CN111054738A - Soil indirect thermal desorption gas treatment device and method - Google Patents
Soil indirect thermal desorption gas treatment device and method Download PDFInfo
- Publication number
- CN111054738A CN111054738A CN202010021489.6A CN202010021489A CN111054738A CN 111054738 A CN111054738 A CN 111054738A CN 202010021489 A CN202010021489 A CN 202010021489A CN 111054738 A CN111054738 A CN 111054738A
- Authority
- CN
- China
- Prior art keywords
- temperature
- thermal desorption
- condenser
- desorption gas
- superheater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09C—RECLAMATION OF CONTAMINATED SOIL
- B09C1/00—Reclamation of contaminated soil
- B09C1/06—Reclamation of contaminated soil thermally
Abstract
The invention discloses a device and a method for treating soil indirect thermal desorption gas, which comprises a superheater, a high-temperature dust remover, a high-temperature cooler, a condenser and a thermal oxidizer which are sequentially connected through pipelines; the superheater is connected with a thermal desorption soil remediation system; the hot side of the high-temperature cooler is connected with the dedusted thermal desorption gas, and the cold side is introduced into the outside at normal temperature through an air blower for heat exchange; the preheated air directly enters a subsequent thermal oxidizer through a pipeline; the condenser is connected with a circulating cooling water device and an organic wastewater collecting device; the outlets of the superheater, the high-temperature cooler and the condenser are respectively provided with a temperature measuring instrument; the thermal oxidizer air inlet is respectively connected with the condenser and the high-temperature cooler, and is provided with a fuel supplementing port and a fuel supplementing port, high-temperature flue gas is formed through internal combustion, one part of the high-temperature flue gas is used as a heat source in the superheater and used for heating indirect thermal desorption gas coming out of the thermal desorption soil remediation system, and the rest part of the high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system for recycling.
Description
Technical Field
The invention belongs to the technical field of soil remediation of contaminated sites, is suitable for soil indirect thermal desorption remediation and purification, and particularly relates to a device and a method for treating soil indirect thermal desorption gas.
Background
With the increasing strictness of economic development and environmental regulations, a large number of industrial plants such as chemical plants, pesticide plants and the like need to be moved, and a large number of organic matter pollution sites are left. The indirect thermal desorption technology is one of the mainstream technologies for restoring the soil of the organic contaminated site.
The indirect thermal desorption technology is to heat the excavated polluted soil to a temperature higher than the boiling point of a target pollutant by indirect heating, and to selectively gasify and volatilize the pollutant by controlling the system temperature and the material retention time, so that the target pollutant is separated from soil particles and removed. The soil and the hot flue gas are separated in the indirect thermal desorption process, and the main components of the thermal desorption gas generated by heating are superheated steam, organic waste gas, dust and a small amount of air.
Aiming at the problem that thermal desorption gas treatment is always a technical difficulty, the current common technology is to spray and wash with circulating water, then adsorb with active carbon and finally discharge. Most superheated steam and organic waste gas are condensed into liquid in the spraying and washing process and enter circulating water to form organic waste water, uncondensed steam, organic waste gas and a small amount of air are adsorbed by activated carbon, and finally the remaining non-condensable gas is discharged to the atmosphere, wherein most dust enters the circulating water through spraying and washing, and a small amount of dust passes through the activated carbon and is finally discharged to the atmosphere. The problems with this technique are:
(1) cooling scrubbing and adsorption do not remove all organic waste gases (e.g., low boiling point organics such as methane, ethane, benzene, etc.); (2) the concentration of organic matters in the circulating water is continuously increased and finally saturated, and the washing function is lost, so that the purification of organic waste gas is ineffective; (3) dust enters circulating water and is accumulated continuously, so that solid impurities in the circulating water are increased, a circulating pipeline is blocked finally, and a system frequently breaks down; (3) the active carbon is easily blocked by condensed water and dust, and loses the adsorption capacity; (4) the activated carbon with saturated adsorption can generate secondary pollution.
The reason for adopting the thermal desorption gas treatment technology is as follows:
(1) the temperature of thermal desorption gas generated by the thermal desorption soil remediation system is 100-500 ℃, and the dust concentration is usually more than or equal to 3000mg/m3The characteristics of high upper limit of temperature, large temperature fluctuation, high dust concentration and the like exist; (2) the upper limit of the temperature is as high as 500 ℃, the temperature resistance of the common precise filter bag type dust removal is not more than 200 ℃, meanwhile, the temperature fluctuation is large, especially, the lower limit of the temperature is as low as 100 ℃, superheated steam is easily saturated and condensed into liquid drops to block a filter bag, and even if a high-temperature filter dust removal technology is used, the problem that the filter bag is blocked by condensate cannot be avoided. Therefore, the dust removal measures for the thermal desorption gas can only adopt a coarse dust removal mode such as cyclone dust removal; (3) the dust concentration of the thermal desorption gas is high, the dust removal efficiency of the coarse dust removal mode is generally less than 70 percent, and the dust concentration after the coarse dust removal is still as high as 900mg/m3Above, spray washing is therefore commonly used to further reduce dust concentration; (4) the dust blocking resistance of the conventional heat exchanger is generally less than or equal to 150mg/m3Therefore, the thermal desorption gas after coarse dust removal does not meet the requirements of the conventional heat exchanger; (5) the heat exchanger with strong dust resistance has the advantages that most of heat exchange efficiency must be sacrificed in order to resist blockage, so that the heat exchange capability is weak, the equipment scale is large, the heat exchanger with strong dust resistance is unreasonable to treat the thermal desorption gas, and even if the dust concentration of the thermal desorption gas after coarse dust removal is still high, the heat exchanger with strong dust resistance still needs to be used.
