CN108840544A - 一种工业污泥资源化处理方法 - Google Patents
一种工业污泥资源化处理方法 Download PDFInfo
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- CN108840544A CN108840544A CN201810845829.XA CN201810845829A CN108840544A CN 108840544 A CN108840544 A CN 108840544A CN 201810845829 A CN201810845829 A CN 201810845829A CN 108840544 A CN108840544 A CN 108840544A
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- sludge
- temperature
- reaction kettle
- hydrothermal reaction
- gas
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- 239000010802 sludge Substances 0.000 title claims abstract description 279
- 238000003672 processing method Methods 0.000 title claims abstract description 17
- 238000001027 hydrothermal synthesis Methods 0.000 claims abstract description 75
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000009272 plasma gasification Methods 0.000 claims abstract description 41
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- 238000010791 quenching Methods 0.000 claims description 32
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- 239000005416 organic matter Substances 0.000 claims description 27
- 238000002309 gasification Methods 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 24
- 239000010801 sewage sludge Substances 0.000 claims description 16
- 239000010865 sewage Substances 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicium dioxide Chemical group 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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- 230000016615 flocculation Effects 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- 239000007791 liquid phase Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound 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[Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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[P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
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[Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 1
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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
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
-
- 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
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/06—Sludge reduction, e.g. by lysis
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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
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- 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
本发明公开了一种工业污泥资源化处理方法,属于工业污泥无害化处置技术领域,包括污泥分选混合步骤、污泥输送步骤、水热反应步骤、板框压滤脱水步骤、污泥干化步骤、裂解步骤、等离子气化步骤和尾气处理步骤,是一种能有效利用污泥的热值,回收其中潜在的热能,可回收金属部分,剩余无机物熔融成玻璃体,将剩余重金属包裹其中,可作为建筑材料使用,避免了重金属进入水体的危害,基本做到污染物零排放的工业污泥资源化处理方法。
Description
一种工业污泥资源化处理方法
技术领域
[0001] 本发明属于工业污泥无害化处置技术领域,具体涉及一种工业污泥资源化处理方 法。
背景技术
[0002] 工业污泥是指污水处理站在处理工业污水过程中产生的污泥,该污泥经过絮凝脱 水后呈现半固态或固态。该污泥含水率高达70〜90%,甚至更高,一般每处理1000m3污水会产 生近5吨污泥,根据工业污水种类不同,所产生的污泥中有毒有害物质种类和量不相同,如 化工废水中有机物居多,电镀废水中重金属居多,污泥中所含有毒有害物质,如不能将其彻 底处理,污染会一直存在。因此,资源化处置工业污泥,不仅可以减少占地,而且可减轻环境 污染。
[0003] 在国家对工业污泥危害认识不透彻,对环保不重视的早期,国内外对于工业污泥 的处置,都以堆放和填埋为主,将污泥倾倒入绿化地、山坡地堆放或垃圾填埋场填埋。堆放 的方法只起到污染物转移的作用,填埋的方法也只是将污染物集中堆放,填埋后污泥发酵 释放出的恶臭和渗滤液严重威胁着周边居民的身心健康,这两种处置方法漠视了污染隐 患,严重威胁环境质量,已非受推崇处置方法。
[0004] 目前国内处理工业污泥主要有如下几种方法:发酵堆肥法,焚烧填埋法和干化焚 烧固化填埋法。
[0005] 发酵堆肥法:发酵堆肥法主要针对污水处理过程中产生的生化污泥,这类污泥中 有机质含量高,便于发酵,发酵后产生的沼气可做燃气使用,同时发酵后的残渣富含钙、镁、 磷、钾、钠等元素,是上好的热性速效有机肥料。但是该处理方式对于工业污泥的处理范围 很局限,要求污泥来源必须是有机质含量高,污染物含量低的生化污泥,要求前端分选很彻 底,否则发酵效果不佳,而且发酵残渣作为有机肥很容易带来二次污染。
[0006] 焚烧填埋法:焚烧填埋法指的是将含水率高的污泥直接或混合燃料进入焚烧炉进 行焚烧,焚烧后的残渣进入填埋场进行填埋,如现有技术中公开为CN1270988C的中国发明 公开了一种污泥焚烧处理方法,该方法是将含水率为75%〜85%的脱水污泥输送至循环流化 床的燃烧室中,将脱水污泥在贮藏过程中产生的污染气体送入循环流化床的燃烧室中,脱 水污泥、污染气体与煤一起焚烧,焚烧产生的尾气经处理后排放,焚烧后的残渣进入垃圾填 埋场进行填埋。该方法在污泥减量上起到了立竿见影的效果,但是焚烧过程能耗高,同时焚 烧产生尾气,尤其是中高温条件下产生的二噁英排入大气,严重影响周边居民的身心健康, 同时焚烧残渣中含有重金属等有毒有害物质,进入填埋场带来二次污染。
[0007] 焚烧固化填埋法:焚烧固化填埋法与焚烧填埋法的区别在于,污泥经过焚烧后,残 渣混合水泥进行固化,经固化后进入填埋场进行填埋,该方法同样存在二噁英污染大气的 问题,同时固化后的残渣短期内能控制重金属进入地下水,但是若干年水泥的固化能力失 效后,重金属将再次进入地下水影响周边环境。
发明内容
[0008] 本发明的目的在于提供一种能有效利用污泥的热值,回收其中潜在的热能,可回 收金属部分,剩余无机物熔融成玻璃体,将剩余重金属包裹其中,可作为建筑材料使用,避 免了重金属进入水体的危害,基本做到污染物零排放的工业污泥资源化处理方法。
