CN210107430U - Catalytic incineration treatment system suitable for treating volatile organic compound tail gas - Google Patents
Catalytic incineration treatment system suitable for treating volatile organic compound tail gas Download PDFInfo
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- CN210107430U CN210107430U CN201822209288.XU CN201822209288U CN210107430U CN 210107430 U CN210107430 U CN 210107430U CN 201822209288 U CN201822209288 U CN 201822209288U CN 210107430 U CN210107430 U CN 210107430U
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Abstract
The utility model relates to a be suitable for catalytic incineration processing system who handles volatile organic compounds tail gas, including the following equipment that connects gradually: the system comprises a gas-liquid separation tank for gas-liquid separation, a preheating device for heating waste gas, a first-stage catalytic oxidation reactor for catalytic oxidation reaction, a first-stage heat recovery device for recovering and utilizing waste gas heat generated after the first-stage catalytic oxygen reaction, a second-stage catalytic oxidation reactor for catalytic oxidation reaction, a second-stage heat recovery device for recovering and utilizing waste gas heat generated after the second-stage catalytic oxygen reaction, and a selective catalytic reduction reactor for performing selective catalytic reduction reaction on the waste gas generated after the second-stage catalytic oxidation reaction to eliminate nitrogen oxides. The utility model discloses be adapted to acrylonitrile absorption tower tail gas etc. contain volatile organic compounds and nitrogen oxide's exhaust-gas treatment, help reducing the energy consumption, convenient operation reduces the nitrogen oxide and discharges.
Description
Technical Field
The utility model relates to a catalytic incineration processing system still relates to this kind of exhaust treatment system's regulation control method, and this kind of exhaust treatment system is suitable for and handles volatile organic compounds tail gas, belongs to pollution control technical field, mainly is adapted to the exhaust treatment that contains volatile organic compounds and nitrogen oxide such as acrylonitrile absorption tower tail gas.
Background
In chemical production processes, a main production process often produces tail gas containing a large amount of volatile organic compounds, and the atmospheric environment is seriously polluted. For example, the production process of acrylonitrile adopts propylene ammoxidation technology, and uses propylene and ammonia as main raw materials to react under the action of a catalyst to generate acrylonitrile and other byproducts, and then acrylonitrile products are obtained through the process flows of quenching, recovery, refining and the like. An acrylonitrile absorption tower is arranged in the recovery process, the main components of tail gas discharged from the top of the tower are nitrogen, water vapor and carbon dioxide, and the tail gas contains a small amount of carbon monoxide, acrylonitrile, propylene, propane, trace hydrogen cyanide and the like, and the calorific value of the tail gas is about 820-343 kJ/Nm3Much less than 7880kJ/Nm3And (4) cannot be discharged into a flare system.
The main technical routes of the existing modes for treating the tail gas comprise an open flame burning method and a catalytic burning method, wherein the open flame burning method is to send the tail gas into a burning furnace for burning, which is a common treatment mode for the tail gas of a foreign acrylonitrile absorption tower, various organic matters in the tail gas are converted into inorganic matters such as carbon dioxide, water and the like through flame burning and are discharged into the atmosphere together, and the concentration of nitrogen oxides in the flue gas can be controlled by controlling the burning temperature and the excess air amount, so that the concentration of the nitrogen oxides meets the emission standard. The catalytic combustion method is to realize the oxidative decomposition of combustible components in the tail gas at relatively low temperature in a catalytic reactor, but because volatile organic compounds in the tail gas have high relative concentration and high heat release amount, and a catalyst is easy to sinter and inactivate, the concentration of the organic compounds in the waste gas to be treated is limited to a certain extent, the adaptability to the fluctuation of the concentration of the organic compounds is weak, the process control requirement is relatively high, the operation difficulty is high, a large amount of cold air needs to be introduced for cooling, relatively high energy consumption is generated, in addition, the emission of nitrogen oxides does not reach the standard, and certain pollution still exists to the atmospheric environment.
