CN112588078B - High-efficient organic waste gas recovery processing system - Google Patents
High-efficient organic waste gas recovery processing system Download PDFInfo
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Abstract
The invention relates to the technical field of organic waste gas treatment, in particular to a high-efficiency organic waste gas recovery treatment system, which comprises an adsorption subsystem and a desorption subsystem; the adsorption subsystem comprises two or more adsorption beds connected in parallel, and the desorption subsystem comprises a condensation unit; the condensing unit comprises a vacuum pump, a condenser, a gas-liquid separator and a storage tank which are connected in sequence; the gas-liquid separator is characterized in that the air exhaust end of the vacuum pump is communicated with an adsorption bed in the desorption process, and the gas phase outlet of the gas-liquid separator is communicated with the adsorption bed in the adsorption process. The system solves the technical problem that the organic matters cannot be fully recovered by activated carbon adsorption in the prior art. The scheme can be applied to practical operation of organic waste gas recovery and treatment, can efficiently and harmlessly treat the organic waste gas, and can fully recover organic matters in the organic waste gas.
Description
Technical Field
The invention relates to the technical field of organic waste gas treatment, in particular to a high-efficiency organic waste gas recovery treatment system.
Background
In the field of organic waste gas recovery and treatment, activated carbon adsorption is a relatively common technology. The active carbon (located in the adsorption bed) can adsorb organic matters in the organic waste gas through the adsorption process, and then the active carbon is heated, so that the organic matters are desorbed from the active carbon (namely, the desorption process), and the regeneration of the active carbon is realized. The research and practice of the existing activated carbon adsorption technology mainly focuses on the purification of organic waste gas by activated carbon, and a large amount of organic matters in the organic waste gas are not fully utilized. Even if some active carbon adsorption systems in the prior art have designed the condensation recovery structure of organic matter, current condensation recovery structure can not collect the purpose organic matter effectively, and the rate of recovery is limited. Therefore, in order to meet the requirements of practical applications, it is necessary to design a system capable of efficiently and harmlessly treating organic waste gas and sufficiently recovering organic substances in the organic waste gas.
Disclosure of Invention
The invention aims to provide a high-efficiency organic waste gas recovery and treatment system to solve the technical problem that the organic matters cannot be fully recovered by activated carbon adsorption in the prior art.
In order to achieve the purpose, the invention adopts the following technical scheme:
a high-efficiency organic waste gas recovery processing system comprises an adsorption subsystem and a desorption subsystem; the adsorption subsystem comprises two or more adsorption beds connected in parallel, and the desorption subsystem comprises a condensation unit; the condensing unit comprises a vacuum pump, a condenser, a gas-liquid separator and a storage tank which are connected in sequence; the gas-liquid separator is characterized in that the air exhaust end of the vacuum pump is communicated with an adsorption bed in the desorption process, and the gas phase outlet of the gas-liquid separator is communicated with the adsorption bed in the adsorption process.
The principle and the advantages of the scheme are as follows: the desorption subsystem containing the condensation unit is additionally arranged on the basis of the adsorption subsystem, and the desorption subsystem not only can effectively regenerate the active carbon (desorb the organic matters adsorbed on the active carbon), but also can fully condense and recycle the organic matters (including the organic matters adsorbed on the active carbon) in the organic waste gas. After the adsorption bed enters the desorption process, the vacuum pump firstly pumps out gas in the desorption subsystem to enable the desorption subsystem to form a vacuum state, then nitrogen is introduced into the desorption subsystem to replace air, the air is condensed by the condenser, the organic matter is liquefied, gas-liquid separation is carried out in the gas-liquid separator, the liquid phase part enters the storage tank (organic matter), the gas phase part circulates back to the adsorption bed in the adsorption process to further absorb the organic matter in the gas phase part, the above process is repeated for 2-3 times, so that the oxygen content in the desorption subsystem is reduced to be below 3%, and the safety of the desorption process is ensured. After the nitrogen replacement process is completed, the activated carbon on the adsorption bed is heated again, so that the organic matters are desorbed from the activated carbon, the gas material containing the desorbed organic matters is condensed by the condensing unit again and is separated from gas and liquid, the generated liquid phase part enters the storage tank (organic matters), and the gas phase part is circulated to the adsorption bed in the adsorption process to further absorb the organic matters in the gas phase part.
The condensing unit of the scheme can treat gas containing a large amount of organic matters from the adsorption bed after cyclic desorption and can also treat gas generated after nitrogen replacement. The condensing unit achieves two purposes, organic matters in the organic waste gas can be fully recovered, and the recovery rate of the organic matters is improved. In addition, still contain a small amount of organic matters in the gas after the condensation is retrieved, if get back to the desorption subsystem, can have certain influence to the desorption effect, this scheme is with the gaseous input adsorption subsystem of condensation in, avoided above-mentioned influence. Except the improvement organic matter rate of recovery of condensation unit and the function that promotes the desorption effect, the setting up of vacuum pump also is favorable to going on of active carbon desorption, is favorable to the active carbon desorption for the negative pressure before the vacuum pump, is favorable to subsequent condensation for the malleation behind the vacuum pump.