In recent years, the control of the emission of atmospheric pollutants in China is more and more strict, and the emission concentration of dust is required to be lower than 120mg/m according to GB16297 Integrated emission Standard of atmospheric pollutants3The emission concentration of organic substances is generally required to be lower than 60mg/m3。
The application number is CN201610543589.9 contaminated soil repair system, including thermal desorption device, filter core adsorption equipment, fan, packed tower and indicator tank that communicate in proper order through the pipeline; the thermal desorption device comprises a furnace chamber, a fuel gas heating assembly, an air inlet valve positioned on the side wall of the furnace chamber and a heat pipe positioned in the furnace chamber; the top of the furnace chamber is communicated with the filter element adsorption device through a pipeline. An air heat exchanger is also arranged on the pipeline between the thermal desorption device and the filter element adsorption device. The main methods for treating the thermal desorption gas in the patent are heat exchanger cooling and filter element adsorption, and the problems that the low-boiling-point organic waste gas cannot be thoroughly purified, necessary purification measures are lacked for dust, and the risk that the organic matters and the dust in the finally discharged tail gas exceed the standard is high.
Application number is CN201910263915.4 soil thermal desorption dystopy repair system, including thermal desorption section of thick bamboo, cyclone, soil collection device, tail gas combustor and preheating air supply arrangement. An ultrasonic generator and a microwave heater are arranged in the thermal desorption. This patent is equipped with cyclone and purifies the dust, but it is known that cyclone as a coarse dust collector, its dust collection efficiency is low, and is not good to the treatment effect of small-particle size dust especially, hardly satisfies the dust and discharges concentration requirement.
The thermal desorption mechanism comprises a thermal desorption channel, a soil crushing mechanism, an electric heating rod, a cyclone separator, a heat exchanger and an air blower, and is characterized in that thermal desorption is carried out after soil is crushed, and dust is removed from gas generated by the thermal desorption. The patent also has the problems that the cyclone separator cannot remove dust thoroughly, the dust concentration at the inlet of the heat exchanger is high, the heat exchanger is easy to block, and the like. And the organic matter is not thoroughly purified only by the cyclone separator and the heat exchanger.
From the above analysis, it can be seen that the thermal desorption gas treatment difficulty is large and the technical problem is complex. The existing thermal desorption gas purification technology has the problems that organic matters and dust are not thoroughly purified, the requirement of tail gas emission cannot be met, the purification device is blocked due to excessive dust, secondary pollution can be generated due to activated carbon adsorption, and the like.
Disclosure of Invention
The invention aims to solve the technical problems of the prior art, provides a comprehensive treatment method of overheating temperature adjustment, high-temperature dust removal, cooling, condensation and thermal oxidation aiming at the defects of the prior art, and solves the problems of incomplete tail gas purification, large dust amount, easy blockage, secondary pollution and the like in the traditional indirect thermal desorption gas treatment process.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
the indirect thermal desorption gas treatment device for the soil is characterized by comprising a superheater, a high-temperature dust remover, a high-temperature cooler, a condenser and a thermal oxidizer which are sequentially connected through pipelines;
a cold side air inlet of the superheater is connected with an indirect thermal desorption soil remediation system so as to introduce soil indirect thermal desorption gas to be treated;
the air inlet of the high-temperature dust remover is connected with the air outlet of the cold side of the superheater, and the soil indirect thermal desorption gas heated by the superheater is subjected to high-temperature dust removal to remove most of dust;
the hot side of the high-temperature cooler is connected with the dedusted thermal desorption gas, and the cold side of the high-temperature cooler is provided with normal-temperature air by an air blower and exchanges heat with the dedusted thermal desorption gas through the normal-temperature air; the cooled thermal desorption gas enters a subsequent condenser; the preheated air directly enters a subsequent thermal oxidizer through a pipeline to provide a combustion atmosphere for the thermal oxidizer;
the condenser is connected with a circulating cooling water device, a high-temperature medium at the hot side of the condenser is thermal desorption gas coming out of the high-temperature cooler, and a low-temperature medium at the cold side of the condenser is circulating water introduced from the circulating cooling water device; the condenser is also connected with an external organic wastewater collecting device and is used for collecting the organic wastewater generated by liquefaction in the condenser;
the air inlet of the thermal oxidizer is respectively connected with the condenser and the high-temperature cooler and is provided with a fuel supplementing port, a high-temperature field is formed by internal combustion, the air outlet of the thermal oxidizer is connected with the indirect thermal desorption soil remediation system and the superheater, the non-condensable gas led in from the condenser is combusted at high temperature to form high-temperature flue gas, one part of the high-temperature flue gas is used as a heat source in the superheater and is used for heating the indirect thermal desorption gas coming out of the thermal desorption soil remediation system, and the rest part of the high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system for;
a first temperature measuring instrument is arranged on a connecting pipeline between the superheater and the high-temperature dust remover, a flow control valve is arranged on a connecting pipeline between the thermal oxidizer and the superheater, and the flow of high-temperature flue gas entering the superheater is adjusted according to temperature information fed back by the first temperature measuring instrument;
a second temperature measuring instrument is arranged on a connecting pipeline between the high-temperature cooler and the condenser, and the normal-temperature air flow introduced into the high-temperature cooler by the air blower is adjusted according to the temperature information fed back by the second temperature measuring instrument;
and a third temperature measuring instrument is arranged on a connecting pipeline of the condenser and the thermal oxidizer, a circulating water flow valve is arranged on a circulating cooling water device pipeline, and the flow of circulating cooling water entering the condenser is adjusted according to temperature information fed back by the third temperature measuring instrument.
