WO2020093583A1 - 吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺 - Google Patents

吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺 Download PDF

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WO2020093583A1
WO2020093583A1 PCT/CN2019/070293 CN2019070293W WO2020093583A1 WO 2020093583 A1 WO2020093583 A1 WO 2020093583A1 CN 2019070293 W CN2019070293 W CN 2019070293W WO 2020093583 A1 WO2020093583 A1 WO 2020093583A1
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adsorbent
regeneration
exhaust gas
gas treatment
regeneration tank
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PCT/CN2019/070293
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English (en)
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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Priority claimed from CN201811311879.6A external-priority patent/CN109482165A/zh
Priority claimed from CN201821822244.8U external-priority patent/CN209968418U/zh
Application filed by 无锡四方集团有限公司 filed Critical 无锡四方集团有限公司
Publication of WO2020093583A1 publication Critical patent/WO2020093583A1/zh

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    • 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
    • B01D53/02—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 by adsorption, e.g. preparative gas chromatography
    • 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

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  • the invention relates to the field of desorption regeneration, in particular to an adsorbent (including activated carbon, activated coke, zeolite, etc.) that adsorbs organic matter dissolved in water after adsorption saturation and a desorption regeneration process, as well as a tail gas treatment process generated during the desorption regeneration process .
  • an adsorbent including activated carbon, activated coke, zeolite, etc.
  • Activated carbon has a large specific surface area and strong adsorption capacity for various organic and inorganic substances, so it is widely used in the adsorption and purification treatment of various exhaust gases and wastewater, and the separation treatment of some mixtures, such as hydrocarbons Adsorption and purification of exhaust gas, adsorption and purification of sulfur-containing compound exhaust gas, and adsorption purification of oily sewage, etc.
  • the activated carbon needs to be regenerated after being saturated with adsorption.
  • vacuum regeneration that is, the material adsorbed in the pores of activated carbon is desorbed under vacuum conditions
  • steam regeneration that is, the substance adsorbed in the pores of activated carbon is steam Desorption.
  • the steam regeneration process it is generally necessary to reduce the temperature of the activated carbon bed to a certain degree, and then use air to dry. Direct air drying at high temperature is prone to safety accidents, and the toxic and harmful gases generated after activated carbon regeneration are directly released into the environment Will cause pollution to the environment.
  • the invention provides the desorption regeneration of the adsorbent for adsorbing the organic matter in the water body and the tail gas treatment process, so as to solve the problems of the prior art that the adsorbent regeneration has poor effect, poor safety, and poor tail gas treatment.
  • the present invention provides a desorption regeneration of an adsorbent that adsorbs organic matter in water and its tail gas treatment process, including a steam injection system, a regeneration tank, and an exhaust gas treatment system.
  • the steam injection system includes a superheated steam generator, a main Steam pipes, secondary steam pipes and nozzles.
  • an accommodation space provided in the regeneration tank and a number of secondary steam pipes are provided in the accommodation space, and one end of the secondary steam pipe is connected to the superheated steam generator through the main steam pipe And the nozzle is provided at the other end, an exhaust gas outlet and a compressed air inlet are provided on the regeneration tank, and the compressed air inlet is located at an upper part of the regeneration tank, and the exhaust gas outlet is connected to an exhaust gas treatment system through an exhaust gas pipe.
  • the desorption regeneration of the adsorbent adsorbing the organic matter in the water body and its tail gas treatment process include the following steps:
  • the compressed air is passed through the compressed air inlet to remove all the water inside the adsorbent
  • the heating and volatilization stage, the compressed air inlet and the drain outlet are closed, the valves on the main steam pipe and the exhaust gas pipe are opened, the superheated steam generator is started to pass the superheated steam into the regeneration tank, and the exhaust gas pipe is connected to the exhaust gas treatment system
  • the pressure in the regeneration tank is maintained at 0.1 ⁇ 2bar, and the temperature in the regeneration tank is in the range of 200 °C ⁇ 800 °C, which can be set as required;
  • the third step the heat preservation stage, when the temperature in the regeneration tank reaches the set temperature, it is necessary to continuously pass superheated steam for heat preservation, and the heat preservation time is more than 0.5 hours;
  • the fourth step is the low temperature purge phase. After the heat preservation phase is completed, the temperature in the regeneration tank is adjusted to 100 to 200 ° C, the pressure in the regeneration tank is maintained at 0.1 to 2 bar, and the low temperature purge time is 0.2 to 3 hours.
  • the time for the compressed air to pass in the first step is 0.25 to 2 hours.
  • the temperature in the regeneration tank in the second step is 250 ° C, 340 ° C, 380 ° C, 400 ° C, 450 ° C, 600 ° C, 800 ° C.
  • the holding time in the third step is 0.5 to 24 hours.
  • the time of the low-temperature purge stage in the fourth step is 0.2 to 3 hours.
  • the adsorbent includes activated carbon, activated coke, and zeolite.
  • the present invention provides a desorption regeneration of adsorbent that adsorbs organic matter in water and its exhaust gas treatment equipment.
  • a steam injection system By installing a steam injection system, a regeneration tank, and an exhaust gas treatment system, the desorption is regenerated in the regeneration tank
  • the temperature and pressure are strictly controlled to improve the efficiency and safety of the adsorbent desorption regeneration.
