阅读说明：本技术 一种吸附剂的脱附再生活化工艺及其系统 (Desorption regeneration activation process and system for adsorbent ) 是由 茆林凤 于 2020-04-26 设计创作，主要内容包括：本发明提供一种吸附剂的脱附再生活化工艺,包括以下步骤：1)将吸附剂罐内水分通过真空泵抽除；2)开启循环风机和再加热器,除去吸附剂床层的残余水；3)控制再加热器的温度为200～750℃,使吸附剂床层升温至300～550℃,保温0.5～8 h,开启排气及火排尾气处理装置；4)关闭循环风机,向吸附剂罐内的吸附剂通入混合气体进行活化；5)将吸附剂冷却到规定温度,得到再生吸附剂。本发明的吸附剂的脱附再生活化工艺,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活化,具有良好的脱附再生效果,进而使吸附剂长时间使用,节约企业成本。(The invention provides a desorption regeneration activation process of an adsorbent, which comprises the following steps: 1) pumping water in the adsorbent tank through a vacuum pump; 2) turning on a circulating fan and a reheater to remove residual water in the adsorbent bed layer; 3) controlling the temperature of the reheater to be 200-750 ℃, heating the adsorbent bed layer to 300-550 ℃, preserving the heat for 0.5-8 h, and starting an exhaust and fire exhaust tail gas treatment device; 4) closing the circulating fan, and introducing mixed gas into the adsorbent in the adsorbent tank for activation; 5) and cooling the adsorbent to a specified temperature to obtain the regenerated adsorbent. The desorption regeneration activation process of the adsorbent can realize online in-situ desorption regeneration activation of the adsorbent for adsorbing organic matters in water, has good desorption regeneration effect, further enables the adsorbent to be used for a long time, and saves enterprise cost.)

1. A desorption regeneration activation process of an adsorbent is characterized in that: the method comprises the following steps:

1) intermittently pumping water in the adsorbent tank by a vacuum pump;

2) starting a circulating fan and a reheater, controlling the temperature of the reheater to be 200-700 ℃, controlling the temperature of an adsorbent bed layer to be 105-120 ℃ in a thermal circulation mode, and keeping the temperature for 1-2 hours, wherein the pressure in an adsorbent tank is ensured to be 10-60 kPa in the period; if the pressure is lower than 10kPa, starting a steam boiler, supplementing steam in real time, and removing residual water in the adsorbent bed;

3) controlling the temperature of the reheater to be 200-750 ℃, heating the adsorbent bed layer to 300-550 ℃, preserving the heat for 0.5-8 h, and starting an exhaust and fire exhaust tail gas treatment device in real time during the heating process according to the pressure condition in the adsorbent tank to ensure that the pressure in the adsorbent tank is 10-60 kPa; if the pressure is lower than 10kPa, starting a steam boiler to supplement steam in real time;

4) closing the circulating fan, introducing mixed gas into the adsorbent in the adsorbent tank for activation, controlling the temperature of the mixed gas to be 300-800 ℃, and activating for 10-60 min;

5) and cooling the adsorbent to a specified temperature to obtain the regenerated adsorbent.

2. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the adsorbent cooling process in the step 5) specifically comprises the following steps: closing a pipeline and a reheater for providing steam in the mixed gas, cooling the gas in the adsorbent tank through a condenser, sending the cooled gas into the adsorbent tank through a circulating fan, starting a steam boiler when the pressure in the adsorbent tank is less than 10kpa, introducing 100-120 ℃ steam, and cooling the adsorbent to a specified temperature in a circulating mode.

3. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the adsorbent cooling process in the step 5) specifically comprises the following steps: and closing the circulating fan and the reheater, and continuously introducing steam at 100-120 ℃ into the adsorbent tank for cooling.

4. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the adsorbent cooling process in the step 5) specifically comprises the following steps: and (4) closing the circulating fan and the reheater, and adding a proper amount of normal-temperature water into the adsorbent tank for cooling.

5. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the adsorbent is one of activated carbon, activated coke or zeolite.

6. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the mixed gas in the step 4) comprises pure oxygen and water vapor, and the volume concentration of the pure oxygen is 0.05-0.3%.

7. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: the mixed gas in the step 4) comprises air and water vapor, and the volume concentration of the air is 0.25% -2%.

8. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: in the step 2), in the process of removing the residual water in the adsorbent bed, when the internal pressure of the adsorbent tank is smaller than a set value, steam is supplemented, and the internal pressure of the adsorbent tank is kept positive all the time; when the pressure in the adsorbent tank is larger than a set value, opening an exhaust valve at the top of the adsorbent tank, allowing the gas discharged from the adsorbent tank to enter a condenser for cooling, and cooling part of the steam, wherein when the non-condensable gas reaches the spontaneous combustion concentration, no auxiliary fuel is added, and the non-condensable gas is ignited and combusted through a fire grate, and the combusted gas is added into a washing tower through an air inducing device for washing; when the non-condensable gas does not reach the spontaneous combustion concentration, the non-condensable gas is directly added into a washing tower through fire grate to be washed, and the washed gas is subjected to activated carbon adsorption treatment through an activated carbon adsorption device and then is discharged after reaching the standard.

9. The desorption regeneration activation process for an adsorbent according to claim 1, characterized in that: in the step 3), in the processes of heating, warming and heat preservation of the adsorbent in the adsorbent tank, when the internal pressure of the adsorbent tank is smaller than a set value, steam is supplemented, and the internal pressure of the adsorbent tank is kept positive all the time; when the pressure in the adsorbent tank is larger than a set value, opening an exhaust valve at the top of the adsorbent tank, allowing the gas discharged from the adsorbent tank to enter a condenser for cooling, and cooling part of the steam, wherein when the non-condensable gas reaches the spontaneous combustion concentration, no auxiliary fuel is added, and the non-condensable gas is ignited and combusted through a fire grate, and the combusted gas is added into a washing tower through an air inducing device for washing; when the non-condensable gas does not reach the spontaneous combustion concentration, the non-condensable gas is directly added into a washing tower through fire grate to be washed, and the washed gas is subjected to activated carbon adsorption treatment through an activated carbon adsorption device and then is discharged after reaching the standard.

10. A desorption regeneration activation system of adsorbent is characterized in that: the device comprises an adsorbent tank, wherein the adsorbent tank is connected with a water collecting tank through a vacuum pump; the adsorbent tank is connected with the reheater through a first pipeline, so that superheated steam is introduced into the adsorbent tank; a first pipeline for connecting the adsorbent tank with the reheater is connected with a circulating fan, and the output end of the circulating fan is connected with the input end of the reheater; a first pipeline of the reheater connected with the circulating fan is also connected with a steam boiler, and a first valve is arranged on a superheated steam pipeline at a superheated steam inlet end of the steam boiler connected with the first pipeline; the superheated steam pipeline is connected with the outlet end of the gas tank through a gas pipeline; the adsorbent tank is connected with the input end of the condensing device through a second pipeline, the output end of the condensing device is connected with the input end of a flame arrester, the output end of the flame arrester is connected with the input end of a fire grate, the output end of the fire grate is connected with the input end of a washing tower, the output end of the washing tower is connected with the input end of an activated carbon adsorption device, and the output end of the activated carbon adsorption device discharges the treated gas through a fan; a second valve is arranged on a first pipeline which is connected with the adsorbent tank and the input end of the circulating fan; a third valve is arranged on a second pipeline which connects the adsorbent tank with the condensing device; the output end of the adsorbent tank is also connected with a third pipeline, and a fourth valve is arranged on the third pipeline.

Technical Field

The invention relates to a desorption regeneration activation process of an adsorbent for adsorbing organic matters in water, in particular to a desorption regeneration activation process of an adsorbent and a system thereof.

Background

At present, the technology for adsorbing organic matters by using disposable adsorbents (such as activated carbon, activated coke, zeolite and the like) is widely applied to the advanced treatment link of tap water, domestic sewage and industrial sewage. The adsorbent is required to be replaced by a new adsorbent after being adsorbed and saturated, the adsorbent after being adsorbed and saturated is generally treated as hazardous waste disposal unit requiring delegation of qualification or recycled by enterprises requiring delegation of recycling qualification, a large amount of disposal cost is required, and the replacement and transportation are complicated and are not easy to operate, so that the recycling of the adsorbent is a technology which is urgently needed in the aspect of the market application of the current adsorbent.