Further, the first temperature detector and the flow control valve are connected to the overheating control module; the overheating control module comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and the flow of high-temperature flue gas entering the superheater is adjusted by controlling a flow control valve according to temperature information fed back by the first temperature measuring instrument;
the second temperature measuring instrument and the blower are connected to the cooling control module; the cooling control module comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of the normal temperature air introduced into the high-temperature cooler by controlling the power of the air blower according to the temperature information fed back by the second temperature measuring instrument;
the third temperature measuring instrument and the circulating water flow valve are connected to the condensation control module; the condensation control module comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of circulating cooling water entering the condenser by controlling a circulating water flow valve according to temperature information fed back by a third temperature measuring instrument.
The heat control module, the cooling control module and the condensation control module are all existing industrial automatic control modules, the working principle is that the flow sensor collects flow information, the flow information is converted into an electric signal through the converter, and the AD converter converts the analog electric signal into a discrete signal and transmits the discrete signal to the single chip microcomputer. The single chip microcomputer software system processes the acquired flow information and temperature information according to a preset value and outputs a discrete control signal. The DA converter converts the discrete control signal into analog electric quantity. The action of the valve and the power of the air blower are controlled by simulating electric quantity, so that the flow is adjusted, and the accurate control of the flow is realized.
Specifically, the superheater is a dividing wall type heater, the heating form adopts a vertical tube type, the distance between internal heat exchange tubes is more than or equal to 40mm, and a mechanical rapping device is arranged to remove dust on the surfaces of the heat exchange tubes.
The high-temperature dust collector adopts a metal filter bag or a ceramic filter tube as a dust-collecting filter material, the porosity is more than or equal to 80 percent, and the aperture is less than or equal to 1 um. In the field of superheated steam purification, it is generally considered that a fine filtering manner such as a metal filter bag or a ceramic filter tube is not feasible, because once the temperature of superheated steam is improperly controlled, droplets are easily condensed out, so that fine filter holes are blocked, and the filtering and dedusting functions are disabled. The invention can effectively avoid the formation of condensed liquid drops by strictly controlling the temperature of the superheated steam entering the high-temperature dust remover.
The high-temperature cooler is a dividing wall type cooler, the cooling form is a tube type, a plate type or a spiral plate type, and the distance between internal heat exchange tubes or heat exchange plates is more than or equal to 20 mm.
The condenser is a dividing wall type condenser and adopts a plate type heat exchanger, the condensing form adopts a tube type, a plate type or a spiral plate type, the distance between internal heat exchange tubes or heat exchange plates is more than or equal to 20mm, and the dust resistance is more than 100mg/m3。
The circulating cooling water device consists of a circulating pump, a water tank and a radiator, and the radiator adopts a dividing wall type heat exchange.
The thermal oxidizer is a direct-fired thermal oxidizer.
The invention also provides a method for carrying out indirect thermal desorption gas treatment on soil by adopting the device, which comprises the following steps:
(1) sending indirect thermal desorption gas generated by the indirect thermal desorption soil remediation system into a superheater for heating temperature control treatment, wherein the temperature of the thermal desorption gas after heating temperature control by the superheater is 350-550 ℃;
(2) the thermal desorption gas heated by the superheater and controlled in temperature is sent to high temperatureThe dust collector is used for removing most of dust to ensure that the dust content is less than or equal to 30mg/m3；
(3) Enabling the high-temperature dedusted thermal desorption gas to enter a high-temperature cooler through a pipeline, introducing normal-temperature air into the high-temperature cooler, performing heat exchange between the thermal desorption gas and the normal-temperature air to cool the thermal desorption gas to 120-150 ℃, introducing preheated air into a thermal oxidizer, and introducing the cooled thermal desorption gas into a condenser;
(4) introducing normal-temperature clean water serving as a low-temperature medium into the condenser through a circulating cooling water device, performing heat exchange with thermal desorption gas in the condenser, condensing superheated steam and organic waste gas in the thermal desorption gas into liquid, and collecting the liquid through an organic wastewater collecting device; cooling the rest non-condensable gas to be less than or equal to 60 ℃ and introducing the cooled non-condensable gas into a thermal oxidizer;
(5) and a small amount of fuel is replenished to the thermal oxidizer again, preheated air introduced by the high-temperature cooler is used as atmosphere, a high-temperature field is formed by combustion, the non-condensable gas is oxidized and decomposed at high temperature to form high-temperature flue gas with the temperature of more than or equal to 850 ℃, one part of the high-temperature flue gas is used as a heat source in the superheater and is used for heating indirect thermal desorption gas coming out of the thermal desorption soil remediation system, and the rest part of the high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system for recycling.