Before the inventor designs and develops the system, an attempt was made to directly introduce the gas generated in the nitrogen substitution step into the adsorption bed in the adsorption process, and it is considered that the above means cannot have a great influence on the recovery rate of the organic matter, but the inventor proves through a comparative experiment that the gas escaping from the adsorption bed in the nitrogen substitution step is condensed and recovered, and the gas phase generated in the recovery process is returned to the adsorption bed in the adsorption process, and the above operation plays a significant role in improving the recovery rate of the target organic matter. The inventors further analyzed the cause of the above phenomenon, and the flow of nitrogen affects the adsorption stability of some small molecular organic matters, especially in the case of using a vacuum pump, so that the gas escaping from the adsorption bed during nitrogen replacement needs to enter the condensation recovery to ensure the ideal organic matter recovery rate.
Furthermore, the adsorption subsystem also comprises an organic waste gas inlet and an exhaust fan; the waste gas inlet of the adsorption bed is communicated with the organic waste gas inlet, and the purified gas outlet of the adsorption bed is communicated with the exhaust fan.
By adopting the technical scheme, the exhaust fan drives the organic waste gas to move from the organic waste gas inlet to the purified gas outlet and the system through the adsorption bed, and organic matters in the organic waste gas are adsorbed by the activated carbon in the process, so that the gas purification is realized.
Further, the desorption subsystem also comprises a circulating desorption unit; the circulating desorption unit comprises a cooler and a heater which are connected in sequence; the tube side inlet of the cooler is used for being communicated with a waste gas inlet of the adsorption bed in the desorption process, and the tube side outlet of the heater is used for being communicated with a purified gas outlet of the adsorption bed in the desorption process.
By adopting the technical scheme, the heater of the circulating desorption unit works, so that nitrogen in the pipeline can be heated, the activated carbon in the adsorption bed is heated, and desorption of organic matters and regeneration of the activated carbon are realized. The cooler of the circulating desorption unit works to cool the nitrogen in the pipeline, so that the activated carbon is cooled, and the activated carbon is recovered to be capable of adsorbing organic matters.
Further, the cyclic desorption unit also comprises a circulating fan which is positioned between the cooler and the heater; and a purified gas outlet of the adsorption bed is communicated with a nitrogen inlet.
By adopting the technical scheme, the circulating fan can drive the gas in the pipeline to flow, so that the heating or cooling of the activated carbon in the adsorption bed is realized.
Further, a condensation valve is arranged upstream of the vacuum pump, and a circulating valve is arranged upstream of the cooler.
By adopting the technical scheme, the condensing valve is opened, the gas material in the pipeline flows to the vacuum pump, and the condensing recovery process is started. And (3) opening a circulating valve, and enabling the gas material in the pipeline to flow to the cooler and the heater, so that the heating or cooling process of the activated carbon can be carried out. In this case, the upstream of the process and the downstream of the process are identified in terms of the direction of flow of the material.
Further, the adsorption beds include a first adsorption bed and a second adsorption bed.
By adopting the technical scheme, the first adsorption bed and the second adsorption bed can alternately perform an adsorption process and a desorption process, so that the working efficiency is improved.
Further, a first adsorption bed first valve and a second adsorption bed first valve are respectively arranged at a waste gas inlet of the first adsorption bed and a waste gas inlet of the second adsorption bed, and a first adsorption bed fourth valve and a second adsorption bed fourth valve are respectively arranged at a purified gas outlet of the first adsorption bed and a purified gas outlet of the second adsorption bed; first valve of first adsorption bed and first valve of second adsorption bed all are used for with organic waste gas entry intercommunication, first valve of fourth adsorption bed and second adsorption bed all be used for with the exhaust fan intercommunication.
By adopting the technical scheme, when the first valve of the first adsorption bed, the first valve of the second adsorption bed and the fourth valve of the first adsorption bed and the fourth valve of the second adsorption bed are both opened, the organic waste gas flows to the exhaust fan from the organic waste gas inlet through the adsorption beds, and the organic waste gas is purified in the process.
Furthermore, a first adsorption bed second valve and a second adsorption bed second valve are respectively arranged at a waste gas inlet of the first adsorption bed and a waste gas inlet of the second adsorption bed; when the first adsorption bed is in the desorption process and the second adsorption bed is in the adsorption process, the first adsorption bed is communicated with the second adsorption bed through a second valve of the first adsorption bed, the condensation unit and a first valve of the second adsorption bed; when the second adsorption bed is in the desorption process and the first adsorption bed is in the adsorption process, the second adsorption bed is communicated with the first adsorption bed through a second valve of the second adsorption bed, the condensing unit and a first valve of the first adsorption bed.