Chinese patent CN108970596A discloses an in-situ desorption regeneration process of an adsorbent for adsorbing organic matters in a water body, which comprises the steps of blowing the adsorbent, starting a superheated steam generator, heating the adsorbent in an adsorbent tank in an online in-situ manner, keeping the temperature of the adsorbent in the adsorbent tank at a set temperature within the range of 200-800 ℃, continuously heating and preserving heat for 0.5-8 hours, and desorbing most of organic matters at high temperature or by pyrolysis, carbonization and desorption; and (5) purging and cooling. The method has the defects that the activating and regenerating effect of the adsorbent is poor, the adsorbent is weak in adsorption performance after 3-5 times of regeneration, the adsorption material needs to be replaced in a certain period, and the wastewater treatment cost is high.

Disclosure of Invention

Aiming at the problem that the prior desorption regeneration activation process of the adsorbent has poor regeneration effect, the invention provides the desorption regeneration activation process of the adsorbent and a system thereof.

In order to solve the technical problems, the invention adopts the technical scheme that:

a desorption regeneration activation process of an adsorbent is characterized in that: the method comprises the following steps:

1) the water in the adsorbent tank is pumped out in an intermittent mode through a vacuum pump;

2) starting a circulating fan and a reheater, controlling the temperature of the reheater to be 200-700 ℃, controlling the temperature of an adsorbent bed layer to be 105-120 ℃ in a thermal circulation mode, and keeping the temperature for 1-2 hours, wherein the pressure in an adsorbent tank is ensured to be 10-60 kPa in the period; if the pressure is lower than 10kPa, starting a steam boiler to supplement the steam in real time, and removing residual water in the adsorbent bed layer mainly in the process;

after water in an adsorbent tank is intermittently pumped by a vacuum pump, a part of water in an adsorbent bed layer is heated by a reheater and a heat circulation system to a saturated adsorbent in the adsorbent tank, the temperature of the adsorbent bed layer is controlled to be a certain value of 105-120 ℃, the purpose is to remove most of the water in the bed layer, at the stage, after the internal pressure of the adsorbent tank is greater than the set pressure, a part of gas is discharged from the adsorbent tank, the gas enters a condenser for cooling, part of water vapor is cooled down, when the non-condensable gas reaches the spontaneous combustion concentration, no auxiliary fuel is added, the non-condensable gas is ignited and combusted through fire exhaust, and the combusted gas is added into a washing tower through an air inducing device for washing; when the non-condensable gas does not reach the spontaneous combustion concentration, the non-condensable gas is directly added into a washing tower through a fire grate for washing. And (5) carrying out activated carbon adsorption treatment on the washed gas through an activated carbon adsorption device. The pressure in the adsorbent tank is guaranteed to be 10-60 kPa in the whole process, when the pressure is low, steam is supplemented in real time, the pressure in the adsorbent tank is repeatedly circulated, the pressure can not reach the set pressure any more, and the water adsorbed by the saturated adsorbent in the adsorbent tank is dried in the time.

3) Controlling the temperature of the reheater to be 200-750 ℃, heating the adsorbent bed layer to 300-550 ℃, preserving the heat for 0.5-8 h, and starting an exhaust and fire exhaust tail gas treatment device in real time during the heating process according to the pressure condition in the adsorbent tank to ensure that the pressure in the adsorbent tank is 10-60 kPa; if the pressure is lower than 10kPa, starting a steam boiler to supplement the steam in real time, and removing residual water in the adsorbent bed layer mainly in the process;

in the stage, the adsorbent is mainly used for desorbing and carbonizing the organic matters adsorbed by the adsorbent, so that the adsorbent can be reused.