Wherein in the step (1), the temperature of thermal desorption gas generated by the thermal desorption soil remediation system is 100-500 ℃, and the dust concentration is more than or equal to 3000mg/m3。
Has the advantages that:
the invention forms a comprehensive treatment method of overheating temperature adjustment, high-temperature dust removal, cooling, condensation and thermal oxidation, solves the problems of large temperature fluctuation of thermal desorption temperature and blockage of a filter bag by condensate, and provides conditions for high-temperature precise filtration and dust removal; the superheater is a heat exchanger with strong dust resistance, but the use working condition of the superheater is low heat exchange coefficient under large temperature difference, and the required heat exchange efficiency is not high, so that the equipment scale is controllable; on one hand, the high-temperature dust removal device effectively removes dust, ensures that dust in tail gas reaches the standard, and simultaneously reduces the fault risk of subsequent cooling, condensation and thermal oxidation links; the two-stage cooling measures of cooling and condensation are adopted, so that most of organic matters are purified and removed, the tail gas load of thermal oxidation treatment is reduced, and meanwhile, heat recovery and utilization are realized; organic waste gas in the thermal oxidizer is thoroughly purified, the tail gas is ensured to be discharged up to the standard, and meanwhile, high-temperature flue gas generated by thermal oxidation provides a heat source for repairing front-end thermal desorption soil, so that waste heat utilization is realized. The treatment device effectively solves the problems of incomplete tail gas purification, large dust amount, easy blockage, secondary pollution and the like in the traditional indirect thermal desorption gas treatment process while saving energy consumption.
Drawings
The foregoing and/or other advantages of the invention will become further apparent from the following detailed description of the invention when taken in conjunction with the accompanying drawings.
Fig. 1 is a schematic block diagram of a soil indirect thermal desorption gas treatment device in embodiment 1.
Fig. 2 is a schematic block diagram of the indirect thermal desorption gas treatment device for soil in embodiment 2.
Wherein each reference numeral represents:
1 an indirect thermal desorption soil remediation system; 2, a superheater; 3, a high-temperature dust remover; 31 a dust collection tank; 4, a high-temperature cooler; 5, a condenser; 6 a thermal oxidizer; 7, a first temperature measuring instrument; 8, a second temperature measuring instrument; 9 a third temperature measuring instrument; 10 flow control valves; 11 a blower; 12 circulating cooling water device; 13 circulating water flow valve; 14 a superheat control module; 15 cooling the control module; 16 condensation control module.
Detailed Description
The invention will be better understood from the following examples.
The structures, proportions, and dimensions shown in the drawings and described in the specification are for understanding and reading the present disclosure, and are not intended to limit the scope of the present disclosure, which is defined in the claims, and are not essential to the skilled in the art. In addition, the terms "upper", "lower", "front", "rear" and "middle" used in the present specification are for clarity of description, and are not intended to limit the scope of the present invention, and the relative relationship between the terms and the relative positions may be changed or adjusted without substantial technical changes.
Example 1
As shown in fig. 1, the indirect thermal desorption gas treatment device for soil comprises a superheater 2, a high-temperature dust remover 3, a high-temperature cooler 4, a condenser 5 and a thermal oxidizer 6 which are connected in sequence through pipelines.
Wherein the heat exchanger 2 adopts a floating head type heat exchanger, the model is AES325-0.6-30-3/25-21, the nominal diameter is 325, the design pressure is 0.6MPa, and the heat exchange area is 30m2The length of the tube is 3m, and the number of tube passes is 2.
The high-temperature dust remover 3 adopts a pulse single-machine dust remover, model HMC-80, and treats air volume 4000 and 4500m3H, filtration area 62m2And the filtering wind speed is 1.1-1.25 m/min.
The high-temperature cooler 4 adopts a spiral plate heat exchanger with the model number BLC of 0.6-32-1.0/800-20/24, the distance between two spiral channel plates is 20mm and 24mm respectively, the nominal pressure is 0.6MPa, the nominal diameter is 800mm, and the heat exchange area is 32m2。
The condenser 5 adopts a spiral plate heat exchanger with model number BLC of 0.6-50-1.0/1000-20/24, the distance between two spiral channel plates is 20mm and 24mm respectively, the nominal pressure is 0.6MPa, the nominal diameter is 1000mm, and the heat exchange area is 50m2。
The thermal oxidizer 6 adopts a direct-fired thermal oxidation furnace with model TO-800 and rated treatment air volume of 800-1000 m3The rated heating temperature is 850 ℃, and the design pressure is 0.6 MPa.
A cold side air inlet of the superheater 2 is connected with the existing indirect thermal desorption soil remediation system 1 so as to introduce the soil indirect thermal desorption gas to be treated; the air inlet of the high-temperature dust remover 3 is connected with the air outlet of the cold side of the superheater 2, and the soil indirect thermal desorption gas heated by the superheater 2 is subjected to high-temperature dust removal to remove most of dust and is concentrated in the dust collection tank 31 for centralized treatment; the hot side of the high-temperature cooler 4 is connected with the dedusted thermal desorption gas, and the cold side of the high-temperature cooler is provided with normal-temperature air by an air blower 11, and the normal-temperature air exchanges heat with the dedusted thermal desorption gas; the cooled thermal desorption gas enters a subsequent condenser 5; the preheated air directly enters the subsequent thermal oxidizer 6 through a pipeline to provide the combustion atmosphere of the thermal oxidizer; the condenser 5 is connected with a circulating cooling water device 12, a high-temperature medium at the hot side of the condenser 5 is thermal desorption gas coming out of the high-temperature cooler 4, and a low-temperature medium at the cold side is circulating water introduced from the circulating cooling water device 12; the condenser 5 is also connected with an external organic wastewater collecting device 51 for collecting the organic wastewater generated by liquefaction in the condenser; an air inlet of the thermal oxidizer 6 is respectively connected with the condenser 5 and the high-temperature cooler 4, a fuel supplementing port is arranged, a high-temperature field is formed through internal combustion, an air outlet of the thermal oxidizer 6 is connected with the indirect thermal desorption soil remediation system 1 and the superheater 2, non-condensable gas led in from the condenser 5 is combusted at high temperature, a part of formed high-temperature flue gas is used as a heat source in the superheater 2 and is used for heating indirect thermal desorption gas coming out of the thermal desorption soil remediation system 1, and the rest part of formed high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system 1 for recycling.
