WO2019001516A1 - 一种湿污泥焚烧方法及流化床焚烧炉 - Google Patents

一种湿污泥焚烧方法及流化床焚烧炉 Download PDF

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WO2019001516A1
WO2019001516A1 PCT/CN2018/093378 CN2018093378W WO2019001516A1 WO 2019001516 A1 WO2019001516 A1 WO 2019001516A1 CN 2018093378 W CN2018093378 W CN 2018093378W WO 2019001516 A1 WO2019001516 A1 WO 2019001516A1
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wet sludge
dense phase
sludge
phase zone
mud
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PCT/CN2018/093378
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English (en)
French (fr)
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俞国豪
张冬梅
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俞国豪
张冬梅
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Publication of WO2019001516A1 publication Critical patent/WO2019001516A1/zh

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/24—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a vertical, substantially cylindrical, combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/70—Blending
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/12—Sludge, slurries or mixtures of liquids

Definitions

  • the invention relates to a wet sludge incineration method and a fluidized bed incinerator, in particular to a dry and wet sludge co-firing method and a feed-type wet and dry sludge mixed-fired fluidized bed incinerator.
  • the sludge moisture content of most sewage treatment plants after centrifugation or vacuum dewatering is 75-85%, while the heat of drying base is only 2500-4000 kcal/kg.
  • the heat provided by wet sludge combustion alone is not enough to maintain The furnace temperature of 750-900 °C.
  • the sludge having a moisture content of more than 75% to be dried or pressure-filtered before being put into the furnace to reduce the moisture content.
  • metal indentation heating surfaces are arranged in these incinerators, and heat is absorbed by heat transfer oil or steam.
  • the sludge used as fuel for this incinerator is like a general coal-fired fluidized bed furnace, which is added from above the dense phase zone.
  • the above method not only causes the structure of the incinerator to be complicated, but also increases the energy consumption generated by the incineration process.
  • the invention provides a wet sludge incineration method and a fluidized bed incinerator, which mainly solves the problems of complicated structure and high energy consumption in the prior art.
  • the wet sludge incineration method comprises the following steps:
  • the dry sludge and the wet sludge are respectively introduced into the bottom of the dense phase zone through a plurality of inlet mud points; by adjusting the amount of dry and wet sludge, the temperature of the dense phase zone is controlled at 750-950 ° C; The setting should ensure that the dry and wet sludge is mixed evenly with the combustion air.
  • the elevation of the entry point should be 50 to 200 mm higher than the outlet of the hood.
  • the dry sludge is carried into the dense phase zone by the air, and the wet sludge is extruded into the dense phase zone.
  • the amount of mud entering each cubic meter in the dense phase zone is 5 to 60, wherein the wet sludge enters the mud point is 3 to 30, and the dry sludge enters the mud point is 2 to 30.
  • the wet sludge fluidized bed incinerator comprises a furnace body, a dense phase zone with high material concentration is arranged in the furnace body, a hood air outlet is arranged at the bottom of the furnace body, and a plurality of mud inlet pipes are included, and the mud pipe is used for respectively
  • the dry sludge and the wet sludge are introduced into the bottom of the dense phase zone of the furnace body, and the dry sludge and the wet sludge are relatively uniformly mixed with the combustion air in the dense phase zone, and the temperature in the dense phase zone of the furnace is 750-950 ° C;
  • the elevation of the mud outlet of the mud pipe should be 50 to 200 mm higher than that of the hood outlet.
  • the dense phase zone has 5 to 60 inlet pipes per cubic meter, wherein the wet sludge is 3 to 30, and the dry sludge is 2 to 30.
  • the wet sludge incineration method provided by the invention adopts a feed-feeding method to simplify the existing treatment process.
  • the fluidized bed incinerator provided by the invention does not have a pressure-absorbing heat-absorbing surface in the furnace, but directly injects part of the wet sludge into the furnace for incineration.
  • the heat of combustion mainly consists of the moisture of the wet sludge evaporating heat, solids and gas (including The steam and the combustion flue gas are heated and absorbed, which saves the construction cost and reduces the amount of sludge that needs to be dried, and avoids the high energy consumption caused by the continuous drying of the wet sludge or the filter press treatment.