  • the desorption regeneration of the adsorbent that adsorbs the organic matter in the water body and its tail gas treatment process first remove all the moisture inside the adsorbent, and then heat up and heat and volatilize, then heat up at a high temperature, heat up at high temperature, or decompose at high temperature, and desorb at carbonization.
  • the low-temperature purge process has a small amount of carbides and residual organics that are continuously purged and brought out of the activated carbon pores by the superheated steam, so that the adsorbent is activated and regenerated.
  • the temperature value of the adsorbent desorption regeneration is determined according to the characteristics of the organic matter to be processed. There are two situations where there is a cracking requirement or only desorption and no cracking. If there is a cracking requirement, it is set according to the specific cracking temperature of the processed object For the temperature value, set the desorption temperature only when desorption does not crack.
  • FIG. 1 is a schematic diagram of the overall structure of an adsorbent desorption regeneration process and a desorption regeneration tail gas treatment process according to the first embodiment of the present invention.
  • FIG. 2 is a schematic diagram of the overall structure of an adsorbent desorption regeneration process and a desorption regeneration tail gas treatment process according to a second embodiment of the present invention.
  • FIG. 3 is a schematic diagram of the overall structure of an adsorbent desorption regeneration process and a desorption regeneration tail gas treatment process according to a third embodiment of the present invention.
  • 101-superheated steam generator 102-main steam pipeline, 103-secondary steam pipeline, 2-regeneration tank, 3-condensation pipe, 301-cooling water inlet, 302-cooling water outlet, 4-condensation water collection tank , 5-water pump, 6-combustion chamber, 7-droplet separator, 8-sink, 9-fire arrester.
  • the present invention provides a desorption regeneration of adsorbent that adsorbs organic matter in water and its exhaust gas treatment equipment includes a steam injection system, a regeneration tank 2, and an exhaust gas treatment system.
  • the steam injection system includes a superheated steam generator 101, a main steam pipe 102, a secondary steam pipe 103, and a nozzle, an accommodating space provided in the regeneration tank 2 and a number of secondary A steam pipe 103, one end of the secondary steam pipe 103 is connected to the superheated steam generator 101 through the main steam pipe 102 and the nozzle is provided at the other end, and the exhaust gas outlet and The compressed air inlet is located at the upper part of the regeneration tank 2, and the exhaust gas outlet is connected to an exhaust gas treatment system through an exhaust gas pipe.
  • the secondary steam pipe 103 has a tree structure.
  • the regeneration tank 2 includes a tank body and a tank lid. The tank lid is tightly closed above the tank body. The bottom end of the regeneration tank 2 is provided with a drainage outlet. The regeneration tank 2 is provided in the accommodation space There are temperature sensors and pressure sensors. Valves are provided on the main steam pipe 102 and the exhaust gas pipe.
  • the tail gas condensation treatment can be used for the crackable carbonized tail gas.
  • the exhaust gas treatment system includes a condenser pipe 3 and a condensate collection tank 4.
  • the exhaust gas outlet of the regeneration tank 2 is connected to the inlet of the condenser pipe 3 through an exhaust gas pipe, and the outlet of the condenser pipe 3 is connected to the condensate water In the collecting tank 4, cooling water inlet 301 and cooling water outlet 302 are respectively provided at both ends of the condenser tube 3.
  • This embodiment provides a desorption regeneration of an adsorbent that adsorbs organic matter in water and its tail gas treatment process, including the following steps:
  • the compressed air is introduced into the compressed air to remove all the moisture inside the adsorbent, and the compressed air is passed for 0.25 to 2 hours.
  • the heating and volatilization stage close the compressed air inlet and drain outlet, open the valves on the main steam pipe and the exhaust gas pipe, start the superheated steam generator 101, and the superheated steam quickly heats up to the set temperature of 200 ⁇ 1000 °C
  • the steam injection system pre-buried in the regeneration tank enters the regeneration tank and heats the adsorbent in the regeneration tank.
  • the exhaust gas pipeline leads to the exhaust gas treatment system, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the temperature in the regeneration tank 2 is in the range of 200 ° C to 800 ° C, which can be set as required.
  • This specific set temperature value is determined according to the characteristics of the organic matter to be processed. If there is a cracking requirement, the temperature value is set according to the specific cracking temperature of the processed object.
  • the special temperature is 380 °C, 400 °C, 600 ⁇ 800 °C, 380 °C can crack to remove the carbon-containing dry distillation contained in the adsorbent, 400 °C can crack to remove the organic compounds of CO and CN bond contained in the adsorbent, 400 ⁇ 800 °C can carbonize and remove the carbon compounds contained in the adsorbent.
  • the third step the heat preservation stage, when the temperature in the regeneration tank 2 reaches the set temperature, it is necessary to continuously pass hot steam for heat preservation, the heat preservation time is more than 0.5 hours, and the special heat preservation time is 1 hour.
  • the fourth step is the low temperature purge stage.
  • the temperature in the regeneration tank 2 is adjusted to 100 to 200 ° C, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the low temperature purge time is 0.2 to 3 hours
  • the time for the special low-temperature purge stage is 0.2 to 3 hours.
  • a small part of the carbides and residual organics are swept out of the activated carbon pores by the continuously entering superheated steam, so that the adsorbent is activated and regenerated. After purging, close the main steam pipe and let it cool naturally.
  • the adsorbent includes activated carbon, activated coke, and zeolite.
  • the present invention provides a desorption regeneration of adsorbent that adsorbs organic matter in water and its exhaust gas treatment equipment includes a steam injection system, a regeneration tank 2, and an exhaust gas treatment system.
  • the steam injection system includes superheated steam generation 101, main steam pipe 102, secondary steam pipe 103 and nozzle.
  • an accommodating space provided in the regeneration tank 2 and a plurality of secondary steam pipes 103 are provided in the accommodating space, and one end of the secondary steam pipe 103 is connected to the superheat through the main steam pipe 102
  • the steam generator 101 is provided with the nozzle at the other end, an exhaust gas outlet and a compressed air inlet are provided on the regeneration tank 2 and the compressed air inlet is located at an upper portion of the regeneration tank 2, the exhaust gas outlet passes through an exhaust gas pipeline Connected to the exhaust gas treatment system.
  • the secondary steam pipe 103 has a tree structure.
  • the regeneration tank 2 includes a tank body and a tank lid. The tank lid is tightly closed above the tank body. The bottom end of the regeneration tank 2 is provided with a drainage outlet. The regeneration tank 2 is provided in the accommodation space There are temperature sensors and pressure sensors. Valves are provided on the main steam pipe 102 and the exhaust gas pipe.
  • the tail gas is directly incinerated, which can be used to desorb the tail gas without cracking.
  • the tail gas treatment system includes tail gas incineration treatment equipment, the tail gas incineration treatment equipment includes a water droplet separator 7, a flame arrester, a water tank 8 and a combustion chamber 6, the gas output end of the water droplet separator 7 and the input of the flame arrester End, the liquid output end of the droplet separator 7 is connected to the water tank 8, the water tank 8 communicates with the water inlet of the combustion chamber 6, and the output end of the flame arrester is connected to the inlet of the combustion chamber 6 At the gas end, the exhaust gas outlet of the regeneration tank 2 is connected to the water droplet separator 7 through an exhaust gas pipeline, and air and LNG enter the combustion chamber 6 through the air inlet and the LNG inlet, respectively, and the top of the combustion chamber 6 is provided. There is a chimney.
  • This embodiment provides a desorption regeneration of an adsorbent that adsorbs organic matter in water and its tail gas treatment process, including the following steps:
  • the compressed air is introduced into the compressed air to remove all the moisture inside the adsorbent, and the compressed air is passed for 0.25 to 2 hours.
  • the heating and volatilization stage close the compressed air inlet and drain outlet, open the valves on the main steam pipe and the exhaust gas pipe, start the superheated steam generator 101, and the superheated steam quickly heats up to the set temperature of 200 ⁇ 1000 °C
  • the steam injection system pre-buried in the regeneration tank enters the regeneration tank and heats the adsorbent in the regeneration tank.
  • the exhaust gas pipeline leads to the exhaust gas treatment system, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the temperature in the regeneration tank 2 is in the range of 200 ° C to 800 ° C, which can be set as required.
  • the specific set temperature value is determined according to the characteristics of the organic matter to be processed. There are two situations where there is a cracking requirement or only desorption and no cracking. If there is a cracking requirement, the temperature is set according to the specific cracking temperature of the processed object Value, set the desorption temperature as long as desorption does not crack.
  • 250 °C and 340 °C can remove small molecule inorganic substances such as oxygen, sulfur, CO 2 and hour 2 S contained in adsorbent. Organic matter.
  • the third step the heat preservation stage, when the temperature in the regeneration tank 2 reaches the set temperature, it is necessary to continuously pass hot steam for heat preservation, and the heat preservation time is more than 0.5 hours.
  • the fourth step is the low temperature purge stage.
  • the temperature in the regeneration tank 2 is adjusted to 100 to 200 ° C, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the low temperature purge time is 0.2 to 3 hours
  • the time for the special low-temperature purge stage is 0.2 to 3 hours.
  • a small part of the carbides and residual organics are swept out of the activated carbon pores by the continuously entering superheated steam, so that the adsorbent is activated and regenerated. After purging, close the main steam pipe and let it cool naturally.
  • the adsorbent includes activated carbon, activated coke, and zeolite.
  • the present invention provides a desorption regeneration of an adsorbent that adsorbs organic matter in water and its exhaust gas treatment equipment includes a steam injection system, a regeneration tank 2, and an exhaust gas treatment system.
  • the steam injection system includes superheated steam generation 101, main steam pipe 102, secondary steam pipe 103 and nozzle.
  • an accommodating space provided in the regeneration tank 2 and a plurality of secondary steam pipes 103 are provided in the accommodating space, and one end of the secondary steam pipe 103 is connected to the superheat through the main steam pipe 102
  • the steam generator 101 is provided with the nozzle at the other end, an exhaust gas outlet and a compressed air inlet are provided on the regeneration tank 2 and the compressed air inlet is located at an upper portion of the regeneration tank 2, the exhaust gas outlet passes through an exhaust gas pipeline Connected to the exhaust gas treatment system.
  • the secondary steam pipe 103 has a tree structure.
  • the regeneration tank 2 includes a tank body and a tank lid. The tank lid is tightly closed above the tank body. The bottom end of the regeneration tank 2 is provided with a drainage outlet. The regeneration tank 2 is provided in the accommodation space There are temperature sensors and pressure sensors. Valves are provided on the main steam pipe 102 and the exhaust gas pipe.
  • the exhaust gas is first condensed and then incinerated.
  • the exhaust gas treatment system includes a condenser pipe 3, a condensed water collection tank 4, a water pump 5, a vaporization device, and an exhaust gas incineration treatment device.
  • the vaporization device is provided in the condensed water collection
  • the tail gas incineration processing equipment includes a water droplet separator 7, a flame arrester, a water tank 8 and a combustion chamber 6, the gas output end of the water droplet separator 7 and the flame arrester The input end is connected, the liquid output end of the water droplet separator 7 is connected to the water tank 8, the water tank 8 communicates with the water inlet end of the combustion chamber 6, and the output end of the flame arrester is connected to the combustion chamber 6
  • the exhaust gas outlet of the regeneration tank 2 is connected to the inlet of the condensing pipe 3 through an exhaust gas pipe, and the outlet of the condensing pipe 3 is connected to the condensate collecting tank
  • the condensed water in the condensed water collecting tank 4 is sent to the vaporizing device through the water pump 5 and finally enters the water droplet separator 7, and air and LNG pass through the air inlet respectively And LNG
  • the inlet enters the combustion chamber 6, and a chimney is provided on the top of the combustion chamber 6.
  • This embodiment provides a desorption regeneration of an adsorbent that adsorbs organic matter in water and its tail gas treatment process, including the following steps:
  • the compressed air is introduced into the compressed air to remove all the moisture inside the adsorbent, and the compressed air is passed for 0.25 to 2 hours.
  • the heating and volatilization stage close the compressed air inlet and drain outlet, open the valves on the main steam pipe and the exhaust pipe, start the superheated steam generator 101, and the superheated steam quickly heats up to the set temperature of 200 ⁇ 1000 °C
  • the steam injection system pre-buried in the regeneration tank enters the regeneration tank and heats the adsorbent in the regeneration tank.
  • the exhaust gas pipeline leads to the exhaust gas treatment system, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the temperature in the regeneration tank 2 is in the range of 200 ° C to 800 ° C, which can be set as required.
  • This specific set temperature value is determined according to the characteristics of the processed organic matter, and the desorption temperature can be set only when desorption does not crack.
  • the special temperature is 380 °C, 400 °C, 600 ⁇ 800 °C, 380 °C can crack to remove the carbon-containing dry distillation contained in the adsorbent, 400 °C can crack to remove the organic compounds of CO and CN bond contained in the adsorbent, 400 ⁇ 800 °C can carbonize and remove the carbon compounds contained in the adsorbent.
  • the third step the heat preservation stage, when the temperature in the regenerating tank 2 reaches the set temperature, it is necessary to continuously pass hot steam for heat preservation, the heat preservation time is more than 0.5 hours, and the special heat preservation time is 0.5 hours.
  • the fourth step is the low temperature purge stage.
  • the temperature in the regeneration tank 2 is adjusted to 100 to 200 ° C, the pressure in the regeneration tank 2 is maintained at 0.1 to 2 bar, and the low temperature purge time is 0.2 to 3 hours
  • the time for the special low-temperature purge stage is 0.2 to 3 hours.
  • a small part of the carbides and residual organics are swept out of the activated carbon pores by the continuously entering superheated steam, so that the adsorbent is activated and regenerated. After purging, close the main steam pipe and let it cool naturally.
  • the adsorbent includes activated carbon, activated coke, and zeolite.
  • the present invention provides a desorption regeneration of adsorbent that adsorbs organic matter in water and its exhaust gas treatment equipment.
  • the desorption regeneration is performed in the regeneration tank, strictly Controlling temperature and pressure improves the efficiency and safety of adsorbent desorption regeneration.
  • the desorption regeneration of the adsorbent that adsorbs the organic matter in the water body and its tail gas treatment process first remove all the moisture inside the adsorbent, and then heat up and heat and volatilize, then heat up at a high temperature, heat up at high temperature, or decompose at high temperature, and desorb at carbonization.
  • the low-temperature purge process has a small amount of carbides and residual organics that are continuously purged and brought out of the activated carbon pores by the superheated steam, so that the adsorbent is activated and regenerated.
  • the temperature value of the adsorbent desorption regeneration is determined according to the characteristics of the organic matter to be processed. There are two situations where there is a cracking requirement or only desorption and no cracking. If there is a cracking requirement, it is set according to the specific cracking temperature of the processed object For the temperature value, set the desorption temperature only when desorption does not crack.

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Abstract

一种吸附溶于水体中有机物的吸附剂(包括活性炭、活性焦、沸石等)吸附饱和后的脱附再生工艺以及脱附再生过程中产生的尾气的处理工艺。吸附剂在预埋有蒸汽喷射系统的再生罐(2)中进行脱附再生，蒸汽喷射系统包括主蒸汽管道(102)和设置于主蒸汽管道上的若干树枝状次级蒸汽管道(103)，每根次级蒸汽管道(103)均设有蒸汽喷嘴，蒸汽喷射系统被吸附剂包埋。通入过热蒸气对再生罐(2)内吸附剂加热，吸附剂所吸附的大部分有机物被高温脱附或者被高温裂解、碳化脱附，并用蒸汽吹扫去除吸附剂孔隙中有机物和碳化物，使吸附剂活化再生。再生过程中产生的尾气经尾气处理设备，具体为尾气冷凝处理设备、尾气焚烧处理设备或尾气先冷凝再焚烧处理设备进行处理。

Description

吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺 技术领域
本发明涉及一种脱附再生领域，具体涉及一种吸附溶于水中有机物的吸附剂(包括活性炭、活性焦、沸石等)吸附饱和后脱附再生工艺，以及脱附再生过程产生的尾气处理工艺。
背景技术
活性炭具有很大的比表面积，对多种有机、无机物质具有较强的吸附能力，因此广泛用于各种废气、废水的吸附净化处理工艺中，以及一些混合物的分离处理过程，如含烃类废气的吸附净化、含硫化合物废气的吸附净化、含油污水的吸附净化等。
在吸附处理工艺中，活性炭吸附饱和后需要再生处理。再生方法主要包括两种，一种是真空再生，即在真空条件下将吸附在活性炭孔道中的物质脱附出来；另一种再生方法为蒸汽再生，即用蒸汽将吸附在活性炭孔道中的物质脱附。在蒸汽再生工艺中，一般需要将活性炭床层温度降到一定程度以后，再用空气进行干燥，高温下直接用空气干燥易发生安全事故，而且活性炭再生后产生的有毒有害气体直接释放到环境中会对环境造成污染。
发明内容
本发明提供吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，以解决现有技术存在的吸附剂再生的效果差、安全性差、尾气不好处理的问题。
为解决上述技术问题，本发明提供吸附水体中有机物的吸附剂的脱附再生 及其尾气处理工艺，包括蒸汽喷射系统、再生罐、尾气处理系统，所述蒸汽喷射系统包括过热蒸汽发生器、主蒸汽管道、次级蒸汽管道和喷嘴。其中，所述再生罐内设置有的容纳空间且所述容纳空间内设置有若干的次级蒸汽管道，所述次级蒸汽管道的一端通过所述主蒸汽管道连接到所述过热蒸汽发生器上且另一端设置有所述喷嘴，所述再生罐上设置有尾气出口和压缩空气入口且所述压缩空气入口位于所述再生罐的上部，所述尾气出口通过尾气管道连接到尾气处理系统。
吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，包括以下步骤：
第一步，排水阶段，待再生罐的排水出口没有水流出后，通过压缩空气入口通入压缩空气将吸附剂内部的水份全部去除；
第二步，升温加热挥发阶段，关闭压缩空气入口和排水出口，打开主蒸汽管道和尾气管道上的阀，启动过热蒸汽发生器将过热蒸汽通入再生罐中，尾气管道通到尾气处理系统里，再生罐内的压力保持在0.1～2bar，再生罐内的温度为200℃～800℃范围，可以根据需要设置；
第三步，保温阶段，当再生罐内的温度达到设定的温度后，需要持续通入过热蒸汽进行保温，保温时间为0.5小时以上；
第四步，低温吹扫阶段，保温阶段结束后，将再生罐内的温度调整到100～200℃，再生罐内的压力保持在0.1～2bar，低温吹扫的时间为0.2～3小时。
优选的，在所述第一步中压缩空气的通入时间为0.25～2小时。
优选的，在所述第二步中再生罐内的温度为250℃、340℃、380℃、400℃、450℃、600℃、800℃。
优选的，在所述第三步中保温时间为0.5～24小时。
优选的，在所述第四步中低温吹扫阶段的时间为0.2～3小时。
优选的，所述吸附剂包括活性炭、活性焦、沸石。
本发明带来的有益效果：本发明提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备通过设置蒸汽喷射系统、再生罐、尾气处理系统，将脱附再生在再生罐进行，严格控制温度和压力，提高了吸附剂脱附再生的效率和使用安全性。在吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺中，先将吸附剂内部的水份全部去除，再升温加热挥发、再高温保温、高温脱附或高温裂解、碳化脱附，最后低温吹扫处理少部分碳化物和残留有机物被持续进入的过热水蒸气从活性炭孔隙中吹扫带出来，从而使吸附剂得到活化再生。吸附剂脱附再生的温度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。
附图说明
图1是根据本发明第一实施例的吸附剂脱附再生工艺以及脱附再生的尾气处理工艺的整体结构示意图。
图2是根据本发明第二实施例的吸附剂脱附再生工艺以及脱附再生的尾气处理工艺的整体结构示意图。
图3是根据本发明第三实施例的吸附剂脱附再生工艺以及脱附再生的尾气处理工艺的整体结构示意图。
其中，101-过热蒸汽发生器，102-主蒸汽管道，103-次级蒸汽管道，2-再生罐，3-冷凝管，301-冷却水入口，302-冷却水出口，4-冷凝水收集槽，5-水泵，6-燃烧室，7-水滴分离器，8-水槽，9-阻火器。
具体实施方式
为使本发明的目的、技术方案和优点更加清楚，以下结合附图及具体实施例，对本发明作进一步地详细说明。
第一实施例：
如图1所示，本发明提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备包括蒸汽喷射系统、再生罐2、尾气处理系统。其中，所述蒸汽喷射系统包括过热蒸汽发生器101、主蒸汽管道102、次级蒸汽管道103和喷嘴，所述再生罐2内设置有的容纳空间且所述容纳空间内设置有若干的次级蒸汽管道103，所述次级蒸汽管道103的一端通过所述主蒸汽管道102连接到所述过热蒸汽发生器101上且另一端设置有所述喷嘴，所述再生罐2上设置有尾气出口和压缩空气入口且所述压缩空气入口位于所述再生罐2的上部，所述尾气出口通过尾气管道连接到尾气处理系统。
进一步来说，所述次级蒸汽管道103为树状结构。所述再生罐2包括罐体和罐盖，所述罐盖紧密盖合在所述罐体的上方，所述再生罐2的底端设置有排水出口，所述再生罐2的容纳空间内设置有温度感应器和压力感应器。所述主蒸汽管道102和所述尾气管道上设置有阀。
在本实施例中，尾气冷凝处理，可用于可裂解碳化的尾气。所述尾气处理系统包括冷凝管3、冷凝水收集槽4，所述再生罐2的尾气出口通过尾气管道连接到所述冷凝管3的入口，所述冷凝管3的出口连接到所述冷凝水收集槽4，所述冷凝管3的两端分别设置有冷却水入口301和冷却水出口302。
本实施例提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，包括以下步骤：
第一步，排水阶段，待再生罐2的排水出口没有水流出后，通过压缩空气入口通入压缩空气将吸附剂内部的水份全部去除，压缩空气的通入时间为0.25～2小时。
第二步，升温加热挥发阶段，关闭压缩空气入口和排水出口，打开主蒸汽管道和尾气管道上的阀，启动过热蒸汽发生器101，过热水蒸气快速升温至设定温度200～1000℃，经再生罐内预埋的蒸汽喷射系统进入到再生罐内，对再生罐内吸附剂加热。尾气管道通到尾气处理系统里，再生罐2内的压力保持在0.1～2bar，再生罐2内的温度为200℃～800℃范围，可以根据需要设置。这个具体的设定温度值是根据被处理有机物的特性来确定，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。
特别的温度为380℃、400℃、600～800℃，380℃可以裂解去除吸附剂中含有的含C的干馏物，400℃可以裂解去除吸附剂中含有的C-O和C-N键的有机化合物，400～800℃可以碳化去除吸附剂中含有的含碳化合物。
第三步，保温阶段，当再生罐2内的温度达到设定的温度后，需要持续通入热蒸汽进行保温，保温时间为0.5小时以上，特别的保温时间为1小时。
第四步，低温吹扫阶段，保温阶段结束后，将再生罐2内的温度调整到100～200℃，再生罐2内的压力保持在0.1～2bar，低温吹扫的时间为0.2～3小时，特别的低温吹扫阶段的时间为0.2～3小时。少部分碳化物和残留有机物被持续进入的过热水蒸气从活性炭孔隙中吹扫带出来，从而使吸附剂得到活化再生。吹扫完成，关闭主蒸汽管道，自然冷却。
所述吸附剂包括活性炭、活性焦、沸石。
第二实施例：
如图2所示，本发明提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备包括蒸汽喷射系统、再生罐2、尾气处理系统，所述蒸汽喷射系统包括过热蒸汽发生器101、主蒸汽管道102、次级蒸汽管道103和喷嘴。其中，所述再生罐2内设置有的容纳空间且所述容纳空间内设置有若干的次级蒸汽管道103，所述次级蒸汽管道103的一端通过所述主蒸汽管道102连接到所述过热蒸汽发生器101上且另一端设置有所述喷嘴，所述再生罐2上设置有尾气出口和压缩空气入口且所述压缩空气入口位于所述再生罐2的上部，所述尾气出口通过尾气管道连接到尾气处理系统。
进一步来说，所述次级蒸汽管道103为树状结构。所述再生罐2包括罐体和罐盖，所述罐盖紧密盖合在所述罐体的上方，所述再生罐2的底端设置有排水出口，所述再生罐2的容纳空间内设置有温度感应器和压力感应器。所述主蒸汽管道102和所述尾气管道上设置有阀。
在本实施例中，尾气直接焚烧处理，可用于只需脱附不裂解的尾气。所述尾气处理系统包括尾气焚烧处理设备，所述尾气焚烧处理设备包括水滴分离器7、阻火器、水槽8和燃烧室6，所述水滴分离器7的气体输出端与所述阻火器的输入端连接，所述水滴分离器7的液体输出端与所述水槽8连接，所述水槽8与所述燃烧室6的进水端连通，所述阻火器的输出端连接到燃烧室6的进气端，所述再生罐2的尾气出口通过尾气管道连接到所述水滴分离器7上，空气和LNG分别通过空气进口和LNG进口进入所述燃烧室6内，所述燃烧室6的顶部设置有烟囱。
本实施例提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，包括以下步骤：
第一步，排水阶段，待再生罐2的排水出口没有水流出后，通过压缩空气入口通入压缩空气将吸附剂内部的水份全部去除，压缩空气的通入时间为0.25～2小时。
第二步，升温加热挥发阶段，关闭压缩空气入口和排水出口，打开主蒸汽管道和尾气管道上的阀，启动过热蒸汽发生器101，过热水蒸气快速升温至设定温度200～1000℃，经再生罐内预埋的蒸汽喷射系统进入到再生罐内，对再生罐内吸附剂加热。尾气管道通到尾气处理系统里，再生罐2内的压力保持在0.1～2bar，再生罐2内的温度为200℃～800℃范围，可以根据需要设置。这个具体的设定温度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。
特别的温度为250℃和340℃，250℃可以去除吸附剂中含有的氧、硫、CO 2、小时 2S等小分子无机物，340℃可以去除吸附剂中含有的脂肪、甲醛等小分子有机物。
第三步，保温阶段，当再生罐2内的温度达到设定的温度后，需要持续通入热蒸汽进行保温，保温时间为0.5小时以上。
第四步，低温吹扫阶段，保温阶段结束后，将再生罐2内的温度调整到100～200℃，再生罐2内的压力保持在0.1～2bar，低温吹扫的时间为0.2～3小时，特别的低温吹扫阶段的时间为0.2～3小时。少部分碳化物和残留有机物被持续进入的过热水蒸气从活性炭孔隙中吹扫带出来，从而使吸附剂得到活化再生。吹扫完成，关闭主蒸汽管道，自然冷却。
所述吸附剂包括活性炭、活性焦、沸石。
第三实施例：
如图3所示，本发明提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备包括蒸汽喷射系统、再生罐2、尾气处理系统，所述蒸汽喷射系统包括过热蒸汽发生器101、主蒸汽管道102、次级蒸汽管道103和喷嘴。其中，所述再生罐2内设置有的容纳空间且所述容纳空间内设置有若干的次级蒸汽管道103，所述次级蒸汽管道103的一端通过所述主蒸汽管道102连接到所述过热蒸汽发生器101上且另一端设置有所述喷嘴，所述再生罐2上设置有尾气出口和压缩空气入口且所述压缩空气入口位于所述再生罐2的上部，所述尾气出口通过尾气管道连接到尾气处理系统。
进一步来说，所述次级蒸汽管道103为树状结构。所述再生罐2包括罐体和罐盖，所述罐盖紧密盖合在所述罐体的上方，所述再生罐2的底端设置有排水出口，所述再生罐2的容纳空间内设置有温度感应器和压力感应器。所述主蒸汽管道102和所述尾气管道上设置有阀。
在本实施例中，尾气先冷凝再焚烧，所述尾气处理系统包括冷凝管3、冷凝水收集槽4、水泵5、汽化装置、尾气焚烧处理设备，所述汽化装置设置在所述冷凝水收集槽4和所述尾气焚烧处理设备之间，所述尾气焚烧处理设备包括水滴分离器7、阻火器、水槽8和燃烧室6，所述水滴分离器7的气体输出端与所述阻火器的输入端连接，所述水滴分离器7的液体输出端与所述水槽8连接，所述水槽8与所述燃烧室6的进水端连通，所述阻火器的输出端连接到燃烧室6的进气端，所述再生罐2的尾气出口通过尾气管道连接到所述冷凝管3的入口，所述冷凝管3的出口连接到所述冷凝水收集槽4，所述冷凝管3的两端分别设置有冷却水入口301和冷却水出口302，所述冷凝水收集槽4内的冷凝水通过所述 水泵5输送到汽化装置最后进入所述水滴分离器7上，空气和LNG分别通过空气进口和LNG进口进入所述燃烧室6内，所述燃烧室6的顶部设置有烟囱。
本实施例型提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，包括以下步骤：
第一步，排水阶段，待再生罐2的排水出口没有水流出后，通过压缩空气入口通入压缩空气将吸附剂内部的水份全部去除，压缩空气的通入时间为0.25～2小时。
第二步，升温加热挥发阶段，关闭压缩空气入口和排水出口，打开主蒸汽管道和尾气管道上的阀，启动过热蒸汽发生器101，过热水蒸气快速升温至设定温度200～1000℃，经再生罐内预埋的蒸汽喷射系统进入到再生罐内，对再生罐内吸附剂加热。尾气管道通到尾气处理系统里，再生罐2内的压力保持在0.1～2bar，再生罐2内的温度为200℃～800℃范围，可以根据需要设置。这个具体的设定温度值是根据被处理有机物的特性来确定，只需脱附不要裂解的情况就设定脱附温度。
特别的温度为380℃、400℃、600～800℃，380℃可以裂解去除吸附剂中含有的含C的干馏物，400℃可以裂解去除吸附剂中含有的C-O和C-N键的有机化合物，400～800℃可以碳化去除吸附剂中含有的含碳化合物。
第三步，保温阶段，当再生罐2内的温度达到设定的温度后，需要持续通入热蒸汽进行保温，保温时间为0.5小时以上，特别的保温时间为0.5小时。
第四步，低温吹扫阶段，保温阶段结束后，将再生罐2内的温度调整到100～200℃，再生罐2内的压力保持在0.1～2bar，低温吹扫的时间为0.2～3小时，特别的低温吹扫阶段的时间为0.2～3小时。少部分碳化物和残留有机物被持续进 入的过热水蒸气从活性炭孔隙中吹扫带出来，从而使吸附剂得到活化再生。吹扫完成，关闭主蒸汽管道，自然冷却。
所述吸附剂包括活性炭、活性焦、沸石。
综上所述，本发明提供的一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备通过设置蒸汽喷射系统、再生罐、尾气处理系统，将脱附再生在再生罐进行，严格控制温度和压力，提高了吸附剂脱附再生的效率和使用安全性。在吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺中，先将吸附剂内部的水份全部去除，再升温加热挥发、再高温保温、高温脱附或高温裂解、碳化脱附，最后低温吹扫处理少部分碳化物和残留有机物被持续进入的过热水蒸气从活性炭孔隙中吹扫带出来，从而使吸附剂得到活化再生。吸附剂脱附再生的温度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。
以上所述仅为本发明的实施例而已，并不用于限制本发明，对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的权利要求范围之内。

Claims (7)

  1. 一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，包括蒸汽喷射系统、再生罐(2)、尾气处理系统，所述蒸汽喷射系统包括过热蒸汽发生器(101)、主蒸汽管道(102)、次级蒸汽管道(103)和喷嘴，所述再生罐(2)内设置有的容纳空间且所述容纳空间内设置有若干的次级蒸汽管道(103)，所述次级蒸汽管道(103)的一端通过所述主蒸汽管道(102)连接到所述过热蒸汽发生器(101)上且另一端设置有所述喷嘴，所述再生罐(2)上设置有尾气出口和压缩空气入口且所述压缩空气入口位于所述再生罐(2)的上部，所述尾气出口通过尾气管道连接到尾气处理系统。
  2. 一种吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺，其特征在于，包括以下步骤：
    第一步，排水阶段，待再生罐(2)的排水出口没有水流出后，通过压缩空气入口通入压缩空气将吸附剂内部的水份全部去除；
    第二步，升温加热挥发阶段，关闭压缩空气入口和排水出口，打开主蒸汽管道和尾气管道上的阀，启动过热蒸汽发生器(101)将热蒸汽通入再生罐(2)中，尾气管道通到尾气处理系统里，再生罐(2)内的压力保持在0.1～2bar，再生罐(2)内的温度为200℃～800℃范围，可以根据需要设置；
    第三步，保温阶段，当再生罐(2)内的温度达到设定的温度后，需要持续通入热蒸汽进行保温，保温时间为0.5小时以上；
    第四步，低温吹扫阶段，保温阶段结束后，将再生罐(2)内的温度调整到100～200℃，再生罐(2)内的压力保持在0.1～2bar，低温吹扫的时间为0.2～3小时。
  3. 如权利要求2所述的吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，在所述第一步中压缩空气的通入时间为0.25～2小时。
  4. 如权利要求2所述的吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，在所述第二步中再生罐(2)内的温度为250℃、340℃、380℃、400℃、450℃、600℃、800℃。
  5. 如权利要求2所述的吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，在所述第三步中保温时间为0.5～24小时。
  6. 如权利要求2所述的吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，在所述第四步中低温吹扫阶段的时间为0.2～3小时。
  7. 如权利要求2～6任一所述的吸附水体中有机物的吸附剂的脱附再生及其尾气处理设备，其特征在于，所述吸附剂包括活性炭、活性焦、沸石。
PCT/CN2019/070293 2018-11-06 2019-01-03 吸附水体中有机物的吸附剂的脱附再生及其尾气处理工艺 WO2020093583A1 (zh)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101362076A (zh) * 2007-08-06 2009-02-11 中国石油化工股份有限公司 一种活性炭吸附剂的再生方法
JP2009273975A (ja) * 2008-05-13 2009-11-26 Toyobo Co Ltd 有機溶剤含有ガス処理システム
JP2011194398A (ja) * 2010-02-25 2011-10-06 Toyobo Co Ltd 有機溶剤回収装置
CN104984628A (zh) * 2015-07-10 2015-10-21 张家港市三星净化设备制造有限公司 一种有机废气吸附回收工艺
CN105498446A (zh) * 2016-01-08 2016-04-20 浙江大学 有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法
CN108970596A (zh) * 2018-08-16 2018-12-11 无锡四方集团有限公司 吸附水体中有机物的吸附剂的原位脱附再生工艺
CN108970597A (zh) * 2018-08-16 2018-12-11 无锡四方集团有限公司 吸附有机废气的吸附剂的原位脱附再生工艺

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101362076A (zh) * 2007-08-06 2009-02-11 中国石油化工股份有限公司 一种活性炭吸附剂的再生方法
JP2009273975A (ja) * 2008-05-13 2009-11-26 Toyobo Co Ltd 有機溶剤含有ガス処理システム
JP2011194398A (ja) * 2010-02-25 2011-10-06 Toyobo Co Ltd 有機溶剤回収装置
CN104984628A (zh) * 2015-07-10 2015-10-21 张家港市三星净化设备制造有限公司 一种有机废气吸附回收工艺
CN105498446A (zh) * 2016-01-08 2016-04-20 浙江大学 有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法
CN108970596A (zh) * 2018-08-16 2018-12-11 无锡四方集团有限公司 吸附水体中有机物的吸附剂的原位脱附再生工艺
CN108970597A (zh) * 2018-08-16 2018-12-11 无锡四方集团有限公司 吸附有机废气的吸附剂的原位脱附再生工艺

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