By adopting the technical scheme, when the first adsorption bed is in the desorption process, the first adsorption bed can form a closed loop with the second adsorption bed through the second valve of the first adsorption bed, the condensation unit and the first valve of the second adsorption bed. When the second adsorption bed is in the desorption process and the first adsorption bed is in the adsorption process, the second adsorption bed and the first adsorption bed can form a closed loop through the second valve of the second adsorption bed, the condensation unit and the first valve of the first adsorption bed. In the two closed loops, nitrogen displacement gas and nitrogen containing a large amount of organic matters are subjected to gas-liquid separation through condensation, the organic matters are partially recovered, and the gas phase part continues to enter the adsorption process, so that the organic matters are fully recovered and utilized.
Further, a purified gas outlet of the first adsorption bed and a purified gas outlet of the second adsorption bed are respectively provided with a fifth valve of the first adsorption bed and a fifth valve of the second adsorption bed; the waste gas inlet of the first adsorption bed is communicated with the purified gas outlet of the first adsorption bed through a second valve of the first adsorption bed, a cyclic desorption unit and a fifth valve of the first adsorption bed; and a waste gas inlet of the second adsorption bed is communicated with a purified gas outlet of the second adsorption bed through a second valve of the second adsorption bed, a cyclic desorption unit and a fifth valve of the second adsorption bed.
Adopt above-mentioned technical scheme, the waste gas entry of first adsorption bed forms closed loop rather than purifying the gas export through circulation desorption unit, and the waste gas entry of second adsorption bed forms closed loop rather than purifying the gas export through circulation desorption unit. And the fifth valve of the first adsorption bed and the second valve of the second adsorption bed control the opening and closing of the closed loop of the second adsorption bed.
Further, a purified gas outlet of the first adsorption bed and a purified gas outlet of the second adsorption bed are respectively provided with a third valve of the first adsorption bed and a third valve of the second adsorption bed.
By adopting the technical scheme, after the third valve of the first adsorption bed or the third valve of the second adsorption bed are opened, nitrogen can enter the first adsorption bed or the second adsorption bed, so that the replacement of the nitrogen is realized.
Drawings
FIG. 1 is a schematic view of a high-efficiency organic waste gas recovery processing system according to example 1.
FIG. 2 is a schematic view of a high efficiency organic waste gas recovery processing system of comparative example 1.
Detailed Description
The following is further detailed by way of specific embodiments:
reference numerals in the drawings of the specification include: the device comprises a first adsorption bed valve A1, a first adsorption bed valve A2, a first adsorption bed valve A3, a first adsorption bed valve A4, a first adsorption bed valve A5, a second adsorption bed valve B1, a second adsorption bed valve B2, a second adsorption bed valve B3, a second adsorption bed valve B4, a second adsorption bed valve B5, a first adsorption bed C1, a second adsorption bed C2, an oxygen concentration detector D, a cooler E1, a condenser E2, a heater E3, a gas-liquid separator F1, an organic waste gas inlet G, a condensation valve K1, a circulating valve K2, a recovery valve K3, a nitrogen inlet N, an exhaust fan P1, a circulating fan P2, a vacuum pump P3 and a storage tank V1.
Example 1:
as shown in fig. 1, a high-efficiency organic waste gas recovery processing system comprises an adsorption subsystem and a desorption subsystem, wherein the adsorption subsystem comprises an organic waste gas inlet G, adsorption beds (in this embodiment, a first adsorption bed C1 and a second adsorption bed C2) and an exhaust fan P1. The desorption subsystem comprises a condensation unit and a circulating desorption unit; the condensing unit comprises a vacuum pump P3, a condenser E2, a gas-liquid separator F1 and a storage tank V1; the cyclic desorption unit includes a cooler E1, a circulating fan P2, and a heater E3. The first adsorption bed C1 and the second adsorption bed C2 are connected in parallel, and specifically comprise: the waste gas inlet above the first adsorption bed C1 and the waste gas inlet above the second adsorption bed C2 are communicated with the organic waste gas inlet G through pipelines, a first valve A1 of the first adsorption bed is arranged on the pipeline between the organic waste gas inlet G and the waste gas inlet of the first adsorption bed C1, the first valve A1 of the first adsorption bed is opened, and the organic waste gas can enter the first adsorption bed C1. And a first valve B1 of the second adsorption bed is arranged on a pipeline between the organic waste gas inlet G and the waste gas inlet of the second adsorption bed C2, and the first valve B1 of the second adsorption bed is opened, so that the organic waste gas can enter the second adsorption bed C2.