A first temperature measuring instrument 7 is arranged on a connecting pipeline between the superheater 2 and the high-temperature dust remover 3, a flow control valve 10 is arranged on a connecting pipeline between the thermal oxidizer 6 and the superheater 2, and the flow of high-temperature flue gas entering the superheater 2 is adjusted according to temperature information fed back by the first temperature measuring instrument 7; a second temperature measuring instrument 8 is arranged on a connecting pipeline between the high-temperature cooler 4 and the condenser 5, and the normal-temperature air flow introduced into the high-temperature cooler 4 by the air blower 11 is adjusted according to the temperature information fed back by the second temperature measuring instrument 8; and a third temperature measuring instrument 9 is arranged on a connecting pipeline of the condenser 5 and the thermal oxidizer 6, a circulating water flow valve 13 is arranged on a circulating cooling water device 12 pipeline, and the flow of circulating cooling water entering the condenser 5 is adjusted according to temperature information fed back by the third temperature measuring instrument 9.
Example 2
As a modification to embodiment 1, the first thermometer 7 and the flow control valve 10 are connected to the overheating control module 14; the heat control module 14 comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of the high-temperature flue gas entering the superheater 2 by controlling the flow control valve 10 according to the temperature information fed back by the first temperature measuring instrument 7.
Connecting the second thermometer 8 and the blower 11 to the cooling control module 15; the cooling control module 15 comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of the normal temperature air introduced into the high temperature cooler 4 by controlling the power of the air blower 11 according to the temperature information fed back by the second temperature measuring instrument 8.
Connecting the third temperature detector 9 and the circulating water flow valve 13 to the condensation control module 16; the condensation control module 16 comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and regulates the flow of circulating cooling water entering the condenser 5 by controlling the circulating water flow valve 13 according to the temperature information fed back by the third temperature measuring instrument 9.
The heat control module, the cooling control module and the condensation control module are all existing industrial automatic control modules, the working principle is that the flow sensor collects flow information, the flow information is converted into an electric signal through the converter, and the AD converter converts the analog electric signal into a discrete signal and transmits the discrete signal to the single chip microcomputer. The single chip microcomputer software system processes the acquired flow information and temperature information according to a preset value and outputs a discrete control signal. The DA converter converts the discrete control signal into analog electric quantity. The action of the valve and the power of the air blower are controlled by simulating electric quantity, so that the flow is adjusted, and the accurate control of the flow is realized.
The input of the overheating control module, the input of the cooling control module and the input of the condensation control module adopt Yutai science and technology (UTEK) UT5508, and the output of the condensation control module adopts Yutai science and technology (UTEK) UT 5564A.
Example 3
Treatment of indirect thermal desorption gas from soil using the apparatus described in example 2
The organic contaminated soil is heated in indirect thermal desorption to produce thermal desorption gas, the main components of which are superheated steam, organic waste gas, dust and a small amount of air, and which needs to be purified. The temperature of the thermal desorption gas is usually 100-500 ℃, and the dust content is more than or equal to 3000mg/m3. The thermal desorption gas firstly enters a superheater which is a dividing wall type heater, the heating form adopts a vertical tube type, the distance between internal heat exchange tubes is 40mm, and the superheater is provided with a mechanical rapping device to clear the surface of the heat exchange tubesDust; and a temperature measuring instrument is arranged at the outlet of the superheater and is connected with a superheating control module in the temperature control system, and the control module controls the temperature of the thermal desorption gas heated and controlled by the heater to be 350-550 ℃ by adjusting the flow of part of high-temperature flue gas from the outlet of the thermal oxidizer.
The thermal desorption gas after the overheating temperature control enters a high-temperature dust removal device, and the dust removal device adopts Al2O3And SiO2The ceramic filter tube which is the main component has the porosity of more than or equal to 80 percent, the aperture of less than or equal to 1um and the dust removal efficiency of more than 99 percent, can resist high-temperature thermal desorption gas at the temperature of between 350 and 600 ℃ by combining a high-temperature resistant stainless steel shell, and simultaneously reduces the dust content in waste gas to less than or equal to 30mg/m3。
The gas after high-temperature dust removal enters a high-temperature cooler through a pipeline, the high-temperature cooler is a dividing wall cooler, a high-temperature medium at the hot side is not in contact with a low-temperature medium at the cold side, the dividing wall conducts heat, the cooler adopts a finned tube type, the space between internal heat exchange tubes or heat exchange plates is 22mm, and the dust resistance is more than 100mg/m3Thus ensuring no clogging by dust in the thermal desorption gas. The cold side is provided with normal temperature air by an air blower, the inlet temperature is normal temperature, and the outlet temperature is 120-150 ℃. The hot side is the hot desorption gas after dust removal, the inlet temperature of the hot desorption gas is 350-550 ℃, the outlet is provided with a temperature measuring instrument, the temperature measuring instrument is connected with a cooling control module in a temperature control system, the control module controls the air quantity entering a high-temperature cooler through the variable frequency speed regulation of an air blower, so that the outlet temperature of the hot desorption gas after being cooled by the high-temperature cooler is controlled to be 150-300 ℃, the hot desorption device cannot be condensed at the temperature, and the waste heat is recovered as far as possible on the premise of avoiding dew point corrosion.
