅拌机的进料口相连接，所述的分离提纯塔上部 排气口与燃烧器的燃气进口相连接，提纯后的气体作为燃料供热风炉使用； 所述的热解碳化炉(8)为外加热式热解碳化炉，炉体外部套设有加热炉(7); 所述的加热炉(7)设有出口 II(IO); 所述的热风炉（15)设有入口（16); 所述的出口 Π (10)与入口（16)相连接； 所述的燃烧器（18)为供热风炉（15)使用的组合式燃烧器。
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