[0009] 本发明的目的是通过以下技术方案实现的: 一种工业污泥资源化处理方法,其特征在于,包括以下步骤: 污泥分选混合步骤:将待处理工业污泥按照物化污泥和生化污泥的分类分别送入污泥 分选机去除其中的杂质,如包装物、石块、铁片等物质,同时为方便后续污泥输送和提高水 热反应处理效率,根据工业污泥来源和种类不同,在分选过程中将物化污泥和生化污泥按 照1: (1〜5)的质量比进行充分混合; 污泥输送步骤:将经过污泥分选混合步骤后的工业污泥通过输送栗送至水热反应器, 污泥输送装置除输送功能外,还可根据要求控制输送量; 水热反应步骤:工业污泥进入水热反应器后,通过导热油对污泥进行加热使温度达90〜 160°C,将反应器内压力升高至0.9〜1.2MPa,在此温度和压力下保压至少2.0小时,使得污泥 中细胞水破壁而出转变为游离水,方便后续污泥中水分的脱除,同时破坏污泥原有的絮凝 作用,污泥流动性增强。处理过程中采用多级错峰生产模式,回收泄压过程中释放的热能, 为下一批待处理污泥进行预热。
[0010] 板框压滤脱水步骤:经水热反应步骤后的污泥中水主要以游离水的形式存在,流 动性好,在温度60〜90°C条件下通过泵输送至板框压滤机中进行脱水,将污泥含水率降低至 40〜60%,脱水过程能耗低。脱出的水进入污水处理站处理后达标排放; 污泥干化步骤:经板框压滤脱水步骤后的污泥趁热进入污泥干燥机,通过180〜20(TC的 导热油为干燥机提供热能,将污泥中剩余水进一步脱除,将污泥含水率降低至15〜30%。
[0011] 裂解步骤:将经过污泥干化步骤的污泥送入裂解机中,在600〜800°C条件下裂解15 〜30min;干化后的污泥含水率低,有机质含量高达60%左右,控制裂解机进料速度,使得污泥 在裂解机中600-800°C条件下停留时间为15-30min,污泥中有机质充分裂解为小分子有机 物,以可燃气的形式存在。
[0012] 等离子气化步骤:向经过裂解步骤的污泥中均匀混合添加剂后送入等离子气化 炉,在1200〜1600°C温度下通入空气进行气化处理,根据裂解步骤后的污泥残渣中无机物含 量添加添加剂,如污泥:添加剂的质量比=100: (10〜25)。在1200〜1600°C温度下,通入少量 空气将污泥中剩余有机质(包括其中有毒有害的有机物)瞬间气化为氢气、甲烷、一氧化碳 等高热值可燃气,无机物和添加剂在高温下熔融形成玻璃体,根据金属和无机物在熔融状 态下密度的不同将污泥中金属汇集收集,作为产品,其他熔融态无机物将污泥中原有有害 物质(如重金属)包裹在玻璃体中,玻璃体从出料口流出进入淬冷池淬冷,淬冷后的玻璃体 可作为建筑材料使用。
[0013] 尾气处理步骤:将等离子气化步骤产生的气体温度保持在850°C以上送入烟气管 道中,向烟气管道中喷入氨水对气体进行脱硝处理,然后对尾气进行急冷处理,将尾气温度 在Is内从850°C降低至20(TC以内,避开了二噁英的生成温度,防止了二噁英的再次生成,经 过急冷处理后的气体再经过除尘、除臭和脱硫处理达标后排放。
[0014] 所述水热反应步骤中,是通过两个并联且可相互独立运行的水热反应釜A和水热 反应釜B进行的,在水热反应釜A运行时,水热反应釜B停止运行,在水热反应釜A进入泄压环 节前,往水热反应釜B中加入待处理污泥,水热反应釜A泄压释放的热蒸汽进入水热反应釜 B,对水热反应釜B的污泥进行加热,同理,之后水热反应釜B泄压释放的热蒸汽对水热反应 釜A的污泥进行加热,如此往复。形成错峰生产模式,采用错峰生产的目的是回收热能,降低 处理能耗,达到热能利用最大化。
[0015] 所述等离子气化步骤中,污泥和添加剂的混合比例为污泥:添加剂的质量比=1〇〇: (10〜25) 〇
[0016] 所述添加剂为硅藻土:B203:AL203=20: (5〜10) : (1〜3)质量比配置而成的均匀粉 末,其中硅藻土、B2〇3和AL2〇3粒度均在30目以上。添加剂的主要作用是协助污泥中无机物形 成网络结构,快速形成流动性较好的玻璃体将重金属包裹在其中,同时降低无机物熔点,降 低处理能耗,也降低了气化炉的制作难度。一般情况下按照污泥:添加剂=100: (1〇_25)的质 量比进行添加,即可降低处置温度近150 °C,并且形成玻璃体流动性好。
[0017] 所述等离子气化步骤,是等离子气化炉中的等离子枪在高压下放电引弧产生的热 能升温至1200〜160(TC,对等离子气化炉中经过所述污泥预处理步骤混合了添加剂的污泥 进行加气化;通过等离子枪为气化炉供热,能将炉内温度升高并稳定在1600°C左右,局部火 焰温度甚至能达3000°C之高,可分解任何有机物,在该温度下,原处理物料中带入的二噁英 瞬间分解,同时避开了二噁英的再次生成温度。
[0018] 所述裂解步骤和等离子气化步骤中还包括热能回用过程,将裂解气化和等离子气 化过程中产生的可燃气通过管道输送至燃气炉中通入氧气进行燃烧,燃烧产生的热能回用 于加热导热油,加热后的导热油用于前端污泥水热反应和干化。
[0019] 所述氧气的通入量为可燃气的10倍。
[0020] 本技术方案的有益效果如下: 本发明中,待处理工业污泥经过污泥分选和混合后,将其中的杂质分选出,并将生化污 泥和物化污泥按一定比例混合均匀,混合均匀的污泥通过污泥输送装置,输送至水热反应 器进行处理,水热反应后的污泥由板框压滤进行脱水,脱出的污水经污水处理后,达标排 放,脱水后的污泥进入污泥干化机后进行污泥干化处理,进一步干化后的污泥进入裂解机 后进行裂解,裂解残渣混入一定比例的添加剂进入等离子炉进行等离子气化处理,在气化 炉高温条件下无机物熔融,根据密度不同汇集分出污泥中金属产品,剩余无机物在高温环 境下产生的玻璃体产品可作为建材使用;裂解和等离子气化过程中产生的可燃气进行燃烧 处理,燃烧过程产生的热能进行热能回用,回用热能用于前端污泥干化处理,尾气部分经过 急冷处理后避免了二噁英的产生,尾气中粉尘、硫化物和氮氧化物经过尾气处理后达标排 放。
[0021] 经过分选和充分混合将其中的杂质去除,同时确保待处理污泥中水分和有机物的 相对稳定,一方面减小了处置过程中对设备的损伤,另一方面保证了处置工况相对稳定,确 保了设备24h连续安全稳定运行;分选混合后的污泥通过水热反应模式进行预处理,将污泥 中难脱除的细胞水转变为游离水,然后再以板框压滤这种机械的方式脱水,相比高温加热 方式脱水,大大降低了处置能耗;并且处置过程中采取错峰生产方式,能回收泄压过程中释 放的热能,进一步降低了处置能耗;干化后的污泥在缺氧高温条件下进行裂解,产生低分子 可燃气,混合气化产生的可燃气一起燃烧加热导热油,回收热能,用于則顺污泥预处理和干 化,降低了外加能耗的使用量;气化过程在12〇〇°C以上进行,配合尾气急冷处理工艺,一方 面将原有二噁英分解,避开了二噁英的生成温度,防止了二噁英的再次生成。气化炉中高温 条件下配合添加剂,回收其中金属部分,剩余无机物熔融成玻璃体,将重金属等有害物质包 裹其中,淬冷后的玻璃体作为建筑材料使用,真正做到污染物零排放。
[0022] 总体来说本处置方法经济环保,避免了二噁英等二次污染,同时将工业污泥处置 后回用于建筑行业,解决了堆放问题。真正做到了工业污泥资源化利用。
附图说明
[0023] 本发明的前述和下文具体描述在结合以下附图阅读时变得更清楚,附图中: 图1是本发明处理方法一种优选方案的流程示意图。
具体实施方式
[0024]下面通过几个具体的实施例来进一步说明实现本发明目的技术方案,需要说明的 是,本发明要求保护的技术方案包括但不限于以下实施例。
[0025] 实施例1 作为本发明一种最基本的实施方案,公开了一种工业污泥资源化处理方法,如图1,包 括以下步骤: 污泥分选混合步骤:将待处理工业污泥按照物化污泥和生化污泥的分类分别送入污泥 分选机去除其中的杂质,如包装物、石块、铁片等物质,同时为方便后续污泥输送和提高水 热反应处理效率,根据工业污泥来源和种类不同,在分选过程中将物化污泥和生化污泥按 照1: (1〜5)的质量比进行充分混合; 污泥输送步骤:将经过污泥分选混合步骤后的工业污泥通过输送泵送至水热反应器, 污泥输送装置除输送功能外,还可根据要求控制输送量; 水热反应步骤:工业污泥进入水热反应器后,通过导热油对污泥进行加热使温度达90〜 160°C,将反应器内压力升高至0.9〜1.2MPa,在此温度和压力下保压至少2.0小时,使得污泥 中细胞水破壁而出转变为游离水,方便后续污泥中水分的脱除,同时破坏污泥原有的絮凝 作用,污泥流动性增强。处理过程中采用多级错峰生产模式,回收泄压过程中释放的热能, 为下一批待处理污泥进行预热。
[0026] 板框压滤脱水步骤:经水热反应步骤后的污泥中水主要以游离水的形式存在,流 动性好,在温度60〜90°C条件下通过栗输送至板框压滤机中进行脱水,将污泥含水率降低至 40〜60%,脱水过程能耗低。脱出的水进入污水处理站处理后达标排放; 污泥干化步骤:经板框压滤脱水步骤后的污泥趁热进入污泥干燥机,通过180〜200°C的 导热油为干燥机提供热能,将污泥中剩余水进一步脱除,将污泥含水率降低至15〜30%。
[0027]裂解步骤:将经过污泥干化步骤的污泥送入裂解机中,在600〜80(TC条件下裂解15 〜30min;干化后的污泥含水率低,有机质含量高达60%左右,控制裂解机进料速度,使得污泥 在裂解机中6〇〇-SOO°C条件下停留时间为15-30min,污泥中有机质充分裂解为小分子有机 物,以可燃气的形式存在。
[0028]等离子气化步骤:向经过裂解步骤的污泥中均匀混合添加剂后送入等离子气化 炉,在12〇〇〜l6〇0°C温度下通入空气进行气化处理。在1200〜l6〇0°C温度下,通入少量空气将 污泥中剩余有机质(包括其中有毒有害的有机物)瞬间气化为氢气、甲烷、一氧化碳等高热 值可燃气,无机物和添加剂在高温下熔融形成玻璃体,根据金属和无机物在熔融状态下密 度的不同将污泥中金属汇集收集,作为产品,其他熔融态无机物将污泥中原有有害物质(如 重金属)包裹在玻璃体中,玻璃体从出料口流出进入淬冷池淬冷,淬冷后的玻璃体可作为建 筑材料使用。
[0029] 尾气处理步骤:将等离子气化步骤产生的气体温度保持在850°C以上送入烟气管 道中,向烟气管道中喷入氨水对气体进行脱硝处理,然后对尾气进行急冷处理,将尾气温度 在1 s内从85(TC降低至200°C以内,避开了二噁英的生成温度,防止了二噁英的再次生成,经 过急冷处理后的气体再经过除尘、除臭和脱硫处理达标后排放。
[0030] 待处理工业污泥经过污泥分选和混合后,将其中的杂质分选出,并将生化污泥和 物化污泥按一定比例混合均匀,混合均匀的污泥通过污泥输送装置,输送至水热反应器进 行处理,水热反应后的污泥由板框压滤进行脱水,脱出的污水经污水处理后,达标排放,脱 水后的污泥进入污泥干化机后进行污泥干化处理,进一步干化后的污泥进入裂解机后进行 裂解,裂解残渣混入一定比例的添加剂进入等离子炉进行等离子气化处理,在气化炉高温 条件下无机物熔融,根据密度不同汇集分出污泥中金属产品,剩余无机物在高温环境下产 生的玻璃体产品可作为建材使用;裂解和等离子气化过程中产生的可燃气进行燃烧处理, 燃烧过程产生的热能进行热能回用,回用热能用于前端污泥干化处理,尾气部分经过急冷 处理后避免了二噁英的产生,尾气中粉尘、硫化物和氮氧化物经过尾气处理后达标排放。
[0031] 经过分选和充分混合将其中的杂质去除,同时确保待处理污泥中水分和有机物的 相对稳定,一方面减小了处置过程中对设备的损伤,另一方面保证了处置工况相对稳定,确 保了设备24h连续安全稳定运行;分选混合后的污泥通过水热反应模式进行预处理,将污泥 中难脱除的细胞水转变为游离水,然后再以板框压滤这种机械的方式脱水,相比高温加热 方式脱水,大大降低了处置能耗;并且处置过程中采取错峰生产方式,能回收泄压过程中释 放的热能,进一步降低了处置能耗;干化后的污泥在缺氧高温条件下进行裂解,产生低分子 可燃气,混合气化产生的可燃气一起燃烧加热导热油,回收热能,用于前端污泥预处理和千 化,降低了外加能耗的使用量;气化过程在1200°C以上进行,配合尾气急冷处理工艺,一方 面将原有二噁英分解,避开了二噁英的生成温度,防止了二噁英的再次生成。气化炉中高温 条件下配合添加剂,回收其中金属部分,剩余无机物熔融成玻璃体,将重金属等有害物质包 裹其中,淬冷后的玻璃体作为建筑材料使用,真正做到污染物零排放。
[0032]总体来说本处置方法经济环保,避免了二噁英等二次污染,同时将工业污泥处置 后回用于建筑行业,解决了堆放问题。真正做到了工业污泥资源化利用 实施例2 作作为本发明方法一种优选地实施方案,公开了一种工业污泥资源化处理方法,如图 1,包括以下步骤: 污泥分选混合步骤:将待处理工业污泥按照物化污泥和生化污泥的分类分别送入污泥 分选机去除其中的杂质,如包装物、石块、铁片等物质,同时为方便后续污泥输送和提高水 热反应处理效率,根据工业污泥来源和种类不同,在分选过程中将物化污泥和生化污泥按 照1: (1〜5)的质量比进行充分混合; 污泥输送步骤:将经过污泥分选混合步骤后的工业污泥通过输送泵送至水热反应器, 污泥输送装置除输送功能外,还可根据要求控制输送量; 水热反应步骤:工业污泥进入水热反应器后,通过导热油对污泥进行加热使温度达90〜 160°C,将反应器内压力升高至〇 • 9〜1 • 2MPa,在此温度和压力下保压至少2 • 0小时,使得污泥 中细胞水破壁而出转变为游离水,方便后续污泥中水分的脱除,同时破坏污泥原有的絮凝 作用,污泥流动性增强。是通过两个并联且可相互独立运行的水热反应釜A和水热反应釜B 进行的,在水热反应爸A运行时,水热反应IIB停止运行,在水热反应|gA进入泄压环节前,往 水热反应釜B中加入待处理污泥,水热反应釜A泄压释放的热蒸汽进入水热反应釜B,对水热 反应釜B的污泥进行加热,同理,之后水热反应釜B泄压释放的热蒸汽对水热反应釜A的污泥 进行加热,如此往复。形成错峰生产模式,采用错峰生产的目的是回收热能,降低处理能耗, 达到热能利用最大化。
[0033] 板框压滤脱水步骤:经水热反应步骤后的污泥中水主要以游离水的形式存在,流 动性好,在温度60〜9(TC条件下通过泵输送至板框压滤机中进行脱水,将污泥含水率降低至 40〜60%,脱水过程能耗低。脱出的水进入污水处理站处理后达标排放; 污泥干化步骤:经板框压滤脱水步骤后的污泥趁热进入污泥干燥机,通过180〜200°C的 导热油为干燥机提供热能,将污泥中剩余水进一步脱除,将污泥含水率降低至15〜30%。
[0034] 裂解步骤:将经过污泥干化步骤的污泥送入裂解机中,在600〜800°C条件下裂解15 〜30min;干化后的污泥含水率低,有机质含量高达60%左右,控制裂解机进料速度,使得污泥 在裂解机中600-800°C条件下停留时间为15-30min,污泥中有机质充分裂解为小分子有机 物,以可燃气的形式存在。