The high-temperature cooled thermal desorption gas enters a condenser through a pipeline, the condenser is a dividing wall condenser, a hot-side high-temperature medium is not in contact with a cold-side low-temperature medium, and the dividing wall conducts heat. The hot side is thermal desorption gas at 150-300 ℃, and the cold side is circulating cooling water. After heat exchange, the temperature of the thermal desorption gas is reduced to be below 60 ℃, more than 85% of superheated steam and organic waste gas are condensed into liquid state to form organic wastewater, and the organic wastewater is collected and treated. The condenser adopts a plate heat exchanger, the thickness of a plate is only 0.6mm, and a plurality of waves are addedThe heat exchange coefficient is large, the cost is high, the efficiency is high, the plate interval is 22mm, and the dust resistance is more than 100mg/m3Thus ensuring no clogging by dust in the thermal desorption gas. Similarly, a temperature measuring instrument is arranged at the outlet of the hot side of the condenser and is connected with a condensation control module in the temperature control system, and the control module controls the temperature of the thermal desorption gas cooled by the condenser to be reduced to below 60 ℃ by adjusting the flow rate of circulating cooling water.
The outlet of the condenser is the rest non-condensable gas with a concentration less than 15%, the main components of the non-condensable gas are air, saturated steam and low-boiling-point non-condensable organic matters, and the dust concentration is less than or equal to 30mg/m3. The non-condensable gas enters a thermal oxidizer through a pipeline, a small amount of fuel is supplemented to the thermal oxidizer, air is preheated at 120-150 ℃ by a high-temperature cooler, a high-temperature field with the temperature of more than or equal to 850 ℃ is formed by combustion, and the non-condensable gas is thoroughly oxidized and decomposed at high temperature to form carbon dioxide and steam.
The condenser is provided with a circulating cooling water device which consists of a circulating pump, a water tank and a radiator, wherein the inlet temperature of circulating water is 30-40 ℃, and the outlet temperature of circulating water is 35-60 ℃. Because the circulating medium adopts clean water, the heat exchange of the partition walls does not contact with organic waste gas and dust, so that the heat exchange device does not contain solid impurities, and the problems of pipeline blockage and the like do not occur.
The preheated air in the combination of the high-temperature heat exchanger and the thermal oxidizer has the effect of preheating and utilizing, and the energy consumption can be obviously reduced. The high-temperature flue gas generated by fuel combustion in the thermal oxidizer and the flue gas generated by oxidative decomposition of non-condensable gas are mostly sent back to the front-end soil thermal desorption system to be used as heat sources, a small amount of indirect thermal desorption gas passes through the superheater to heat the outlet of the thermal desorption soil remediation system, and then the indirect thermal desorption gas is used as the heat sources in the thermal desorption soil remediation system for recycling. The two energy-saving measures can save the fuel by more than 40 percent.
Comparative example 1
The traditional spray washing method is adopted. The temperature is 100-500 ℃, and the dust content is more than or equal to 3000mg/m3The thermal desorption gas is firstly washed by circulating water spraying to remove 80-90% of dust and about 50-60% of organic matters, and simultaneously, the temperature is reduced to be below 80 ℃, about 30% of non-condensable gas is remained, and then the gas is absorbed by active carbon,about 10-20% of organic matters are removed, and about 15% of the residual tail gas is directly discharged. Wherein circulating water device includes circulating pump, water tank and radiator, has solid particulate matter and organic matter after the circulating water washes, along with the concentration of repeated circulation washing is higher and higher, becomes the high concentration and is organic waste water, leads to easily blockking up circulating pump, radiator cold side, pipeline, shower nozzle etc. in the circulating water flow. The heat radiator directly radiates the heat carried by the thermal desorption gas to the atmosphere without heat recycling. Activated carbon is easy to adsorb moisture and intercept part of dust to become dangerous waste after saturation.
Comparative example 2
The temperature is 100-500 ℃, and the dust content is more than or equal to 3000mg/m3The thermal desorption gas is subjected to cyclone dust removal to remove about 70% of dust, then is cooled to below 80 ℃ by a cooler, is combusted at high temperature by a thermal oxidizer to generate high-temperature flue gas of 850 ℃, and is sent to a front-end thermal desorption device to serve as a heat source to realize partial recovery of heat. The cooler adopts circulating water dividing wall heat exchange, and circulating medium is clean water, so that blockage of a circulating pump, a radiator cold side, a pipeline, a spray head and the like in a circulating water flow cannot be caused. However, the cyclone dust removal efficiency is insufficient, and the concentration of tail gas dust is high, which can cause the blockage of the pipeline at the hot side of the thermal oxidizer and the radiator.
The treatment effects of example 3 and comparative examples 1 and 2 are shown in table 1.
TABLE 1
As can be seen from the comparison effect of the table 1, the treatment method combining overheating temperature adjustment, high-temperature dust removal, cooling, condensation and thermal oxidation effectively solves the problems of incomplete tail gas purification, large dust amount, easy blockage, secondary pollution and the like in the traditional indirect thermal desorption gas treatment process.