The purified gas outlet below the first adsorption bed C1 and the purified gas outlet below the second adsorption bed C2 are communicated with an exhaust fan P1 through pipelines. A fourth valve A4 of the first adsorption bed is arranged on a pipeline between the purified gas outlet of the first adsorption bed C1 and the exhaust fan P1, the fourth valve A4 of the first adsorption bed is used for controlling whether the gas material in the first adsorption bed C1 is exhausted to the exhaust fan P1, and the gas exhausted from the exhaust fan P1 is purified gas from which most organic matters are removed and is conveyed to downstream process equipment. A fourth valve B4 of the second adsorption bed is arranged on a pipeline between the purified gas outlet of the second adsorption bed C2 and the exhaust fan P1, and the fourth valve B4 of the second adsorption bed is used for controlling whether the gas materials in the second adsorption bed C2 are exhausted to the exhaust fan P1.
The waste gas inlet above the first adsorption bed C1 and the waste gas inlet above the second adsorption bed C2 are communicated with the tube pass inlet of the cooler E1 through pipelines, the tube pass outlet of the cooler E1 is communicated with the tube pass inlet of the heater E3 through a pipeline, and the tube pass outlet of the heater E3 is communicated with the purified gas outlet below the first adsorption bed C1 and the purified gas outlet below the second adsorption bed C2 through pipelines. A circulating fan P2 is arranged on a pipeline between the cooler E1 and the heater E3, and a circulating valve K2 is arranged at the upstream of the cooler E1. And a second valve A2 of the first adsorption bed is arranged on a pipeline between the waste gas inlet of the first adsorption bed C1 and the circulating valve K2, and after the second valve A2 of the first adsorption bed is opened, the gas in the first adsorption bed C1 flows to the direction of the circulating valve K2. A second valve B2 of the second adsorption bed is arranged on a pipeline between the waste gas inlet of the second adsorption bed C2 and the circulating valve K2, and after the second valve B2 of the second adsorption bed is opened, the gas in the second adsorption bed C2 flows to the direction of the circulating valve K2. A fifth valve A5 of the first adsorption bed is arranged on a pipeline between a purified gas outlet of the first adsorption bed C1 and the heater E3, the fifth valve A5 of the first adsorption bed is opened, and gas materials flow into the first adsorption bed C1 from the heater E3. A fifth valve B5 of the second adsorption bed is arranged on a pipeline between the purified gas outlet of the second adsorption bed C2 and the heater E3, the fifth valve B5 of the second adsorption bed is opened, and the gas material flows into the second adsorption bed C2 from the heater E3.
The purified gas outlets of the first adsorption bed C1 and the second adsorption bed C2 are communicated with the nitrogen inlet N through a pipeline, a third valve A3 of the first adsorption bed is arranged on the pipeline between the purified gas outlet of the first adsorption bed C1 and the nitrogen inlet N, the third valve A3 of the first adsorption bed is opened, and nitrogen is input into the first adsorption bed C1; and a third valve B3 of the second adsorption bed is arranged on a pipeline between the purified gas outlet of the second adsorption bed C2 and the nitrogen inlet N, the third valve B3 of the second adsorption bed is opened, and nitrogen is input into the second adsorption bed C2.
The air exhaust end of the vacuum pump P3 is communicated with a pipeline between the second adsorption bed valve B2 and the circulating valve K2 through the pipeline, a condensing valve K1 is arranged on the pipeline between the vacuum pump P3 and the second adsorption bed valve B2, the condensing valve K1 is opened, and the gas material in the pipeline flows to the vacuum pump P3. The air outlet end of the vacuum pump P3 is communicated with the inlet of the tube pass of the condenser E2, and the outlet of the tube pass of the condenser E2 is communicated with the inlet of the gas-liquid separator F1. And a gas phase outlet of the gas-liquid separator F1 is communicated with the first valve A1 of the first adsorption bed and the first valve B1 of the second adsorption bed through pipelines. The liquid phase outlet of the gas-liquid separator F1 is communicated with the inlet of the storage tank V1 through a pipeline.
In order to detect the oxygen concentration in the pipeline, an oxygen concentration detector D is provided on the pipeline between the continuous gas-liquid separator F1 and the organic waste gas inlet G, and the oxygen concentration detector D is located upstream of the first valve A1 of the first adsorption bed and the first valve B1 of the second adsorption bed.
In this scheme, various valves, first adsorption bed C1, second adsorption bed C2, oxygen concentration detector D, heat exchange equipment (cooler E1, condenser E2, heater E3), vapour and liquid separator F1, various fans (exhaust fan P1, circulating fan P2), vacuum pump P3, storage tank V1 etc. are the equipment commonly used in chemical industry field and exhaust-gas treatment field, and this scheme utilizes equipment commonly used to connect the setting, has obtained the exhaust-gas treatment and the organic matter recovery effect of ideal. The heat exchange apparatus in this embodiment is a conventional heat exchange apparatus comprising a shell side and a tube side. The tube side of the heat exchange device refers to a channel in the heat exchanger through which materials (for example, gas pumped by a vacuum pump P3 in the nitrogen replacement process) flow and a part communicated with the channel, and the materials can be heated or cooled after flowing through the shell side so as to meet the process requirements. The shell side of a heat exchange device refers to a channel outside a heat exchanger through which a heating or cooling medium (a heat source or a cold source, such as cold water or steam) flows and a part communicated with the channel. In this embodiment, the upstream and downstream of the process are determined according to the flow direction of the material, for example, the oxygen concentration detector D is located at the first valve A1 and the second valve B1 of the first adsorption bed, which means that the gas material flows through the oxygen concentration detector D first and then flows into the first valve A1 or the second valve B1 of the first adsorption bed.
The specific implementation process comprises the following steps:
1 adsorption Process
The first valve A1 and the fourth valve A4 of the first adsorption bed are opened, organic waste gas enters the first adsorption bed C1 from the organic waste gas inlet G, organic matters in the organic waste gas are adsorbed on the activated carbon in the first adsorption bed C1, and the organic waste gas is purified and then discharged (or sent to a subsequent device) through the exhaust fan P1. After the first adsorption bed C1 is saturated, the first valve A1 and the fourth valve A4 of the first adsorption bed are closed. No. one valve B1 of the second adsorption bed and a No. four valve B4 of the second adsorption bed are both opened, and organic waste gas enters the second adsorption bed C2 from the organic waste gas inlet G for adsorption and purification. Meanwhile, the second valve A2 and the fifth valve A5 of the first adsorption bed are opened, and the first adsorption bed C1 carries out the desorption process. After the second adsorption bed C2 is saturated, the first valve B1 and the fourth valve B4 of the second adsorption bed are both closed, the first valve A1 and the fourth valve A4 of the first adsorption bed are opened, and organic waste gas enters the first adsorption bed C1 for adsorption and purification. And a second valve B2 and a fifth valve B5 of the second adsorption bed C2 of the second adsorption bed are opened to perform the desorption process. The adsorption process and the desorption process of the first adsorption bed C1 and the second adsorption bed C2 are alternately carried out.
2 Desorption Process
2.1 Nitrogen substitution
The desorption process is illustrated by taking the second adsorption bed C2 as an example, and the organic substance adsorption capacity of the activated carbon in the second adsorption bed C2 is restored by the desorption process. A first valve B1 of the second adsorption bed and a fourth valve B4 of the second adsorption bed are closed, a second valve B2 of the second adsorption bed C2 and a fifth valve B5 of the second adsorption bed are opened, a condensing valve K1 is opened, a circulating valve K2 is closed, a vacuum pump P3 is started, and the second adsorption bed C2 and a pipeline are vacuumized to-0.07 to-0.09 Mpa; the vacuum pump P3 is stopped. Then a third valve B3 of the second adsorption bed is opened, nitrogen enters the system from a nitrogen inlet N, the pressure is recovered to the normal pressure, and the valve B3 is closed. The above process is repeated for 2-3 times. The nitrogen replaces the oxygen in the second adsorption bed C2 and the pipeline, so that the oxygen content is reduced, and the safety is ensured (until the oxygen concentration detected by the oxygen concentration detector D is less than 3%). Compared with the continuous nitrogen replacement process, the vacuumizing and nitrogen indirect replacement can save nitrogen. And gas pumped by the vacuum pump P3 is sent to the condenser E2, gas-liquid separation is carried out under the action of the gas-liquid separator F1, the liquid phase part enters the storage tank V1, and the gas phase part enters the first adsorption bed C1 through a pipeline for an adsorption process. The vacuum pump P3 is in front of the negative pressure to facilitate desorption with the active carbon, and the vacuum pump P3 is in back of the positive pressure to facilitate subsequent condensation.
2.2 Cyclic Desorption
After the nitrogen replacement is finished, the condensing valve K1 is closed, the circulating valve K2 is opened, the circulating fan P2 is started, and the nitrogen forms closed-loop flow in the second adsorption bed C2 and the corresponding pipeline. The heater E3 (the heat source is steam, which is a conventional manner in the prior art) is started to circularly heat the gas (nitrogen) in the system, so as to heat the activated carbon in the second adsorption bed C2, and the activated carbon (the second adsorption bed C2) is desorbed in the process. In the process, the activated carbon of the adsorption bed in the desorption process is heated to 100-120 ℃, and the duration of the cyclic desorption step is 0.5-1 h.
2.3 post-treatment of Desorption
When the temperature of the activated carbon layer reaches 120 ℃, the circulating valve K2, the circulating fan P2 and the heater E3 are closed (gas is not heated), the condensing valve K1 is opened, the vacuum pump P3 is opened for vacuumizing, organic matters desorbed from the activated carbon are taken out together with the gas by the vacuum pump P3 and are sent to the condenser E2 (cold water), gas-liquid separation is carried out under the action of the gas-liquid separator F1, a liquid phase part enters the storage tank V1, and a gas phase part enters the first adsorption bed C1 through a pipeline for adsorption. The duration of the desorption post-treatment step is 3-4 h.
2.4 Cooling with activated carbon
After the desorption post-treatment is finished, closing the condensation valve K1 and the vacuum pump P3, opening the circulating valve K2 and the circulating fan P2, starting the cooler E1 (cold source is cold water) to cool the gas material, cooling the activated carbon in the second adsorption bed C2, closing the circulating valve K2 and the circulating fan P2 when the temperature of the activated carbon layer reaches 20-30 ℃, and closing the cooler E1 (stopping cooling the gas material). The second adsorption bed C2 completes the desorption process and can be used for the adsorption of the organic waste gas. The desorption process of the first adsorption bed C1 is the same as that of the second adsorption bed C2, and will not be described herein.
In this embodiment, a condensing unit is provided which can treat not only the gas containing a large amount of organic matters from the first and second adsorption beds C1 and C2 after the cyclic desorption but also the gas generated after the nitrogen substitution. The condensing unit achieves two purposes, organic matters in the organic waste gas can be fully recovered, and the recovery rate of the organic matters is improved. Still contain a small amount of organic matters in the gas after the condensation is retrieved, if get back to the desorption subsystem, can have certain influence to the desorption effect, this scheme is with the gaseous input adsorption subsystem of condensation in, avoided above-mentioned influence. In addition, the vacuum pump P3 is in front of the negative pressure to facilitate desorption with the active carbon, and the vacuum pump P3 is in back of the positive pressure to facilitate subsequent condensation.
Example 2
In this example, the organic waste gas is recovered based on example 1, andthe Volatile Organic Compounds (VOCs) in the engine waste gas mainly contains dichloromethane, and the content of dichloromethane is 900g/m 3 (ii) a Exhaust gas flow 500m 3 H is used as the reference value. In this embodiment, the organic waste gas is filtered before entering the system, and contains no suspended particles.
The effective adsorption volume of the first adsorption bed C1 and the second adsorption bed C2 was 0.6m 3 And high-efficiency coal-based activated carbon with the grain diameter of 3mm is adopted, and the average gas flow of the organic waste gas in the first adsorption bed C1 and the second adsorption bed C2 is 0.2m/s. During the adsorption, the organic waste gas flows through the first adsorption bed C1 or the second adsorption bed C2 at an average velocity of 0.2m/s (in practice, the average flow velocity of the organic waste gas can be maintained at 0.1-0.3 m/s), and is discharged from the purified gas outlets of the first adsorption bed C1 and the second adsorption bed C2. In the adsorption process, the internal pressure of the first adsorption bed C1 or the second adsorption bed C2 is maintained at 0.001MPa (which can be changed within the range of 0.0005-0.001 MPa), the temperature is maintained at 25 ℃ (which can be changed within the range of 20-30 ℃), each adsorption process lasts for 6h (until the adsorption is saturated, in actual operation, the duration of the adsorption process can be 5-6 h), the adsorption process is carried out at normal temperature, the adsorption bed is replaced after the adsorption is finished, and the used adsorption bed is subjected to the desorption process.
Taking the desorption of the second adsorption bed C2 as an example, in the nitrogen replacement step of the desorption process, the air in the second adsorption bed C2 is replaced by nitrogen, specifically: and (3) vacuumizing the second adsorption bed C2 to-0.07 to-0.09 Mpa by using gas pumped out by the vacuum pump P3, then opening a third valve B3 of the second adsorption bed, and introducing nitrogen to recover the normal pressure. And vacuumizing by using the vacuum pump P3 again, introducing nitrogen to the normal pressure, and repeating the process of vacuumizing and introducing nitrogen to recover the normal pressure for 3 times (repeating for 2-3 times according to actual conditions until the oxygen concentration in the detection pipeline of the oxygen concentration detector D is less than 3%). Gas material (named as gas I) from a vacuum pump is sent to a condenser E2 (the temperature of the gas material is reduced to 5-8 ℃), gas and liquid are separated under the action of a gas-liquid separator F1 (the working temperature is 5-10 ℃, and the pressure is 0.001-0.002 MPa), a liquid phase part I and a gas phase part I are formed, the liquid phase part I enters a storage tank V1, and the gas phase part I enters a first adsorption bed C1 through a pipeline for an adsorption process.
In the cyclic desorption step, the temperature of nitrogen (with the average flow speed of 11-15 m/s) in the pipeline is raised through the heater E3, then the nitrogen heats the activated carbon in the second adsorption bed C2, so that the organic matters are desorbed until the temperature of the activated carbon in the second adsorption bed C2 reaches 120 ℃, and the process lasts for 1 hour.
In the post-desorption treatment step, the organic matter desorbed from the activated carbon is carried out together with the gas by the vacuum pump P3 (referred to as gas II), the vacuum pump P3 makes the pressure of the second adsorption bed C2 be-0.07 to-0.09 Mpa, and keeps the temperature of the activated carbon in the second adsorption bed C2 at 100 to 120 ℃. The gas material (gas II) is sent to a condenser E2 by a vacuum pump P3, the condenser E2 reduces the temperature of the gas II to 5-8 ℃, and then gas-liquid separation is carried out under the action of a gas-liquid separator F1 (the working temperature is 5-10 ℃ and the pressure is 0.001-0.002 MPa) to form a liquid phase part II and a gas phase part II. And the liquid phase part II enters the storage tank V1, and the gas phase part II enters the first adsorption bed C1 through a pipeline to carry out an adsorption process. The duration of the post-desorption treatment step was 4h.
In the activated carbon temperature-decreasing step, nitrogen (average flow velocity of 11 to 15 m/s) is decreased in temperature by the cooler E1 so that the temperature of the activated carbon in the second adsorption bed C2 is decreased to 25 ℃.
The desorption process and parameter conditions of the first adsorption bed C1 are the same as those of the second adsorption bed C2. After the cyclic adsorption is performed for 10 times according to the process (the first adsorption bed C1 and the second adsorption bed C2 are respectively subjected to 5 adsorption processes and 5 desorption processes), the recovery rate of the volatile organic compounds is detected by the calculation method: the mass of the target organic matter in the storage tank V1/the mass of the target organic matter in the organic waste gas entering the system is multiplied by 100 percent, wherein the calculation method of the mass of the target organic matter in the storage tank V1 comprises the following steps: converting the volume of the target organic matter in the storage tank V1 into the target organic matter quantity; the method for calculating the mass of the target organic matters in the organic waste gas entering the system comprises the following steps: and detecting the content of the target organic matters in the organic waste gas, and calculating the mass of the target organic matters according to the quantity of the organic waste gas entering the system. In this example, the recovery of methylene chloride was 95%.
Comparative example 1
This comparative example is basically the same as example 2 except that, as shown in fig. 2, a recovery valve K3 is provided. The recovery valve K3 is arranged on a pipeline between the oxygen concentration detector D and the first valve B1 of the second adsorption bed and a pipeline between the oxygen concentration detector D and the first valve A1 of the first adsorption bed, the recovery valve K3 is opened, and gas materials can flow to the first valve A1 of the first adsorption bed and the first valve B1 of the second adsorption bed. Before developing the system of example 2, it was not considered to treat the gas material by means of condensation in the nitrogen substitution step, but to open the recovery valve K3, close the condensation valve K1 and the circulation valve K2 in the stage of nitrogen substitution, and the gas material from the first adsorption bed C1 or the second adsorption bed C2 was returned to the adsorption bed (the second adsorption bed C2 or the first adsorption bed C1) in the adsorption stage through the recovery valve K3 until the oxygen concentration detector D detected that the oxygen concentration was less than 3%. The nitrogen pushes the gas material in the adsorption bed to enter downstream equipment through a recovery valve K3, and the average flow speed of the nitrogen is 11-15 m/s. The other work flow and parameters of this comparative example were the same as example 2. In this comparative example, the recovery of dichloromethane was 85%. The inventors initially considered that the gas exiting the adsorption bed during the nitrogen displacement step may contain very small amounts of organic substances, and this gas can be recycled back to the adsorption bed in the adsorption stage without having to turn on the vacuum pump P3 and the subsequent condenser E2 to save energy. However, in practical use, it was found that the recovery rate of the organic matter in this manner of comparative example 1 was low as compared with example 2, indicating that it was necessary to sufficiently condense and recover the gas in the nitrogen substitution step.
The above description is only an example of the present invention, and the general knowledge of the known specific technical solutions and/or characteristics and the like in the solutions is not described herein too much. It should be noted that, for those skilled in the art, without departing from the technical solution of the present invention, several variations and modifications can be made, which should also be regarded as the protection scope of the present invention, and these will not affect the effect of the implementation of the present invention and the practicability of the patent. The scope of the claims of the present application shall be determined by the contents of the claims, and the description of the embodiments and the like in the specification shall be used to explain the contents of the claims. In this embodiment, unless otherwise specified, MPa means gauge pressure.