[0035] 等离子气化步骤:按照污泥:添加剂的质量比=100: (10〜25)的比例向经过裂解步 骤的污泥中均匀混合添加剂后送入等离子气化炉,在1200〜1600°C温度下通入空气进行气 化处理。所述添加剂为硅藻土:B2〇3:AL2〇3=20: (5〜10) : (1〜3)质量比配置而成的均匀粉 末,其中硅藻土、B203和AL2〇3粒度均在30目以上。添加剂的主要作用是协助污泥中无机物形 成网络结构,快速形成流动性较好的玻璃体将重金属包裹在其中,同时降低无机物熔点,降 低处理能耗,也降低了气化炉的制作难度。一般情况下按照污泥:添加剂=100: (10-25)的质 量比进行添加,即可降低处置温度近150°C,并且形成玻璃体流动性好;等离子气化炉中的 等离子枪在高压下放电引弧产生的热能升温至1200〜1600°C,对等离子气化炉中经过所述 污泥预处理步骤混合了添加剂的污泥进行加气化;通过等离子枪为气化炉供热,能将炉内 温度升高并稳定在1600°C左右,局部火焰温度甚至能达3000°C之高,可分解任何有机物,在 该温度下,原处理物料中带入的二噁英瞬间分解,同时避开了二噁英的再次生成温度在 12〇0〜1600°C温度下,通入少量空气将污泥中剩余有机质(包括其中有毒有害的有机物)瞬 间气化为氢气、甲烷、一氧化碳等高热值可燃气,无机物和添加剂在高温下熔融形成玻璃 体,根据金属和无机物在熔融状态下密度的不同将污泥中金属汇集收集,作为产品,其他熔 融态无机物将污泥中原有有害物质(如重金属)包裹在玻璃体中,玻璃体从出料口流出进入 淬冷池淬冷,淬冷后的玻璃体可作为建筑材料使用。
[0036]尾气处理步骤:将等离子气化步骤产生的气体温度保持在85(TC以上送入烟气管 道中,向烟气管道中喷入氨水对气体进行脱硝处理,然后对尾气进行急冷处理,将尾气温度 在Is内从85〇°C降低至20(TC以内,避开了二噁英的生成温度,防止了二噁英的再次生成,经 过急冷处理后的气体再经过除尘、除臭和脱硫处理达标后排放。
[0037] 所述裂解步骤和等离子气化步骤中还包括热能回用过程,将裂解气化和等离子气 化过程中产生的可燃气通过管道输送至燃气炉中通入氧气进行燃烧,所述氧气的通入量为 可燃气的10倍,燃烧产生的热能回用于加热导热油,加热后的导热油用于前端污泥水热反 应和干化。
[0038] 实施例3 作为本发明一种优选地实施方案,公开了一种工业污泥资源化处理方法,如图i,包括 以下步骤: 1、污泥分选和混合步骤:将待处理工业污泥送入污泥分选机进行分选,去除其中的杂 质,如包装物、石块、铁片等物质。同时为方便后续污泥输送和提高水热反应处理效率,根据 工业污泥来源和种类不同,在分选过程中将物化污泥和生化污泥按照1:(1〜5)的质量比进 行充分混合。
[0039] 2、污泥输送步骤:经分选和混合均匀后的污泥通过输送泵送至水热反应器,污泥 输送装置除输送功能外,还可根据要求控制输送量。
[0040] 3、水热反应步骤:工业污泥进入水热反应器后,通过导热油对污泥进行加热,将反 应器内压力升高至0 • 9_1 • 2MPa,此时温度达l6〇-l9〇°C间,在此温度和压力下保压2.0小时, 使得污泥中细胞水破壁而出转变为游离水,方便后续污泥中水分的脱除,同时破坏污泥原 有的絮凝作用,污泥流动性增强。处理过程中采用多级错峰生产模式,回收泄压过程中释放 的热能,为下一批待处理污泥进行预热。
[0041] 4、板框压滤脱水步骤:经水热反应处理后的污泥中水主要以游离水的形式存在, 流动性好,在温度60-90°C条件下通过泵输送至板框压滤机中进行高效脱水,可将含水率 80%以上的污泥降低至50%左右,脱水过程能耗低。脱出的水进入污水处理站处理后达标排 放。
[0042] 5、污泥千化步骤:脱水后的污泥趁热进入污泥干燥机,通过180-20(TC温度导热油 为千燥机提供热能,将污泥中剩余水进一步脱除,干化后污泥含水率降低至15-30%。
[0043] 6、裂解步骤:干化后的污泥含水率低,有机质含量高达60%左右,控制裂解机进料 速度,使得污泥在裂解机中600-800°C条件下停留时间为15-30min,污泥中有机质充分裂解 为小分子有机物,以可燃气的形式存在。
[0044] 7、等离子气化步骤:裂解残渣根据其中无机物含量添加添加剂,混合均匀后送入 等离子气化炉进行气化处理。在1200-160(TC温度下,通入少量空气将污泥中剩余有机质 (包括其中有毒有害的有机物)瞬间气化为氢气、甲烷、一氧化碳等高热值可燃气,无机物和 添加剂在高温下熔融形成玻璃体,根据金属和无机物在熔融状态下密度的不同将污泥中金 属汇集收集,作为产品,其他熔融态无机物将污泥中原有有害物质(如重金属)包裹在玻璃 体中,玻璃体从出料口流出进入淬冷池淬冷,淬冷后的玻璃体可作为建筑材料使用。
[0045]添加剂作用:添加剂的主要作用是协助污泥中无机物形成网络结构,快速形成流 动性较好的玻璃体将重金属包裹在其中,同时降低无机物熔点,降低处理能耗,也降低了气 化炉的制作难度。一般情况下按照污泥:添加剂=100: (10-25)的质量比进行添加,即可降低 处置温度近150°C,并且形成玻璃体流动性好。添加剂为硅藻土:B203:AL203=20: (5〜10): (1〜3)质量比配置而成的均匀粉末,其中硅藻土、B203和AL203粒度均要求在30目以上。
[0046]等离子气化处理的好处:通过等离子枪为气化炉供热,能将炉内温度升高并稳定 在1600°C左右,局部火焰温度甚至能达3000°C之高,可分解任何有机物,在该温度下,原处 理物料中带入的二噁英瞬间分解,同时避开了二噁英的再次生成温度。
[0047] 8、热能回用步骤:裂解气化和等离子气化过程中产生的可燃气通过管道输送至燃 气炉中按比例通入氧气进行燃烧,燃烧产生的热能回用于加热导热油,加热后的导热油用 于前端污泥水热反应和干化。
[0048] 9、尾气处理步骤:可燃气燃烧并回用热能后,控制气体温度高于85(TC,在此温度 下往烟气管道中喷入氨水进行脱硝处理,之后对尾气进行急冷处理,将尾气温度在Is内从 850°C降低至200°C以内,避开了二噁英的生成温度,防止了二噁英的再次生成,急冷后的气 体经过除尘、除臭和脱硫等一系列处理后达标排放。
[0049] 其中,裂解步骤中具体包括干化步骤,将污泥通过干燥机进行脱水,使污泥中的含 水率在30%以内;裂解步骤,将经过千化步骤的污泥匀速投加进入裂解系统中,并在在600〜 800°C温度下,至少裂解30min;可燃气燃烧步骤,将裂解步骤中产生的可燃气输送至燃烧室 内,并与氧气混合后在燃烧室内进行燃烧处理;尾气处理步骤,将可燃气燃烧步骤产生的尾 气进行脱硫、脱硝、除尘和除重金属处理至达标后排放。常规污泥处理方法和本技术最接近 的为焚烧处置工艺,焚烧处置工艺为在富氧条件下在90(TC左右温度条件下,将污泥中有机 物彻底燃烧,虽然污泥减量大,但是需要补充热源,污泥中的资源并未得到利用,而本技术 中将裂解条件控制在600〜800 °C的缺氧环境,虽然减量效果不如焚烧,但是可回用污泥中潜 在热能,实现了减量化和资源化的目标,能有效利用污泥的热值,回收其中潜在的热能 等离子气化步骤中具体包括污泥预处理步骤、等离子气化步骤、燃气处理步骤和尾气 处理步骤;所述污泥预处理步骤,脱水后的理污是泥通过污泥投入装置均匀投加进入等离 子气化炉中的,污泥投入等离子气化炉的同时通过添加剂投入装置按比例匀速向污泥中投 加添加剂,污泥和添加剂在投加过程中混合均匀,所述污泥和添加剂的混合比例为污泥:添 加剂的质量比=100: (10〜25),所述添加剂为硅藻土、B2〇3、AL2〇3按照20: (5〜10) : (1〜3)质 量比配置而成的均匀粉末,且硅藻土、B2〇3和AL2O3粒度均在3〇目以上。添加剂的主要作用是 协助污泥中无机物形成网络结构,快速形成流动性较好的玻璃体将重金属包裹在其中,同 时降低无机物熔点,降低处理能耗,也降低了气化炉的制作难度。一般情况下按照污泥:添 加剂=100: (10〜25)的质量比进行添加,即可降低处置温度近150°C,并且形成玻璃体流动 性好。添加剂为桂藻土:B2〇3:AL2〇3=20: (5〜10) : (1〜3)质量比配置而成的均勾粉末,其中 硅藻土、B2〇3和AL2〇3粒度均要求在3〇目以上。所述等离子气化步骤,等离子气化炉中的等离 子枪在高压下放电引弧产生的热能升温至1200〜l6〇0°C,对等离子气化炉中经过所述污泥 预处理步骤混合了添加剂的污泥进行加气化;在1200-1600 °C温度下,通入少量空气将污泥 中剩余有机质(包括其中有毒有害的有机物)瞬间气化为氢气、甲烷、一氧化碳等高热值可 燃气,无机物和添加剂在高温下熔融形成玻璃体,通过密度控制将处理后留下的金属和生 成的玻璃体分别收集处理;根据金属和无机物在熔融状态下密度的不同将污泥中金属汇集 收集,作为产品,其他熔融态无机物将污泥中原有有害物质(如重金属)包裹在玻璃体中,玻 璃体从出料口流出进入淬冷池淬冷,淬冷后的玻璃体可作为建筑材料使用,所述玻璃体生 成后从等离子气化炉的出料口流出进入淬冷池淬冷。所述可燃气处理步骤,是对所述等离 子气化步骤中产生的可燃气体通入氧气并进行燃烧处理;所述尾气处理步骤,是对所述可 燃气处理步骤中产生的尾气在急冷系统中喷入冷却水进行冷却后,尾气的温度降低至200 °c以内,然后经除尘装置、除臭装置和脱硫装置处理排放,在急冷系统中喷入冷却水使得尾 气在Is内温度降低至20(TC以内,避开了二噁英的生成温度,防止了二噁英的再次生成。 [0050] 板框压滤脱水步骤具体包括输送步骤、水热反应步骤、尾气处理步骤、压滤处理步 骤和废水处理步骤,工业污泥经过输送步骤进入水热反应系统的水热反应釜中进行水热反 应步骤,水热反应步骤生成的气项进入尾气处理步骤、剩下的固液相则依次进行压滤处理 步骤和废水处理步骤;所述水热反应步骤包括升温升压过程、保温保压过程和泄压过程;所 述升温升压过程,当进入水热反应釜中污泥量达到额定容积的1/2到3/4时,水热反应釜夹 套中开水加热升温,加热升温过程中不断对污泥进行搅拌,当水热反应釜内蒸汽压力达 0.7Mpa以上、物料温度升高至160〜190°C时进入所述保温保压过程;所述保温保压过程,控 制反应釜内物料温度在160〜190 °C范围内并保持120〜180min;使得污泥中细胞壁破裂,污泥 中细胞水和结合水转化为游离。所述泄压过程,保温保压过程结束后,通过泄压阀将高温蒸 汽释放,将反应釜内压力泄压至0.1〜0.2Mpa范围内时停止泄压。所述泄压过程,保温保压过 程结束后,通过泄压阀将高温蒸汽释放,将反应釜内压力泄压至0.1〜0.2Mpa范围内时停止 泄压。所述输送步骤,通过螺杆泵将与添加剂混合均匀的工业污泥匀速输送至水热反应釜。 所述添加剂与工业污泥是按照(2〜5) : 100的质量比进行混合的。所述保温保压过程是通过 控制导热油的循环量实现对反应釜内温度的控制的。所述泄压过程结束后,是通过放料管 道将水热反应釜内的污泥输送最后暂存槽进行暂存,等待进行尾气处理步骤、压滤处理步 骤和废水处理步骤的。所述水热反应步骤中,是通过两个并联且可相互独立运行的水热反 应釜A和水热反应釜B进行的,在水热反应釜A运行时,水热反应釜B停止运行,在水热反应釜 A进入泄压环节前,往水热反应釜B中加入待处理污泥,水热反应签A泄压释放的热蒸汽进入 水热反应釜B,对水热反应釜B的污泥进行加热,同理,之后水热反应釜B泄压释放的热蒸汽 对水热反应釜A的污泥进行加热,如此往复。形成错峰生产模式,采用错峰生产的目的是回 收热能,降低处理能耗,达到热能利用最大化。所述尾气处理步骤,是泄压过程和通过放料 管道将水热反应釜内的污泥输送至暂存槽的过程中释放的部分不凝气和水蒸气经暂存槽 后进入尾气处理系统,将其中的水蒸气和不凝气进行吸附处理,处理后达标排放。所述压滤 处理步骤,暂存槽中污泥温度降低至70〜95°C范围内后,通过栗抽至压滤机中进行脱水处 理,压滤压力控制在0.4〜0.65Mpa范围内。压滤后污泥含水率降低至50%左右。所述废水处理 步骤是将压滤产生的废水进入污水处理系统处理后达标排放。
Claims (7)
1.一种工业污泥资源化处理方法,其特征在于,包括以下步骤: 污泥分选混合步骤:将待处理工业污泥按照物化污泥和生化污泥的分类分别送入污泥 分选机去除其中的杂质,在分选过程中将物化污泥和生化污泥按照1: (1〜5)的质量比进行 充分混合; 污泥输送步骤:将经过污泥分选混合步骤后的工业污泥通过输送栗送至水热反应器; 水热反应步骤:工业污泥进入水热反应器后,通过导热油对污泥进行加热使温度达90〜 l6〇°C,将反应器内压力升高至0 • 9〜1 • 2MPa,在此温度和压力下保压至少2.0小时; 板框压滤脱水步骤:经水热反应步骤后的污泥,在温度60〜90°C条件下通过栗输送至板 框压滤机中进行脱水,将污泥含水率降低至40〜60%,脱出的水进入污水处理站处理后达标 排放; 污泥千化步骤:经板框压滤脱水步骤后的污泥趁热进入污泥千燥机,通过180〜20(TC的 导热油为干燥机提供热能,将污泥中剩余水进一步脱除,将污泥含水率降低至15〜30%; 裂解步骤:将经过污泥干化步骤的污泥送入裂解机中,在600〜800°C条件下裂解15〜 30min; 等离子气化步骤:向经过裂解步骤的污泥中均匀混合添加剂后送入等离子气化炉,在 1200〜1600°C温度下通入空气进行气化处理; 尾气处理步骤:将等离子气化步骤产生的气体温度保持在850°C以上送入烟气管道中, 向烟气管道中喷入氨水对气体进行脱硝处理,然后对尾气进行急冷处理,将尾气温度在Is 内从850°C降低至200°C以内,经过急冷处理后的气体再经过除尘、除臭和脱硫处理达标后 排放。
2. 如权利要求1所述的一种工业污泥资源化处理方法,其特征在于:所述水热反应步骤 中,是通过两个并联且可相互独立运行的水热反应釜A和水热反应釜B进行的,在水热反应 釜A运行时,水热反应釜B停止运行,在水热反应爸A进入泄压环节前,往水热反应釜B中加入 待处理污泥,水热反应爸A泄压释放的热蒸汽进入水热反应釜B,对水热反应釜B的污泥进行 加热,同理,之后水热反应釜B泄压释放的热蒸汽对水热反应釜A的污泥进行加热,如此往 复。
3. 如权利要求1所述的一种工业污泥资源化处理方法,其特征在于:所述等离子气化步 骤中,污泥和添加剂的混合比例为污泥:添加剂的质量比=100: (10〜25)。
4. 如权利要求1或3所述的一种工业污泥资源化处理方法,其特征在于:所述添加剂为 硅藻土:B2〇3:AL2〇3=20: (5〜10) : (1〜3)质量比配置而成的均匀粉末,其中硅藻土、Bs〇3和 AL2O3粒度均在30目以上。
5. 如权利要求1所述的一种工业污泥资源化处理方法,其特征在于:所述等离子气化步 骤,是等离子气化炉中的等离子枪在高压下放电引弧产生的热能升温至I200〜1600 °C,对 等离子气化炉中经过所述污泥预处理步骤混合了添加剂的污泥进行加气化;通过等离子枪 为气化炉供热,能将炉内温度升高并稳定在woo r左右,局部火焰温度甚至能达3〇〇〇 之 高,可分解任何有机物,在该温度下,原处理物料中带入的二噁英瞬间分解,同时避开了二 噁英的再次生成温度。 +
6. 如权利要求1所述的一种工业污泥资源化处理方法,其特征在于:所述裂解步骤和等 离子气化步骤中还包括热能回用过程,将裂解气化和等离子气化过程中产生的可燃气通过 管道输送至燃气炉中通入氧气进行燃烧,燃烧产生的热能回用于加热导热油,加热后的导 热油用于前端污泥水热反应和干化。
7.如权利要求6所述的一种工业污泥资源化处理方法,其特征在于:所述氧气的通入量 为可燃气的10倍。
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