The present invention provides a device and a method for treating soil indirect thermal desorption gas, and a method and a means for implementing the technical scheme are numerous, the above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be regarded as the protection scope of the present invention. All the components not specified in the present embodiment can be realized by the prior art.
Claims (9)
1. The indirect thermal desorption gas treatment device for the soil is characterized by comprising a superheater (2), a high-temperature dust remover (3), a high-temperature cooler (4), a condenser (5) and a thermal oxidizer (6) which are sequentially connected through pipelines;
a cold side air inlet of the superheater (2) is connected with the indirect thermal desorption soil remediation system (1) to introduce soil indirect thermal desorption gas to be treated;
an air inlet of the high-temperature dust remover (3) is connected with an air outlet at the cold side of the superheater (2), and the soil indirect thermal desorption gas heated by the superheater (2) is subjected to high-temperature dust removal to remove most of dust;
the hot side of the high-temperature cooler (4) is connected with the dedusted thermal desorption gas, and the cold side of the high-temperature cooler is provided with normal-temperature air by an air blower (11) and exchanges heat with the dedusted thermal desorption gas through the normal-temperature air; the cooled thermal desorption gas enters a subsequent condenser (5); the preheated air directly enters the subsequent thermal oxidizer (6) through a pipeline to provide combustion atmosphere for the thermal oxidizer (6);
the condenser (5) is connected with a circulating cooling water device (12), a high-temperature medium at the hot side of the condenser (5) is thermal desorption gas coming out of the high-temperature cooler (4), and a low-temperature medium at the cold side is circulating water introduced from the circulating cooling water device (12); the condenser (5) is also connected with an external organic wastewater collecting device (51) for collecting the organic wastewater generated by liquefaction in the condenser (5);
the air inlet of the thermal oxidizer (6) is respectively connected with the condenser (5) and the high-temperature cooler (4), and is provided with a fuel supplementing port, a high-temperature field is formed by internal combustion, the air outlet of the thermal oxidizer (6) is connected with the indirect thermal desorption soil remediation system (1) and the superheater (2), the non-condensable gas led in from the condenser (5) is combusted at high temperature to form high-temperature flue gas, one part of the high-temperature flue gas is used as a heat source in the superheater (2) and is used for heating the indirect thermal desorption gas coming out of the thermal desorption soil remediation system (1), and the rest part of the high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system (1) for;
a first temperature measuring instrument (7) is arranged on a connecting pipeline between the superheater (2) and the high-temperature dust remover (3), a flow control valve (10) is arranged on a connecting pipeline between the thermal oxidizer (6) and the superheater (2), and the flow of high-temperature flue gas entering the superheater (2) is adjusted according to temperature information fed back by the first temperature measuring instrument (7);
a second temperature measuring instrument (8) is arranged on a connecting pipeline between the high-temperature cooler (4) and the condenser (5), and the normal-temperature air flow introduced into the high-temperature cooler (4) by the air blower (11) is adjusted according to the temperature information fed back by the second temperature measuring instrument (8);
and a third temperature measuring instrument (9) is arranged on a connecting pipeline between the condenser (5) and the thermal oxidizer (6), a circulating water flow valve (13) is arranged on a pipeline of the circulating cooling water device (12), and the flow of circulating cooling water entering the condenser (5) is adjusted according to temperature information fed back by the third temperature measuring instrument (9).
2. The indirect soil thermal desorption gas treatment device according to claim 1, wherein the first temperature detector (7) and the flow control valve (10) are connected to a superheating control module (14); the overheating control module (14) comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of high-temperature flue gas entering the superheater (2) by controlling a flow control valve (10) according to temperature information fed back by the first temperature measuring instrument (7);
the second temperature measuring instrument (8) and the blower (11) are connected to a cooling control module (15); the cooling control module (15) comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of the normal temperature air introduced into the high-temperature cooler (4) by controlling the power of the air blower (11) according to the temperature information fed back by the second temperature measuring instrument (8);
the third temperature measuring instrument (9) and the circulating water flow valve (13) are connected to the condensation control module (16); the condensation control module (16) comprises a flow sensor, an AD-DA converter and a single chip microcomputer, and adjusts the flow of circulating cooling water entering the condenser (5) by controlling a circulating water flow valve (13) according to temperature information fed back by the third temperature measuring instrument (9).
3. The soil indirect thermal desorption gas treatment device according to claim 1 or 2, wherein the superheater (2) is a dividing wall type heater, the heating form adopts a vertical pipe type, the distance between internal heat exchange pipes is more than or equal to 40mm, and a mechanical rapping device is provided for removing dust on the surfaces of the heat exchange pipes.
4. The indirect soil thermal desorption gas treatment device according to claim 1 or 2, wherein the high-temperature dust collector (3) adopts a metal filter bag or a ceramic filter tube as a dust-collecting filter material, the porosity is more than or equal to 80%, and the pore diameter is less than or equal to 1 um.
5. The indirect soil thermal desorption gas treatment device according to claim 1 or 2, wherein the high-temperature cooler (4) is a dividing wall type cooler, the cooling form is a tube type, a plate type or a spiral plate type, and the distance between internal heat exchange tubes or heat exchange plates is more than or equal to 20 mm.