  • Figure 1 is a schematic structural view of the present invention
  • the method and the structure of the present invention provide the heat of evaporation of the wet sludge moisture, the heat absorption of the solid and gas (including steam and combustion fumes) is mainly in the dense phase region at the bottom of the furnace, the heat release from the combustion should be as close as possible to the dense phase.
  • the zone is completed to maintain the heat balance in the dense phase zone to ensure stable combustion.
  • wet sludge and dry sludge are required to have a sufficiently high combustion fraction in the dense phase zone.
  • domestic wet sludge is a fuel with a high volatile content of dry ashless base, and most of it is converted into a gaseous state at 400-500 ° C, which makes it difficult to have a sufficiently high combustion fraction in the dense phase region.
  • the dry sludge is small in particle size and light in specific gravity, if it is simply added from above the dense phase zone, the release of its volatile matter is basically completed on the surface of the dense phase zone, and the combustion fraction in the dense phase zone is small; When added, the particles may be large and the ratio is large. It seems that the dense phase zone will stay in the dense phase for a long time, but the wet sludge particles added from the dense phase zone will enter the dense phase zone and will be in the bed. The combination of impact and rapid release of water vapor bursts into many small particles, which float on the surface of the dense phase to complete the drying and release of volatiles. The combustion process is completed on the dense phase region, and the combustion fraction in the dense phase region is also the same. Very small.
  • Feeding point is directly selected at the bottom of the dense phase zone
  • the feed-down feedstock in which the wet and dry sludge are dispersed from the bottom of the dense phase zone is used.
  • the specific method is as follows: dry sludge having a water content of less than 30% and wet sludge having a water content of more than 70% are respectively introduced into the bottom of the dense phase region through a plurality of inlet points; by adjusting the amount of dry and wet sludge, The temperature of the dense phase zone is controlled at 750-950 °C; the setting of the mud inlet point in the dense phase zone should ensure that the dry and wet sludge is uniformly mixed with the combustion air.
  • the volatiles will be quickly released by heat, and then quickly burned after contact with the air. Under the premise of sufficient air supply, the combustion process is completed in the dense phase zone.
  • the elevation of the mud point should be 50-200mm higher than that of the hood outlet.
  • the reason why the elevation of the mud point is selected in this interval is mainly to avoid avoiding the distance from the vent to cause the wet sludge to become dry and not agglomerate, too high. Will stay away from the dense phase area and cause insufficient combustion.
  • the dry sludge is taken from the dense phase zone by the air, and the wet sludge is squeezed.
  • the method of pressing into the dense phase zone is preferred.
  • the amount of mud entering point is directly related to whether the mixing of dry and wet sludge and combustion air is uniform, that is, whether the wet sludge per unit area can be incinted most quickly and effectively.
  • the mud is injected into each cubic meter in the dense phase zone. The point is 5 to 60, in which the wet sludge enters the mud point from 3 to 30, and the dry sludge enters the mud point from 2 to 30.
  • the amount is too small, the problem of uneven mixing may occur, the cost is high when the number is too large, and the pipe takes up too much space in the furnace.
  • the wet sludge fluidized bed incinerator comprises a furnace body, a dense phase zone with high material concentration is arranged in the furnace body, a hood air outlet is arranged at the bottom of the furnace body, and a plurality of mud inlet pipes are included, and the mud pipe is used for respectively
  • the dry sludge and the wet sludge are introduced into the bottom of the dense phase zone of the furnace body, and the dry sludge and the wet sludge are relatively uniformly mixed in the furnace, and the temperature in the dense phase zone of the furnace is 750-950 ° C;
  • the level of the mud outlet should be 50 to 200 mm higher than the hood outlet.
  • the preferred scheme is: 5 to 60 inlet pipes per cubic meter in the dense phase zone, wherein the wet sludge is 3 to 30, and the dry sludge is 2 to 30.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Treatment Of Sludge (AREA)

Abstract

一种湿污泥焚烧方法及流化床焚烧炉，主要解决了现有技术存在结构复杂，能耗高的问题。该湿污泥焚烧方法采用下饲式给料，在炉内不设置承压吸热受热面，而是将部分湿污泥（3）直接入炉焚烧，燃烧热量主要由湿污泥（3）的水分蒸发热、固体和含汽与燃烧烟的气体升温加以吸收，该方式既节省建造费用又减少需要干化的污泥数量，又避免了对全部湿污泥前续干化或压滤处理造成的高能耗。

Description

一种湿污泥焚烧方法及流化床焚烧炉 技术领域
本发明涉及一种湿污泥焚烧方法及流化床焚烧炉，特别是一种干湿污泥混烧方法以及下饲式湿、干污泥混烧流化床焚烧炉。
背景技术
目前，大多数污水处理厂经离心或真空脱水后的污泥水分含量为75-85％，而干燥基发热量仅2500-4000大卡/公斤，仅靠湿污泥燃烧提供的热量不足以维持750-900℃的炉温。
为了解决上述问题，技术人员目前大多采用入炉前，先对水分含量大于75％的污泥进行干化或压滤，以降低其水分含量。出于干化用热和保持炉内热平衡的需要，这些焚烧炉内都布置金属承压受热面，用导热油或产蒸汽吸收热量。作为这种焚烧炉燃料的污泥像一般燃煤流化床炉一样，是从密相区之上加入。
上述方式不但导致焚烧炉结构复杂，同时会增加焚烧过程产生的能耗。
发明内容
本发明提供一种湿污泥焚烧方法及流化床焚烧炉，主要解决了现有技术存在结构复杂，能耗高的问题。
本发明的具体技术解决方案如下：
该湿污泥焚烧方法，包括以下步骤：
分别将干污泥和湿污泥通过多个进泥点通入密相区底部；通过调节干湿污泥数量，使密相区温度控制在750-950℃；密相区内进泥点的设置应确保干湿污泥与助燃空气混合均匀。
优选的，进泥点标高应较风帽出风口高50～200mm。
优选的，干污泥由空气带入密相区，湿污泥挤压入密相区。
优选的，密相区内每立方米内进泥点为5～60个，其中湿污泥进泥点为3～30个，干污泥进泥点为2～30个。
该湿污泥流化床焚烧炉包括炉体，炉体内设置有物料集中度较高的密相区，炉体底部设置有风帽出风口，还包括若干个进泥管道，进泥管道用于分 别将干污泥和湿污泥通入炉体内密相区底部，且使干污泥和湿污泥在密相区内与助燃空气混合相对均匀，炉内密相区温度为750-950℃；所述进泥管道的出泥口标高应较之风帽出风口高50～200mm。
优选的，密相区每立方米内的进泥管道为5～60个，其中湿污泥进泥管道为3～30个，干污泥进泥管道为2～30个。
本发明的优点在于：
本发明提供的湿污泥焚烧方法采用下饲式给料，简化现有处理流程。
本发明提供的流化床焚烧炉在炉内不设置承压吸热受热面，而是将部分湿污泥直接入炉焚烧，燃烧热量主要由湿污泥的水分蒸发热、固体和气体(含蒸汽与燃烧烟气)升温加以吸收，该方式既节省建造费用又减少需要干化的污泥数量，又避免了全部湿污泥前续干化或压滤处理造成的高能耗。
附图说明
图1为本发明结构示意图；
附图明细如下：1-炉体；2-密相区；3-湿污泥；4-湿污泥进泥点；5-风帽出风口；6-干污泥颗粒；7-空气；8-干污泥进泥点。
具体实施方式
本发明所依据的实现的基本条件是：
满足干湿污泥在密相区，快速完成燃烧；
由于本发明提供方法及结构中湿污泥水分蒸发热、固体和气体(含蒸汽与燃烧烟气)升温吸热主要在位于炉膛底部的密相区，因此应该使燃烧放热也尽量在密相区完成，以保持密相区的热平衡，保证燃烧稳定，为此需要湿污泥与干污泥都能在密相区有足够高的燃烧份额。然而生活湿污泥属于干燥无灰基挥发份高的燃料，而且大部分在400-500℃转化为气态，实现在密相区有足够高的燃烧份额有很大难度。
干污泥由于颗粒小，比重轻，如果简单地从密相区之上加入，其挥发份的释放基本上是在密相区表面完成，在密相区的燃烧份额很小；湿污泥在加入时颗粒可能较大，而且比重大，似乎会在密相区作足够长时间的停留，但从密相区之上加入的湿污泥颗粒一旦进入密相区，就会在床内颗粒群撞击和水蒸气快速释放的共同作用下爆裂为许多小颗粒，它们漂浮在密相区表面完 成干燥和挥发份释放，其燃烧过程是在密相区之上完成，在密相区的燃烧份额同样很小。
为解决这一矛盾，提出如下要求：
1】干湿污泥分别给料
2】给料点直接选在密相区底部
3】给料点相对均匀
即：采用湿、干污泥均从密相区底部分散加入的下饲式给料。
具体采用的方法例如：分别将含水量低于30％的干污泥和含水量高于70％的湿污泥通过多个进泥点通入密相区底部；通过调节干湿污泥数量，使密相区温度控制在750-950℃；密相区内进泥点的设置应确保干湿污泥与助燃空气混合均匀。
干、湿污泥颗粒从密相区底部给入后，其挥发份将迅速受热释放，再与空气接触后快速燃烧，在空气供应充分的前提下，燃烧过程在密相区完成。
进泥点标高应较风帽出风口高50～200mm，之所以将进泥点标高选在这一区间内，主要考虑到避免距离出风口过近导致湿污泥来不及干燥而相互结团，过高会远离密相区导致燃烧不充分。
进泥方式可以选择各种，但考虑到湿污泥与干污泥在密相区的平衡问题，以及尽可能降低能耗，以采用干污泥由空气带入密相区，湿污泥挤压入密相区的方式为佳。
进泥点的数量直接关系到干湿污泥与助燃空气混合是否均匀，即单位面积内湿污泥是否能够最为快速有效的完成焚烧，结合实验情况来看，密相区内每立方米内进泥点为5～60个，其中湿污泥进泥点为3～30个，干污泥进泥点为2～30个为佳。数量过少时会导致混合不均匀的问题，数量过多时成本高，且管道在炉内占用空间过大。
具体采用的结构是：
该湿污泥流化床焚烧炉包括炉体，炉体内设置有物料集中度较高的密相区，炉体底部设置有风帽出风口，还包括若干个进泥管道，进泥管道用于分别将干污泥和湿污泥通入炉体内密相区底部，且使干污泥和湿污泥在炉内混合相对均匀，炉内密相区温度为750-950℃；所述进泥管道的出泥口标高应较 之风帽出风口高50～200mm。
同样的，优选方案是：密相区每立方米内的进泥管道为5～60个，其中湿污泥进泥管道为3～30个，干污泥进泥管道为2～30个。

Claims (6)

  1. 一种湿污泥焚烧方法，其特征在于：分别将干污泥和湿污泥多点通入密相区底部；通过调节干湿污泥数量，使密相区温度控制在750-950℃；密相区内进泥点的设置应确保干湿污泥在密相区内与助燃空气混合均匀。
  2. 根据权利要求1所述的湿污泥焚烧方法，其特征在于：所述进泥点标高应较风帽出风口高50～200mm。
  3. 根据权利要求1所述的湿污泥焚烧方法，其特征在于：所述密相区内每立方米内进泥点为5～60个，其中湿污泥进泥点为3～30个，干污泥进泥点为2～30个。
  4. 根据权利要求1至3任一所述的湿污泥焚烧方法，其特征在于：所述干污泥由空气带入密相区，湿污泥挤压入密相区。
  5. 一种湿污泥流化床焚烧炉，包括炉体，炉体内设置有物料集中度较高的密相区，炉体底部设置有风帽出风口，其特征在于：还包括若干个进泥管道，进泥管道用于分别将干污泥和湿污泥通入炉体内密相区内，且使干污泥和湿污泥在密相区内与助燃空气混合相对均匀，炉内密相区温度为750-950℃；所述进泥管道的出泥口标高应较之风帽出风口高50～200mm。
  6. 根据权利要求5所述的湿污泥流化床焚烧炉，其特征在于：密相区每立方米内的进泥管道为5～60个，其中湿污泥进泥管道为3～30个，干污泥进泥管道为2～30个。
PCT/CN2018/093378 2017-06-29 2018-06-28 一种湿污泥焚烧方法及流化床焚烧炉 WO2019001516A1 (zh)

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CN107461752A (zh) * 2017-06-29 2017-12-12 俞国豪 一种湿污泥焚烧方法及流化床焚烧炉
CN110066095A (zh) * 2018-01-19 2019-07-30 深圳市深水生态环境技术有限公司 一种市政污泥低温干化处理系统

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