Claims (10)
1. A high-efficiency organic waste gas recovery processing system is characterized by comprising an adsorption subsystem and a desorption subsystem; the adsorption subsystem comprises two or more adsorption beds connected in parallel, and the desorption subsystem comprises a condensation unit; the condensing unit comprises a vacuum pump, a condenser, a gas-liquid separator and a storage tank which are connected in sequence; the gas-liquid separator is used for separating the gas phase from the liquid phase, and the gas phase is separated from the liquid phase by the gas-liquid separator;
a condensing valve is arranged at the upstream of the vacuum pump, when the adsorption bed is in a nitrogen replacement step, the condensing valve is opened, the vacuum pump is used for pumping out gas in the adsorption bed, the internal pressure of the adsorption bed is adjusted to-0.07 to-0.09 Mpa, and then the adsorption bed is filled with nitrogen; the extracted gas is processed by a condenser and a gas-liquid separator in sequence to form a liquid phase part I and a gas phase part I; collecting said liquid phase fraction I in said storage tank and passing said gas phase fraction I to an adsorption bed in an adsorption process; the process of pumping and filling nitrogen by the vacuum pump is repeated for 2 to 3 times;
the organic waste gas contains dichloromethane; the filler in the adsorption bed is coal-based activated carbon with the particle size of 3mm, and the effective adsorption volume of the adsorption bed is 0.6m 3 。
2. The system of claim 1, wherein the adsorption subsystem further comprises an organic waste gas inlet and an exhaust fan; the waste gas inlet of the adsorption bed is communicated with the organic waste gas inlet, and the purified gas outlet of the adsorption bed is communicated with the exhaust fan.
3. The system of claim 2, wherein the desorption subsystem further comprises a cyclic desorption unit; the circulating desorption unit comprises a cooler and a heater which are connected in sequence; the tube pass inlet of the cooler is used for being communicated with the waste gas inlet of the adsorption bed in the desorption process, and the tube pass outlet of the heater is used for being communicated with the purified gas outlet of the adsorption bed in the desorption process.
4. The system of claim 3, wherein the cyclic desorption unit further comprises a circulating fan between the cooler and the heater; and a purified gas outlet of the adsorption bed is communicated with a nitrogen inlet.
5. The system of claim 4, wherein a circulation valve is disposed upstream of the cooler.
6. The system of claim 5, wherein the adsorbent beds comprise a first adsorbent bed and a second adsorbent bed.
7. The system for recovering and treating an organic waste gas with high efficiency as claimed in claim 6, wherein a first valve of the first adsorption bed and a first valve of the second adsorption bed are provided at the waste gas inlet of the first adsorption bed and the waste gas inlet of the second adsorption bed, respectively, and a fourth valve of the first adsorption bed and a fourth valve of the second adsorption bed are provided at the purified gas outlet of the first adsorption bed and the purified gas outlet of the second adsorption bed, respectively; first valve of first adsorption bed and first valve of second adsorption bed all are used for with organic waste gas entry intercommunication, first valve of fourth adsorption bed and second adsorption bed all be used for with the exhaust fan intercommunication.
8. The system of claim 7, wherein a second valve of the first adsorption bed and a second valve of the second adsorption bed are respectively arranged at the waste gas inlet of the first adsorption bed and the waste gas inlet of the second adsorption bed; when the first adsorption bed is in a desorption process and the second adsorption bed is in an adsorption process, the first adsorption bed is communicated with the second adsorption bed through a second valve of the first adsorption bed, the condensing unit and a first valve of the second adsorption bed; when the second adsorption bed is in the desorption process and the first adsorption bed is in the adsorption process, the second adsorption bed is communicated with the first adsorption bed through a second valve of the second adsorption bed, the condensing unit and a first valve of the first adsorption bed.
9. The system for recovering and treating organic waste gas with high efficiency as claimed in claim 7, wherein a purified gas outlet of the first adsorption bed and a purified gas outlet of the second adsorption bed are provided with a valve No. five of the first adsorption bed and a valve No. five of the second adsorption bed, respectively; the waste gas inlet of the first adsorption bed is communicated with the purified gas outlet of the first adsorption bed through a second valve of the first adsorption bed, a cyclic desorption unit and a fifth valve of the first adsorption bed; and a waste gas inlet of the second adsorption bed is communicated with a purified gas outlet of the second adsorption bed through a second valve of the second adsorption bed, a cyclic desorption unit and a fifth valve of the second adsorption bed.
10. The system of claim 9, wherein a purified gas outlet of the first adsorption bed and a purified gas outlet of the second adsorption bed are provided with a third valve of the first adsorption bed and a third valve of the second adsorption bed, respectively.
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