6. The indirect thermal desorption gas treatment device for soil as claimed in claim 1 or 2, wherein the condenser (5) is a dividing wall type condenser, a plate type heat exchanger is adopted, the condensing form is a tube type, a plate type or a spiral plate type, the distance between internal heat exchange tubes or heat exchange plates is more than or equal to 20mm, and the dust resistance is more than 100mg/m3。
7. The indirect thermal desorption gas treatment plant of soil according to claim 1 or 2, wherein the thermal oxidizer (6) is a direct-fired thermal oxidizer.
8. A method for indirect thermal desorption gas treatment of soil by using the device of claim 1, which comprises the following steps:
(1) sending indirect thermal desorption gas generated by the indirect thermal desorption soil remediation system into a superheater for heating temperature control treatment, wherein the temperature of the thermal desorption gas after heating temperature control by the superheater is 350-550 ℃;
(2) sending the thermal desorption gas heated and controlled by the superheater into a high-temperature dust remover for dust removal treatment to remove most of dust so that the dust content is less than or equal to 30mg/m3；
(3) Enabling the high-temperature dedusted thermal desorption gas to enter a high-temperature cooler through a pipeline, introducing normal-temperature air into the high-temperature cooler, performing heat exchange between the thermal desorption gas and the normal-temperature air to cool the thermal desorption gas to 120-150 ℃, introducing preheated air into a thermal oxidizer, and introducing the cooled thermal desorption gas into a condenser;
(4) introducing normal-temperature clean water serving as a low-temperature medium into the condenser through a circulating cooling water device, performing heat exchange with thermal desorption gas in the condenser, condensing superheated steam and organic waste gas in the thermal desorption gas into liquid, and collecting the liquid through an organic wastewater collecting device; cooling the rest non-condensable gas to be less than or equal to 60 ℃ and introducing the cooled non-condensable gas into a thermal oxidizer;
(5) and a small amount of fuel is replenished to the thermal oxidizer again, preheated air introduced by the high-temperature cooler is used as atmosphere, a high-temperature field is formed by combustion, the non-condensable gas is oxidized and decomposed at high temperature to form high-temperature flue gas with the temperature of more than or equal to 850 ℃, one part of the high-temperature flue gas is used as a heat source in the superheater and is used for heating indirect thermal desorption gas coming out of the thermal desorption soil remediation system, and the rest part of the high-temperature flue gas is used as a heat source in the thermal desorption soil remediation system for recycling.
9. The method for treating the soil indirect thermal desorption gas according to claim 8, wherein in the step (1), the temperature of the thermal desorption gas generated by the thermal desorption soil remediation system is 100-500 ℃, and the dust concentration is more than or equal to 3000mg/m3。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010021489.6A CN111054738A (en) | 2020-01-09 | 2020-01-09 | Soil indirect thermal desorption gas treatment device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010021489.6A CN111054738A (en) | 2020-01-09 | 2020-01-09 | Soil indirect thermal desorption gas treatment device and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111054738A true CN111054738A (en) | 2020-04-24 |
Family
ID=70306943
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010021489.6A Pending CN111054738A (en) | 2020-01-09 | 2020-01-09 | Soil indirect thermal desorption gas treatment device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111054738A (en) |
-
2020
- 2020-01-09 CN CN202010021489.6A patent/CN111054738A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102242946B (en) | Concentrated heat supply system for reclaiming smoke afterheat by absorption heat pump | |
| RU2580740C2 (en) | Method for cleaning synthesis gas from biomass at negative pressure to obtain oil products and configuration system thereof | |
| JP2014504548A (en) | Non-contact exhaust residual heat sludge drying system | |
| CN107327863A (en) | Suitable for the flue gas purification system and flue gas purifying method of gas turbine | |
| CN211537130U (en) | Adsorption and desorption device and system with dry gas backflow module | |
| CN211679286U (en) | Indirect thermal desorption gas processing apparatus of soil | |
| CN111408200A (en) | Waste gas treatment device used in kitchen waste biochemical treatment equipment | |
| CN110939940A (en) | Waste gas purification and waste heat recovery method and device thereof | |
| CN210045064U (en) | Device for efficiently treating mercury-containing polluted soil thermal desorption waste gas | |
| CN218442325U (en) | System for liquefying and separating oil in pyrolysis gas | |
| CN111054738A (en) | Soil indirect thermal desorption gas treatment device and method | |
| WO2012132003A1 (en) | Exhaust gas treatment system and exhaust gas treatment method | |
| CN208952142U (en) | A kind of smoke comprehensive processing unit | |
| CN103614509B (en) | A kind of carbon steel converter dry cloth bag dedusting process of whole process recovery waste heat and device thereof | |
| CN213288120U (en) | Near zero discharge system of soil thermal dehydration | |
| CN210145785U (en) | Deep dehumidification purification system for wet flue gas | |
| CN213272679U (en) | Ultra-low emission low-temperature white-removing system for waste incineration flue gas | |
| CN114110604A (en) | Pyrolysis method based on full-automatic garbage pyrolysis system | |
| WO2020233390A1 (en) | Evaporation device for treatment of low-heat-mass coal gas | |
| CN103539215A (en) | Sewage treatment system and process | |
| CN102212644A (en) | Converter gas cloth-bag purifying and recycling technology combining cooling extingiushment and heating dust removal | |
| CN207785983U (en) | A kind of desulfurization fume condensation water lift equipment | |
| CN2846429Y (en) | Pure dry type purifier for oxygen convertor smoke | |
| CN218931769U (en) | Desulfurization wastewater integrated treatment system | |
| CN210050826U (en) | Device for evaporating waste water by using boiler flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |