WO2020034279A1 - 吸附水体中有机物的吸附剂的原位脱附再生工艺 - Google Patents

吸附水体中有机物的吸附剂的原位脱附再生工艺 Download PDF

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WO2020034279A1
WO2020034279A1 PCT/CN2018/104376 CN2018104376W WO2020034279A1 WO 2020034279 A1 WO2020034279 A1 WO 2020034279A1 CN 2018104376 W CN2018104376 W CN 2018104376W WO 2020034279 A1 WO2020034279 A1 WO 2020034279A1
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adsorbent
temperature
stage
tank
water
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French (fr)
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茆林凤
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无锡四方集团有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
    • B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
    • B01J20/3466—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase with steam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • 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
    • C02F2303/16—Regeneration of sorbents, filters

Definitions

  • the invention relates to an in-situ desorption regeneration process of an adsorbent that adsorbs organic substances in a water body, in particular to a desorption regeneration process of an activated carbon adsorbent (activated carbon, activated coke, zeolite, etc.).
  • an activated carbon adsorbent activated carbon, activated coke, zeolite, etc.
  • the process for the advanced treatment of tap water, domestic sewage, and industrial sewage is widely used for the adsorption of organic matter by disposable adsorbents (such as activated carbon, activated coke, zeolite, etc.).
  • disposable adsorbents such as activated carbon, activated coke, zeolite, etc.
  • the adsorbed saturated adsorbent is usually treated as a hazardous waste and must be entrusted to a qualified hazardous waste disposal unit for disposal.
  • a large amount of disposal costs, and replacement and transportation are cumbersome and difficult to operate. Therefore, the regeneration and reuse of the adsorbent is an urgently needed technology in the application of the adsorbent market.
  • the effective regeneration technology of adsorbents uses a high-temperature furnace regeneration process, specifically using high temperature to crack and carbonize organics on the surface of the adsorbent, such as [a regenerative activated carbon activation furnace CN105858652].
  • the yield of adsorbent materials such as activated carbon is about 60% -70%, and the adsorption performance is deteriorated after regeneration. That is to say, the adsorption materials such as activated carbon and the like are recycled for a maximum of 3 to 4 times, and the adsorption materials still need to be replaced for a certain period of time.
  • the object of the present invention is to overcome the deficiencies in the prior art, and to provide an in-situ desorption regeneration process for an adsorbent that adsorbs organic matter in a water body, and can realize an online in-situ desorption regeneration of an adsorbent for waste adsorption in a water body , Has a good desorption regeneration effect.
  • the in-situ desorption regeneration process of the adsorbent that adsorbs organic substances in a water body includes the following processes:
  • the first stage remove most of the remaining water in the carbon layer: after the adsorbent in the adsorbent tank is saturated with adsorption, stop the raw water from passing into the adsorbent tank. After no residual water in the adsorbent tank flows out, blow it with compressed air for a certain time;
  • the temperature of the adsorbent in the adsorbent tank is changed from normal temperature. Heating to a certain set temperature in the range of 200 ° C to 800 ° C (this specific temperature set value is determined according to the characteristics of the treated organic matter, there are two cases of cracking requirements or just desorption and not cracking, there are cracking If required, set the temperature value according to the specific cracking temperature of the object to be treated, and set the desorption temperature only for desorption without cracking), and set the pressure condition below 2 bar;
  • the third stage high temperature insulation, high temperature desorption or high temperature cracking carbonization desorption stage: the temperature of the adsorbent in the adsorbent tank reaches a certain set temperature in the range of 200 ° C to 800 ° C (this specific temperature set value is based on To determine the characteristics of the treated organic matter, there are two cases of cracking requirements or just desorption and not cracking. In the case of cracking requirements, the temperature value is set according to the specific cracking temperature of the object to be treated. Set the desorption temperature in the case), keep heating for 0.5 ⁇ 8 hours, most of the organic matter is desorbed by high temperature or carbonized and desorbed by high temperature cracking;
  • the fourth stage purge, activation regeneration, cooling stage: after high temperature insulation, purge with superheated steam below 200 °C, the steam pressure at this stage is set to 0.1 ⁇ 2.0Bar, purge time is 0.2-3.0 hours Then, stop the steam inlet, close the steam inlet valve, and cool naturally.
  • the amount of steam inflow from the second stage to the fourth stage is 0.2-1.5 times of the adsorbed dose in the adsorbent tank.
  • the discharged residual organic matter is collected and then treated by the photo-oxidation device and discharged to the standard or returned to the standby carbon tank for re-adsorption; the liquid or water-soluble part is collected by the condensation device and passed through ozone.