The temperature set value of the step 3) is determined according to the characteristics of the organic matters to be treated, the cracking requirement is met or only the condition that the organic matters are not needed to be cracked is needed to be desorbed, the temperature value is set according to the specific cracking temperature of the treated object under the condition that the cracking requirement is met, the desorption temperature is set under the condition that the organic matters are not needed to be cracked, and particularly, as shown in table 1, the heating and heat preservation are continuously carried out for 0.5-8 hours, and most of the organic matters are desorbed at high temperature or carbonized and desorbed by high-temperature cracking;

TABLE 1

4) Closing the circulating fan, introducing mixed gas into the adsorbent in the adsorbent tank for activation, controlling the temperature of the mixed gas to be 300-800 ℃, and activating for 10-60 min;

the method comprises the following steps that (1) the sewage quality components are complex, the adsorbent is activated and regenerated through the step 3), after the regeneration times are 3-5 times, the adsorbed organic matter is carbonized at high temperature and remains in the adsorbent to become amorphous carbon, pore channels of the adsorbent are blocked, the adsorption performance of the adsorbent after regeneration is reduced through multiple high-temperature regeneration, the amorphous carbon which adsorbs the organic matter is carbonized at high temperature remains in the pore channels, and the amorphous carbon which adsorbs the organic matter remains in the pore channels is activated at high temperature through mixed gas, so that the pore channels remain carbon and pores of the adsorbent are enlarged under the action of the mixed gas; or reacting the amorphous carbon with the mixed gas to separate the amorphous carbon from the pore canal of the adsorbent so as to repair and regenerate the pore canal of the adsorbent; with the increase of the activation time, the carbon on the pore wall of the adsorbent participates in the reaction, and the adsorbent is excessively oxidized, so that the optimal activation time is 10-60 min; the mixed gas is activated in the step 4), so that the selective absorption of the adsorbate in the wastewater is easier in the regeneration process, and the mixed gas is activated, so that the pore structure or the adsorption position and the bonding force in the adsorbent are more favorable for the adsorption of the adsorbate; the mixed gas is activated at 400-800 ℃, so that the kinetic energy of the adsorbate can be increased, the adsorbate can overcome the attraction of the adsorbent and escape from the adsorbent, the carbonized substances in the desorption regeneration process are activated into activated carbon, the outlet of an adsorbent tank is opened in the activation process, water vapor is cooled and collected by a condenser, and a small amount of non-condensable gas is washed and subjected to activated carbon adsorption treatment.

5) And cooling the adsorbent to a specified temperature to obtain the regenerated adsorbent.

Preferably, the desorption regeneration activation process of the adsorbent is that: the adsorbent cooling process in the step 5) specifically comprises the following steps: closing a pipeline and a reheater for providing steam in the mixed gas, cooling the gas in the adsorbent tank through a condenser, sending the cooled gas into the adsorbent tank through a circulating fan, starting a steam boiler when the pressure in the adsorbent tank is less than 10kpa, introducing 100-120 ℃ steam, and cooling the adsorbent to a specified temperature in a circulating mode.

Preferably, the desorption regeneration activation process of the adsorbent is that: the adsorbent cooling process in the step 5) specifically comprises the following steps: and closing the circulating fan and the reheater, and continuously introducing 100-120 ℃ steam into the adsorbent tank for cooling.

Preferably, the desorption regeneration activation process of the adsorbent is that: the adsorbent cooling process in the step 5) specifically comprises the following steps: and (4) closing the circulating fan and the reheater, and adding a proper amount of normal-temperature water into the adsorbent tank for cooling.

Preferably, the desorption regeneration activation process of the adsorbent is that: the adsorbent is one of activated carbon, activated coke or zeolite. The adsorbent includes activated carbon, activated coke, and zeolite, but is not limited to the above three.

Preferably, the desorption regeneration activation process of the adsorbent is that: the mixed gas in the step 4) comprises pure oxygen and water vapor, and the volume concentration of the pure oxygen is 0.05-0.3%.

Preferably, the desorption regeneration activation process of the adsorbent is that: the mixed gas in the step 4) comprises air and water vapor, and the volume concentration of the air is 0.25-2%.

Preferably, the desorption regeneration activation process of the adsorbent is that: in the step 2), in the process of removing the residual water in the adsorbent bed, when the internal pressure of the adsorbent tank is smaller than a set value, steam is supplemented, and the internal pressure of the adsorbent tank is kept positive all the time; when the pressure in the adsorbent tank is larger than a set value, opening an exhaust valve at the top of the adsorbent tank, allowing the gas discharged from the adsorbent tank to enter a condenser for cooling, and cooling part of the steam, wherein when the non-condensable gas reaches the spontaneous combustion concentration, no auxiliary fuel is added, and the non-condensable gas is ignited and combusted through a fire grate, and the combusted gas is added into a washing tower through an air inducing device for washing; when the non-condensable gas does not reach the spontaneous combustion concentration, the non-condensable gas is directly added into a washing tower through fire grate to be washed, and the washed gas is subjected to activated carbon adsorption treatment through an activated carbon adsorption device and then is discharged after reaching the standard.

Preferably, the desorption regeneration activation process of the adsorbent is that: in the step 3), in the processes of heating, warming and heat preservation of the adsorbent in the adsorbent tank, when the internal pressure of the adsorbent tank is smaller than a set value, steam is supplemented, and the internal pressure of the adsorbent tank is kept positive all the time; when the pressure in the adsorbent tank is larger than a set value, opening an exhaust valve at the top of the adsorbent tank, allowing the gas discharged from the adsorbent tank to enter a condenser for cooling, and cooling part of the steam, wherein when the non-condensable gas reaches the spontaneous combustion concentration, no auxiliary fuel is added, and the non-condensable gas is ignited and combusted through a fire grate, and the combusted gas is added into a washing tower through an air inducing device for washing; when the non-condensable gas does not reach the spontaneous combustion concentration, the non-condensable gas is directly added into a washing tower through a fire grate for washing. And (4) carrying out activated carbon adsorption treatment on the washed gas through an activated carbon adsorption device, and then discharging the gas up to the standard.

A desorption regeneration activation system for an adsorbent, wherein: the device comprises an adsorbent tank, wherein the adsorbent tank is connected with a water collecting tank through a vacuum pump; the adsorbent tank is connected with the reheater through a first pipeline, so that superheated steam is introduced into the adsorbent tank; a first pipeline for connecting the adsorbent tank with the reheater is connected with a circulating fan, and the output end of the circulating fan is connected with the input end of the reheater; a steam boiler is also connected to the first pipeline for connecting the reheater and the circulating fan; a first valve is arranged on a superheated steam pipeline at the superheated steam inlet end of the steam boiler connected with the first pipeline; the superheated steam pipeline is connected with the outlet end of the gas tank through a gas pipeline; the adsorbent tank is connected with the input end of the condensing device through a second pipeline, the output end of the condensing device is connected with the input end of a flame arrester, the output end of the flame arrester is connected with the input end of a fire grate, the output end of the fire grate is connected with the input end of a washing tower, the output end of the washing tower is connected with the input end of an activated carbon adsorption device, and the output end of the activated carbon adsorption device discharges the treated gas through a fan; a second valve is arranged on a first pipeline which is connected with the adsorbent tank and the input end of the circulating fan; a third valve is arranged on a second pipeline which connects the adsorbent tank with the condensing device; the output end of the adsorbent tank 1 is also connected with a third pipeline, and a fourth valve is arranged on the third pipeline.

The invention has the advantages that: according to the desorption regeneration activation system of the adsorbent, the adsorbent adsorbs organic matters dissolved in water, after the adsorbent is saturated, the desorption regeneration activation process of the adsorbent is carried out through the desorption regeneration activation system, the temperature of an adsorbent bed layer in the adsorbent tank is raised to 300-550 ℃ through the reheater, most of the organic matters adsorbed by the adsorbent are desorbed or are carbonized and desorbed by high temperature cracking, the adsorbent is oxidized and activated through mixed gas of the steam boiler and the gas tank, and carbonized carbides in adsorbent pores are removed, so that the online desorption regeneration activation of the adsorbent adsorbed by the organic matters in the water can be realized, the desorption regeneration effect is good, the adsorbent is used for a long time, and the enterprise cost is saved.

Drawings

Fig. 1 is a schematic structural view of a desorption regeneration activation system for an adsorbent according to the present invention.

Detailed Description

The invention is further illustrated by the following specific figures and examples.