  • the oxidizing device discharges after treatment or returns to the sewage treatment device to continue processing.
  • the volatile gas is processed by the demister and then connected to the exhaust gas treatment tank for adsorption; the condensed wastewater is connected to a sewage treatment plant for processing.
  • the holding temperature of the adsorbent in the adsorbent tank is a certain set temperature in the range of 200 ° C to 800 ° C (this specific temperature setting value is determined according to the characteristics of the organic substance to be treated, and there is a cracking requirement or There are only two cases of desorption and not cracking. If there is a request for cracking, the temperature value is set according to the specific cracking temperature of the object to be treated. 12 hours.
  • an organic substance dissolved in water is adsorbed by an adsorbent. After the adsorbent is saturated, the adsorbent is desorbed and regenerated in situ. The superheated water vapor at 200 ° C to 1000 ° C is used to enter the adsorbent tank to make the adsorbent. Most of the adsorbed organic matter is desorbed or desorbed by high temperature cracking and carbonization; and the remaining organic matter and carbides in the adsorbent are purged and removed to activate and regenerate the adsorbent.
  • FIG. 1 is a schematic diagram of an in-situ desorption regeneration process of an adsorbent that adsorbs organic matter in a water body.
  • this embodiment is a desorption regeneration system for adsorbent adsorbed by organic waste in wastewater.
  • the activated carbon adsorbent includes a first adsorbent tank A, a second adsorbent tank B, a third adsorbent tank C, and The fourth adsorbent tank D, the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, and the fourth adsorbent tank D are respectively connected to the pretreatment tank 22 through the pump body 21, and the pretreatment tank 22 Connected to the waste water collection tank 23, a first valve 24 is provided on a pipe at the raw water inlet end of the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, and the fourth adsorbent tank D, and by controlling the first The valve 24 can realize the adsorption of activated carbon in the first adsorbent tank A, the second adsorbent tank B, the third a
  • the superheated steam pipe 25 and the reheater 26 are connected respectively, so as to suck the first adsorbent tank A, the second adsorbent tank B, and the third adsorbent tank.
  • Superheated steam is passed through the agent tank C and the fourth adsorbent tank D, and the superheated steam at the inlet end of the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, and the fourth adsorbent tank D is superheated.
  • a second valve 26 is provided on the steam pipe 25; the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, and the fourth adsorbent tank D also pass through the residue pipe 27 and the condensation device 28, respectively.
  • the inlet end is connected, and the output end of the condensing device 28 is connected to the condensed wastewater collection tank 23 and connected to the sewage treatment plant.
  • a backwash pipeline 30 is provided between the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, and the fourth adsorbent tank D and the qualified pool 29.
  • an exhaust gas treatment device may be further provided between the first adsorbent tank A, the second adsorbent tank B, the third adsorbent tank C, the fourth adsorbent tank D, and the condensation device 28, and the entire desorption regeneration process In the gas-water mixture, the volatile gas is connected to the tail gas device after being processed by the demister.
  • Embodiment 2 An in-situ desorption regeneration process for an adsorbent that adsorbs organic matter in water, and the activated carbon adsorbent includes the following specific processes:
  • the first stage remove most of the remaining water in the carbon layer: after the activated carbon in the adsorbent tank is saturated, stop the raw water from passing into the adsorbent tank, and blow out the compressed air with compressed air for a certain period of time;
  • the second stage the third stage: high-temperature insulation, high-temperature desorption or high-temperature cracking carbonization desorption stage: the activated carbon bed temperature in the adsorbent tank reaches a certain set temperature in the range of 200 ° C to 800 ° C (this specific temperature
  • the set value is determined according to the characteristics of the processed organic matter. There are two cases of cracking requirements or just desorption and not cracking. In the case of cracking requirements, the temperature value is set according to the specific cracking temperature of the processed object. Set the desorption temperature if the desorption does not decompose.) As shown in Table 1, continuous heating and holding for 0.5 to 12 hours, most of the organic matter is desorbed by high temperature or carbonized and desorbed by high temperature cracking;
  • the fourth stage purge, activation regeneration, cooling stage: after high temperature insulation, purge with superheated steam below 200 °C, the steam pressure at this stage is set to 0.1 ⁇ 2.0Bar, purge time is 0.2-3.0 hours Then, stop the steam inlet, close the steam inlet valve, and cool naturally.
  • the gas-water mixture in the whole desorption regeneration process, the volatile gas is treated by the demister and connected to the tail gas treatment device; the condensed wastewater is connected to the sewage treatment plant for treatment.
  • Table 3 shows the adsorption performance of the activated carbon adsorbent after the regeneration was performed 10 times in the manner of Example 2.

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  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
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Abstract

一种吸附水体中有机物的吸附剂的原位脱附再生工艺，包括以下过程：第一阶段：排掉炭层内大部分余水：吸附剂罐（A、B、C、D）内的吸附剂吸附饱和后，停止原水通进吸附剂罐（A、B、C、D），吸附剂罐（A、B、C、D）内没有余水流出后用压缩空气吹一定时间；第二阶段：升温加热挥发阶段：启动过热蒸汽发生器，过热蒸汽快速升温，在线原位对吸附剂罐（A、B、C、D）内的吸附剂加热；第三阶段：吸附剂罐（A、B、C、D）内的吸附剂保温，绝大部分有机物被高温脱附或者被高温裂解碳化并脱附；第四阶段：经高温保温后，改变过热蒸汽的温度进行吹扫，而后停止蒸汽的通入，关闭蒸汽进口阀，自然冷却。该方法能够实现用于水体中有机物吸附的吸附剂的在线原位脱附再生，具有良好的脱附再生效果。

Description

吸附水体中有机物的吸附剂的原位脱附再生工艺 技术领域
本发明涉及一种吸附水体中有机物的吸附剂的原位脱附再生工艺，尤其是一种活性炭吸附剂(活性炭、活性焦、沸石等等)的脱附再生工艺。
背景技术
目前，用于自来水、生活污水及工业污水深度处理环节广泛应用一次性吸附剂(如活性炭、活性焦、沸石等等)吸附有机物的工艺。吸附剂吸附饱和后需更换新的吸附材料，且吸附饱和后的吸附剂通常被作为危废需委托有资质的危废处置单位进行处置或委托有再生资质的企业进行再生处理后重复利用，需要一大笔的处置费用，而且更换和运输都是比较繁琐不容易操作。所以吸附剂的再生重复利用是当今吸附剂市场应用方面急需的技术。
当前，有效的吸附剂(如活性炭、活性焦、沸石等等)的再生技术采用高温炉再生工艺，具体为利用高温将吸附剂表面的有机物裂解碳化，如[一种再生活性炭活化炉CN105858652]。该工艺活性炭等吸附材料收率约为60％-70％，并且再生后吸附性能变差。即采用该工艺活性炭等吸附材料最多循环使用3～4次，仍需要一定时期进行更换吸附材料。
发明内容
本发明的目的是克服现有技术中存在的不足，提供一种吸附水体中有机物的吸附剂的原位脱附再生工艺，能够实现用于水体中废物吸附的吸附剂的在线原位脱附再生，具有良好的脱附再生效果。
按照本发明提供的技术方案，所述吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是，包括以下过程：
第一阶段：排掉炭层内大部分余水：吸附剂罐内的吸附剂吸附饱和后，停止原水通进吸附剂罐，吸附剂罐内没有余水流出后用压缩空气吹一定时间；
第二阶段：升温加热挥发阶段：启动过热蒸汽发生器，过热水蒸气快速升温至200～1000℃，在线原位对吸附剂罐内的吸附剂加热，吸附剂罐内吸附剂温度从常温被加热升温至200℃～800℃范围间的某一个设定温度(这个具体的温度设定值是根据被处理有机物的特性来确定，有裂解要求或者只需脱附不要裂解两种情况，有裂解要求的情况就按照被处理对象的特定的裂解温度来设定温度值，只需脱附不要裂解的情况就设定脱附温度)，设定压力条件为2bar以下；
第三阶段：高温保温、高温脱附或高温裂解碳化脱附阶段：吸附剂罐内的吸附剂温度达到200℃～800℃范围间的某一个设定温度(这个具体的温度设定值是根据被处理有机物的特性来确定，有裂解要求或者只需脱附不要裂解两种情况，有裂解要求的情况就按照被处理对象的特定的裂解温度来设定温度值，只需脱附不要裂解的情况就设定脱附温度)，持续加热保温0.5～8小时，绝大部分有机物被高温脱附或者被高温裂解碳化并脱附；
第四阶段：吹扫、活化再生、冷却阶段：经高温保温后，用低于200℃的过热蒸汽进行吹扫，此阶段蒸汽压力设定在0.1～2.0Bar，吹扫时间为0.2-3.0小时，而后停止蒸汽的通入，关闭蒸汽进口阀，自然冷却。
进一步地，所述第二阶段至第四阶段的蒸汽通入量为吸附剂罐中吸附剂量的0.2-1.5倍。
进一步地，整个过程中，排出的残留有机物，经收集后经过光氧化装置处理后达标排放或者用管道送回到备用碳罐再次吸附；呈液态或溶于水的部分经冷凝装置收集并经过臭氧氧化装置处理后排放或者回到污水处理装置继续进行处理。
进一步地，整个脱附再生过程中的气水混合物，挥发性气体经除雾机处理后接入尾气处理罐吸附；冷凝废水接入污水处理厂进行处理。
进一步地，所述吸附剂罐内的吸附剂保温温度为200℃～800℃范围间的某一个设定温度(这个具体的温度设定值是根据被处理有机物的特性来确定，有裂解要求或者只需脱附不要裂解两种情况，有裂解要求的情况就按照被处理对象的特定的裂解温度来设定温度值，只需脱附不要裂解的情况就设定脱附温度)，保温0.5～12小时。
本发明通过吸附剂吸附溶于水体中的有机物，待吸附剂吸附饱和以后，原位进行吸附剂脱附再生过程，利用200℃～1000℃的过热水蒸气进入到吸附剂罐，使吸附剂吸附的大部分的有机物被脱附或者被高温裂解碳化脱附；并吹扫去除吸附剂中残留有机物和碳化物，使吸附剂活化再生。
附图标记说明
图1为吸附水体中有机物的吸附剂的原位脱附再生工艺的示意图。
具体实施方式
下面结合具体实施例对本发明作进一步说明。
实施例1：
如图1所示，本实施例为废水中有机废物吸附的吸附剂的脱附再生系统针对活性炭吸附剂，包括第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D，第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D分别通过泵体21与预处理池22连接，预处理池22与废水收集池23连接，在第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D原水进口端的管道上设置第一阀24，通过控制第一阀24能够实现第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四活性炭罐D中活性炭的吸附；所述第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D的输出端连接合格水池29；所述第一吸附剂罐A、第二吸附剂罐B、第三活性炭罐C和第四吸附剂罐D分别由过热蒸汽管道25与再加热器26连接，从而向第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D中通入过热蒸汽，在第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D的过热蒸汽进口端的过热蒸汽管道25上设置第二阀26；所述第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D还分别通过残留 物管道27与冷凝装置28的进口端连接，冷凝装置28的输出端再连接至冷凝废水收集池23，接入污水处理厂。
在所述第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D和合格水池29之间设置反冲洗管道30。
另外，在所述第一吸附剂罐A、第二吸附剂罐B、第三吸附剂罐C和第四吸附剂罐D与冷凝装置28之间还可以设置尾气处理装置，整个脱附再生过程中的气水混合物，挥发性气体经除雾机处理后接入尾气处装置。
实施例2：一种吸附水体中有机物的吸附剂的原位脱附再生工艺，针对活性炭吸附剂，包括以下具体过程：
第一阶段：排掉炭层内大部分余水：吸附剂罐内的活性炭吸附饱和后，停止原水通进吸附剂罐，碳罐内没有余水流出后用压缩空气吹一定时间；
第二阶段：升温加热挥发阶段：启动过热蒸汽发生器，过热水蒸气快速升温至200～1000℃，在线原位对吸附剂罐内的活性炭加热，吸附剂罐内活性炭炭床温度从常温被加热升温至200℃～800℃范围间的某一个设定温度(这个具体的温度设定值是根据被处理有机物的特性来确定，有裂解要求或者只需脱附不要裂解两种情况，有裂解要求的情况就按照被处理对象的特定的裂解温度来设定温度值，只需脱附不要裂解的情况就设定脱附温度)，设定压力条件为2bar以下；
第二阶段：第三阶段：高温保温、高温脱附或高温裂解碳化脱附阶段：吸附剂罐内的活性炭炭床温度达到200℃～800℃范围间的某一个设定温度(这个具体的温度设定值是根据被处理有机物的特性来确定，有裂解要求或者只需脱附不要裂解两种情况，有裂解要求的情况就按照被处理对象的特定的裂解温度来设定温度值，只需脱附不要裂解的情况就设定脱附温度)，具体如表1所示，持续加热保温0.5～12小时，绝大部分有机物被高温脱附或者被高温裂解碳化并脱附；
表1
Figure PCTCN2018104376-appb-000001
第四阶段：吹扫、活化再生、冷却阶段：经高温保温后，用低于200℃的过热蒸汽进行吹扫，此阶段蒸汽压力设定在0.1～2.0Bar，吹扫时间为0.2-3.0小时，而后停止蒸汽的通入，关闭蒸汽进口阀，自然冷却。
整个脱附再生过程中的气水混合物，挥发性气体经除雾机处理后接入尾气 处理装置；冷凝废水接入污水处理厂进行处理。
经实施例2的方式进行10次再生后的活性炭吸附剂吸附性能表3所示。
表3
Figure PCTCN2018104376-appb-000002

Claims (5)

  1. 一种吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是，包括以下过程：
    第一阶段：排掉炭层内大部分余水：吸附剂罐内的吸附剂吸附饱和后，停止原水通进吸附剂罐，吸附剂罐内没有余水流出后用压缩空气吹一定时间；
    第二阶段：升温加热挥发阶段：启动过热蒸汽发生器，过热水蒸气快速升温至200～1000℃，在线原位对吸附剂罐内的吸附剂加热，吸附剂罐内吸附剂温度从常温被加热升温至200℃～800℃范围间的某一个设定温度，设定压力条件为2bar以下；
    第三阶段：高温保温、高温脱附或高温裂解、碳化脱附阶段：吸附剂罐内的吸附剂温度达到200℃～800℃范围间的一个设定温度，持续加热保温0.5～8小时，绝大部分有机物被高温脱附或者被高温裂解、碳化并脱附；
    第四阶段：吹扫、活化再生、冷却阶段：经高温保温后，用低于200℃的过热蒸汽进行吹扫，此阶段蒸汽压力设定在0.1～2.0Bar，吹扫时间为0.2-3.0小时，而后停止蒸汽的通入，关闭蒸汽进口阀，自然冷却。
  2. 如权利要求1所述的吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是：所述第二阶段至第四阶段的蒸汽通入量为吸附剂罐中吸附剂量的0.2-1.5倍。
  3. 如权利要求1所述吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是：整个过程中，排出的残留有机物，经收集后经过光氧化装置处理后达标排放或者用管道送回到备用碳罐再次吸附；呈液态或溶于水的部分经冷凝装置收集并经过臭氧氧化装置处理后排放或者回到污水处理装置继续进行处理。
  4. 如权利要求1所述吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是：整个脱附再生过程中的气水混合物，挥发性气体经除雾机处理后接入尾气处理罐吸附；冷凝废水接入污水处理厂进行处理。
  5. 如权利要求1所述的吸附水体中有机物的吸附剂的原位脱附再生工艺，其特征是：所述吸附剂罐内的吸附剂保温温度为200℃～800℃范围间的一个设定温度，保温0.5～12小时；该设定温度根据被处理有机物的特性确定，有裂解要求的情况按照被处理有机物的裂解温度来设定温度值，只需脱附不要裂解的情况设定脱附温度。
PCT/CN2018/104376 2018-08-16 2018-09-06 吸附水体中有机物的吸附剂的原位脱附再生工艺 WO2020034279A1 (zh)

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