Organic matters VOCs in tail gas of an absorption tower for producing acrylonitrile mainly comprise propylene and propane, an acrylonitrile production device adopts different raw materials, the concentration of the organic matters in the tail gas is different, the existing raw materials mainly comprise three raw materials, the propylene with the purity of 99 percent is high in price, but the concentration of the organic matters in the tail gas is low; the propylene with the purity of 98 percent has moderate price of the raw material and higher concentration of organic matters in tail gas; the propylene with the purity of 96 percent has the lowest price of the raw material and the highest concentration of organic matters in the tail gas. The factory generally uses the raw materials with the propylene purity of 98%, the raw materials are mainly provided by an ethylene cracking device matched with the front end of the factory, if the propylene purity of 99% is provided, a plurality of separation and purification devices are required to be added in the ethylene cracking factory, and the investment and the manufacturing cost are increased. In the prior art, for the propylene purity of 98% or below, a large amount of dilution air is needed to be supplemented for cooling by adopting the traditional process flow, and even in this way, the temperature in a catalyst reactor is still high and is close to the limit use temperature of materials. Meanwhile, because a large amount of dilution air is supplemented, the power of the air supplementing fan is large, and because of the limitation of the efficiency of the plate heat exchanger, a large amount of hot air is discharged into a chimney, and heat energy is wasted.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides a be suitable for the catalytic incineration processing system who handles volatile organic compounds tail gas and regulation and control method thereof to reduce the energy consumption, convenient operation reduces the nitrogen oxide and discharges.
The technical scheme of the utility model is that: a catalytic incineration treatment system suitable for treating volatile organic tail gas, comprising:
the gas-liquid separation tank is used for separating water from waste gas, and is provided with a waste gas inlet, a waste gas outlet and a sewage discharge port, wherein the waste gas inlet is used for connecting a waste gas input pipeline of the system, and the sewage discharge port is provided with a sewage discharge valve for controlling sewage discharge;
the gas-gas heat exchanger is used for preheating the waste gas by taking the waste gas discharged by the selective catalytic reduction reactor as a heat release medium, and is provided with a heat release medium inlet and a heat release medium outlet, and the inlet of the gas-gas heat exchanger is connected with the waste gas outlet of the gas-liquid separation tank;
the first-stage catalytic oxidation reactor is used for the catalytic oxidation reaction of the preheated waste gas, and an inlet of the first-stage catalytic oxidation reactor is connected with an outlet of the gas-gas heat exchanger;
the first-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the first-stage catalytic oxygen reaction as a heat release medium to reduce the temperature of the waste gas, and an inlet of the heat release medium is connected with an outlet of the first-stage catalytic oxidation reactor;
the second-stage catalytic oxidation reactor is used for carrying out catalytic oxidation reaction on the waste gas after the first-stage catalytic oxidation reaction, and an inlet of the second-stage catalytic oxidation reactor is connected with a heat release medium outlet of the first-stage heat recovery device;
the second-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the second-stage catalytic oxygen reaction as a heat release medium to reduce the temperature of the waste gas, and the heat release medium inlet of the second-stage heat recovery device is connected with the outlet of the second-stage catalytic oxidation reactor;
the selective catalytic reduction reactor is used for performing selective catalytic reduction reaction on the waste gas after the second-stage catalytic oxidation reaction by taking ammonia as a reducing agent, and is provided with an ammonia spraying system, the inlet of the ammonia spraying system is connected with the heat release medium outlet of the second-stage heat recovery device, and the outlet of the ammonia spraying system is connected with the heat release medium inlet of the gas-gas heat exchanger.
The utility model has the advantages that: because the two sections of catalytic oxidation reactors are arranged, all catalytic oxidation processes required by waste gas purification are carried out in the two sections of reactors, so that the reaction intensity and the heat production quantity of a single catalytic oxidation reactor are reduced, the temperature rise in the catalytic oxidation reactor is reduced, and the damage to the catalyst due to overhigh temperature rise is avoided; because the first-stage heat recovery device and the second-stage heat recovery device are respectively arranged between the two sections of catalytic oxidation reactors and between the second-stage catalytic oxidation reactor and the selective catalytic reduction reactor, the redundant heat generated by the first-stage catalytic oxidation reaction and the second-stage catalytic oxidation reaction is taken out of the system and utilized, not only the energy is obtained, but also the temperature of waste gas is reduced, and the excessive temperature generated in the second-stage catalytic oxidation reactor and the selective catalytic reduction reactor due to the accumulation of the heat energy is avoided; because the selective catalytic reduction reactor is arranged, ammonia is used as a reducing agent, nitrogen in the waste gas is reduced into nitrogen through catalytic reduction reaction, and the emission of nitrogen oxides is reduced; the waste gas discharged by the selective catalytic reduction reactor is used as a heat release medium of the preheating device, so that the heat generated by the catalytic reduction reaction is effectively utilized.
The utility model discloses be adapted to acrylonitrile's absorption tower tail gas and handle, also be adapted to other similar exhaust-gas treatment who contains volatile organic compounds and nitrogen oxide.
Drawings
Fig. 1 is a schematic diagram of the system configuration of the present invention.
Detailed Description
Referring to fig. 1, the catalytic incineration system of the present invention includes:
the gas-liquid separation tank 10 is used for separating water from waste gas, and is provided with a waste gas inlet, a waste gas outlet and a sewage discharge port, wherein the waste gas inlet is used for connecting a waste gas input pipeline 62 of the system, the sewage discharge port is provided with a sewage discharge valve for controlling sewage discharge, and the sewage discharge valve can be directly connected into a sewage treatment facility or a sewage storage tank in the system through a pipeline, and can also be connected into a sewage discharge pipeline 67 of the system to be discharged outwards;
a gas-gas heat exchanger, e.g. a gas-gas plate heat exchanger, as a primary heater of the preheating device, for preheating the exhaust gas with the exhaust gas discharged from the selective catalytic reduction reactor as a heat-releasing medium, so as to adapt the temperature of the exhaust gas to the inlet gas temperature requirement of the subsequent stage of the catalytic oxidation reactor 42, or other heating devices supplemented with preheating devices, to adapt the exhaust gas temperature to the inlet gas temperature requirement of the subsequent stage of catalytic oxidation reactor 42, is provided with a heat-releasing medium inlet and a heat-releasing medium outlet, the inlet of the waste gas separator is connected with a waste gas outlet of the gas-liquid separation tank, the waste gas after treatment of catalytic oxidation reaction and selective catalytic reduction reaction is discharged from a heat release medium outlet of the gas-liquid separation tank, and the waste gas can be generally connected with subsequent waste heat recovery equipment, or connected with a chimney through a system discharge pipeline 68, or used as a direct emptying pipe and the like;
the first-stage catalytic oxidation reactor is used for the catalytic oxidation reaction of the preheated waste gas, and an inlet of the first-stage catalytic oxidation reactor is connected with an outlet of the gas-gas heat exchanger;
the first-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the first-stage catalytic oxygen reaction as a heat release medium, reducing the temperature of the waste gas to enable the waste gas to meet the requirement of the inlet gas temperature of a subsequent second-stage catalytic oxidation reactor, and the inlet of the heat release medium is connected with the outlet of the first-stage catalytic oxidation reactor;
a second-stage catalytic oxidation reactor 46 for performing a catalytic oxidation reaction on the exhaust gas after the first-stage catalytic oxidation reaction, an inlet of which is connected to an outlet of the heat releasing medium of the first-stage heat recovery device;
the two-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the two-stage catalytic oxygen reaction as a heat release medium, reducing the temperature of the waste gas to ensure that the waste gas meets the waste gas temperature requirement of a subsequent selective catalytic reduction reactor, and the heat release medium inlet of the two-stage heat recovery device is connected with the outlet of the two-stage catalytic oxidation reactor;
the selective catalytic reduction reactor 20 is configured to perform a selective catalytic reduction reaction on the exhaust gas after the second-stage catalytic oxidation reaction by using ammonia as a reducing agent to convert nitrogen oxides into nitrogen and water, and is provided with an ammonia injection system, an inlet of the ammonia injection system is connected to a heat release medium outlet of the second-stage heat recovery device, and an outlet of the ammonia injection system is connected to a heat release medium inlet of the gas-gas heat exchanger.
Typically, the off-gas inlet of the knock-out pot is located at the top thereof and the sewage discharge port is located at the bottom thereof.
An electric heater 33 can be arranged between the outlet of the gas-gas heat exchanger and the inlet of the first section of the catalytic oxidation reactor, or the electric heater is not arranged, and the electric heater can be arranged according to actual requirements.
The electric heater is used for performing supplementary heating (when needed) on the waste gas heated by the gas-gas heat exchanger, the inlet of the electric heater is connected with the outlet of the gas-gas heat exchanger, the outlet of the electric heater is connected with the inlet of the first section of catalytic oxidation reactor, and therefore the inlet of the first section of catalytic oxidation reactor is connected with the outlet of the gas-gas heat exchanger.
The one-stage heat recovery device preferably includes a one-stage evaporator 53.
The first-stage evaporator takes waste gas as a heat release medium, an inlet of the first-stage evaporator is connected with an outlet of the first-stage catalytic oxidation reactor, and an outlet of the first-stage evaporator is connected with an inlet of the second-stage catalytic oxidation reactor.
The secondary heat recovery device preferably comprises a secondary evaporator 55.
The two-stage evaporator takes waste gas as a heat release medium, the inlet of the two-stage evaporator is connected with the outlet of the two-stage catalytic oxidation reactor, and the outlet of the two-stage evaporator is connected with the inlet of the selective catalytic reduction reactor.
Each evaporator can adopt any heat recycling device capable of generating steam, and comprises an adaptive waste heat boiler, a heater, a heat exchanger and the like, so that waste heat in waste gas is utilized to produce byproduct steam, and the temperature of the waste gas is reduced, so that the waste gas is adaptive to the inlet gas temperature requirement of a subsequent reactor.
The steam outlets of the first-stage evaporator and the second-stage evaporator can be connected into a steam drum 51.
The steam pocket is provided with a steam outlet and a steam inlet for connecting the steam of the first-section evaporator and the second-section evaporator.
The two-stage heat recovery device can also comprise a steam superheater 57, also can not comprise a steam superheater, can be arranged according to actual needs, and can convert steam generated by the evaporator into high-quality superheated steam through the steam superheater.
The steam superheater heats steam to a superheated temperature by taking waste gas as a heat release medium, a steam inlet of the steam superheater is connected with a steam outlet of the steam drum through a pipeline, a steam outlet of the steam superheater is connected with a steam pipe network through a steam output pipeline 66, an inlet of the steam outlet of the steam superheater is connected with an outlet of the first-stage evaporator, an outlet of the steam superheater is connected with an inlet of the selective catalytic reduction reactor, and therefore the outlet of the second-stage evaporator is connected with the inlet of the selective catalytic reduction reactor.
A steam drum steam output control valve 96 can be arranged on a connecting pipeline between a steam inlet of the steam superheater and a steam outlet of the steam drum and is used for controlling the steam output of the steam drum so as to control the working state of the steam superheater and the heat release quantity of the waste gas flowing through the steam superheater, thereby playing a certain role in regulating the inlet gas temperature of the selective catalytic reduction reactor.
The ammonia injection system of the selective catalytic reduction reactor may generally include an ammonia air mixer 72 and an ammonia injection grid 74.
The ammonia injection grid is located in the ammonia injection section 70 of the pipeline at the inlet side of the selective catalytic reduction reactor, and is provided with a plurality of ammonia injection ports, and the ammonia injection ports are generally towards the rear (along the airflow direction) and used for injecting ammonia-air mixed gas into the pipeline.
Generally, a section of pipeline connected with an inlet of the selective catalytic reduction reactor can be used as an ammonia spraying section of the pipeline, and the exhaust gas after ammonia spraying directly enters the selective catalytic reduction reactor to carry out the selective catalytic reduction reaction.
The cross-sectional shape of the ammonia spraying section of the pipeline can be rectangular so as to ensure the uniformity of ammonia spraying, and the ammonia spraying section can be connected with the inlet of the selective catalytic reduction reactor through a reducing connecting pipe.
The section shape of the ammonia spraying section of the pipeline can also be round and other forms.
The ammonia-air mixer is generally provided with an air inlet, an ammonia gas inlet and an ammonia-air mixed gas outlet, the air inlet of the ammonia-air mixer is connected with the air outlet of the air supply system, the ammonia gas inlet is connected with the ammonia supply pipeline 63 of the system, and the ammonia-air mixed gas outlet is connected with the ammonia spraying grid through an ammonia-air mixed gas conveying pipeline.
The ammonia-air mixed gas conveying pipeline is provided with an ammonia conveying main pipe and an ammonia conveying branch pipe, the outer end of the ammonia conveying branch pipe is connected to the ammonia conveying main pipe, and the inner end of the ammonia conveying branch pipe is connected with a corresponding pipeline on the ammonia spraying grid.
Usually, the ammonia conveying main pipe is positioned outside the ammonia spraying section of the pipeline, and the ammonia conveying branch pipe penetrates through the pipe wall of the ammonia spraying section of the pipeline so as to realize connection with the ammonia conveying main pipe and the ammonia spraying grid.
Generally, the number of the ammonia conveying branch pipes is preferably multiple.
The ammonia delivery branch pipes are preferably provided with respective ammonia injection control valves for controlling the flow of each branch pipe, and particularly, the flow distribution can be carried out through the relative flow control of each branch pipe (if a plurality of branch pipes are provided), so that the balance of the ammonia injection amount at each position in the pipeline is realized.
The ammonia spraying grid is preferably divided into one layer or a plurality of layers in the ammonia spraying section of the pipeline along the axial direction, and the ammonia spraying openings are basically distributed in a balanced way on the same layer and distributed on the whole pipeline section so as to ensure the uniformity of ammonia spraying on the same pipeline section.
A spoiler 76 positioned behind the ammonia injection grid is preferably arranged in the ammonia injection section of the pipeline. The spoiler is used for disturbing the airflow and changing the direction of the airflow nearby so as to better realize the mixing of ammonia and waste gas.
The spoilers are preferably arranged in one or more layers along the axial direction in the ammonia spraying section of the pipeline, the number of the spoilers on the same layer is usually a plurality of spoilers which are parallel to each other, can be in a shape of a tilted flat plate or a bent plate with an angular section, and when the spoilers are in the shape of the bent plate, the angular tips face the direction of the ammonia spraying pipe.
When the spoilers are provided in a plurality of layers in the axial direction, the spoilers of adjacent layers are preferably arranged in a staggered manner.
The air supply system may include an air filter 85 and an air make-up fan 83.
The inlet of the air filter is used for being connected with an air supply pipeline or a compressed air supply pipeline 64, the outlet of the air filter is connected with the inlet of the air supply fan, the outlet of the air supply fan forms the air outlet of the air supply system,
according to the requirement, the outlet of the air supply fan forms the air outlet of the air supply system, and can be respectively connected with the air inlet of the ammonia-air mixer, the inlet of the gas-liquid separation tank and the inlet of the two-stage catalytic oxidation reactor through pipelines.
The connection of the air outlet of the air supply system with the relevant inlet through the pipeline can be realized by directly connecting the pipeline with the corresponding inlet or by connecting the pipeline with the pipeline connected with the corresponding inlet, so that filtered air can be supplemented to corresponding equipment as required.
The preheating device is preferably provided with a preheating bypass pipe, which is normally provided with a preheating bypass control valve 94, and both ends of the preheating bypass pipe are respectively connected to an inlet pipe and an outlet pipe of the primary heater in the preheating device to form a bypass for the primary heater of the preheating device.
When only one heater is provided to the preheating device, the heater constitutes a main heater of the preheating device.
When the preheating device comprises a gas-gas heat exchanger, the gas-gas heat exchanger constitutes the main heater of the preheating device.
The primary heater of the pre-heating device should typically be provided with a primary heating control valve.
The main heating control valve may be disposed at an inlet side and/or an outlet side of the main heater between two connection points of the preheating bypass pipe according to the related art, and only controls the opening degree of the inlet/outlet pipe of the main heater.
The temperature of the exhaust gas entering the primary catalytic oxidation reactor (inlet gas temperature) may be adjusted by any one or more of the following:
1) adjusting the preheat bypass control valve, or adjusting the preheat bypass control valve and the main heat control valve;
2) when the preheating device is simultaneously provided with a main heater and an auxiliary heater, the working state of the auxiliary heater is adjusted, and when the preheating device is simultaneously provided with an air-gas heat exchanger and an electric heater, the electric heater forms the auxiliary heater;
3) the air quantity sent into the gas-liquid separation tank by the air supply system is adjusted through a corresponding control valve arranged on a connecting pipeline between an air outlet of the air supply system and an air inlet of the ammonia-air mixer.
Generally, an on-line temperature sensor for collecting the inlet gas temperature of the first catalytic oxidation reactor by using the exhaust gas temperature can be arranged on the inlet side or the inlet side pipeline of the first catalytic oxidation reactor, and the relevant control valve is adjusted according to the inlet gas temperature of the first catalytic oxidation reactor.
Can set up on the exit side of one section catalytic oxidation reactor or the exit side pipeline and be used for adopting exhaust gas temperature's online temperature sensor to carry out the collection of one section catalytic oxidation reactor export gas temperature, under the prerequisite that satisfies one section catalytic oxidation reactor import gas temperature requirement, when export gas temperature is higher than the settlement temperature, through adjusting air gas supply system sends into the amount of wind of gas-liquid separation jar carries out the control of one section catalytic oxidation reactor export gas temperature.
Generally, the air quantity sent into the gas-liquid separation tank by the air supply system and the heating quantity of the preheating device are cooperatively regulated, so that the inlet gas temperature and the outlet gas temperature of a first-stage catalytic oxidation reactor meet the requirements.
The first heat recovery device is preferably provided with a first heat recovery bypass pipeline, the first heat recovery bypass pipeline is usually provided with a first heat recovery bypass control valve 92, two ends of the first heat recovery bypass pipeline are respectively connected to an inlet pipeline and an outlet pipeline of the first heat recovery device, and when the first heat recovery device is provided with a plurality of heat recovery devices, two ends of the first heat recovery bypass pipeline can also be respectively connected to an inlet pipeline and an outlet pipeline of main heat recovery devices of the first heat recovery device, so that a bypass for the first heat recovery device or the main heat recovery devices of the first heat recovery device is formed.
The primary heat recovery device in the primary heat recovery device or the primary heat recovery device in the primary heat recovery device should be provided with a primary heat recovery control valve.
The first section of heat recovery control valve may be disposed at an inlet side and/or an outlet side of the first section of heat recovery device or at an inlet side and/or an outlet side of a main heat recovery device in the first section of heat recovery device, between two connection points of the first section of heat recovery bypass pipeline, according to the prior art, and only controls the pipeline opening degree of the first section of heat recovery device or the main heat recovery device thereof.
The temperature of the exhaust gas entering the two-stage catalytic oxidation reactor may be adjusted by any one or more of the following:
1) adjusting the first-stage heat recycling bypass control valve, or adjusting the first-stage heat recycling bypass control valve and the first-stage heat recycling control valve, thereby adjusting the heat energy (heat extraction amount) extracted from the waste gas by the first-stage heat recovery device;
2) the air quantity sent into the second-stage catalytic oxidation reactor by the air supply system is adjusted through a corresponding control valve arranged on a connecting pipeline between an air outlet of the air supply system and an air inlet of the second-stage catalytic oxidation reactor.
Generally, an on-line temperature sensor for collecting the inlet gas temperature of the secondary catalytic oxidation reactor by using the exhaust gas temperature can be arranged on the inlet side or the inlet side pipeline of the secondary catalytic oxidation reactor, and the relevant control valve is adjusted according to the inlet gas temperature of the secondary catalytic oxidation reactor.
Can set up on the exit side of two-stage catalytic oxidation reactor or the exit side pipeline and be used for adopting exhaust gas temperature's online temperature sensor to carry out the collection of two-stage catalytic oxidation reactor export gas temperature, under the prerequisite that satisfies two-stage catalytic oxidation reactor import gas temperature requirement, when export gas temperature is higher than the settlement temperature, through adjusting air gas supply system sends into the amount of wind of two-stage catalytic oxidation reactor carries out the control of two-stage catalytic oxidation reactor export gas temperature.
Generally, the air quantity fed into the secondary catalytic oxidation reactor by the air supply system and the heat extraction quantity of the primary heat recovery device are cooperatively regulated, so that the inlet gas temperature and the outlet gas temperature of the secondary catalytic oxidation reactor meet the requirements.
The second-stage heat recovery device is preferably provided with a second-stage heat recovery bypass pipeline, a second-stage heat recovery bypass control valve 93 is usually arranged on the second-stage heat recovery bypass pipeline, two ends of the second-stage heat recovery bypass pipeline are respectively connected to an inlet pipeline and an outlet pipeline of the second-stage heat recovery device, and when the second-stage heat recovery device is provided with a plurality of heat recovery devices, two ends of the second-stage heat recovery bypass pipeline can also be respectively connected to the inlet pipeline and the outlet pipeline of a main heat recovery device in the second-stage heat recovery device, so that a bypass for the second-stage heat recovery device or the main heat recovery device is formed.
The second-stage heat recovery device or the main heat recycling equipment in the second-stage heat recovery device should be provided with a second-stage heat recycling control valve.
The second-stage heat recycling control valve can be arranged on the inlet side and/or the outlet side of the second-stage heat recycling device or the inlet side and/or the outlet side of main heat recycling equipment in the second-stage heat recycling device according to the prior art and is positioned between two connecting points of the second-stage heat recycling bypass pipeline, and only the opening degree of the second-stage heat recycling device or the pipeline of the main heat recycling equipment is controlled.
The temperature of the exhaust gas entering the selective catalytic reduction reactor may be adjusted by any one or more of the following:
1) adjusting the second-stage heat recycling bypass control valve, or adjusting the second-stage heat recycling bypass control valve and the second-stage heat recycling control valve, thereby adjusting the heat energy (heat extraction amount) extracted from the waste gas by the second-stage heat recovery device;
2) the air quantity (namely the air quantity sent into the ammonia-air mixer) sent into the selective catalytic reduction reactor by the air supply system is adjusted by corresponding control valves arranged on a connecting pipeline between an air outlet of the air supply system and an air inlet of the ammonia-air mixer.
In general, an on-line temperature sensor for collecting the inlet gas temperature of the selective catalytic reduction reactor may be provided on the inlet side or inlet side duct of the selective catalytic reduction reactor, and the adjustment of the relevant control valve may be performed according to the inlet gas temperature of the selective catalytic reduction reactor.
The device can be arranged on the outlet side of the selective catalytic reduction reactor or an outlet side pipeline and is used for collecting the outlet gas temperature of the selective catalytic reduction reactor by adopting an online temperature sensor of the exhaust gas temperature, and on the premise of meeting the inlet gas temperature requirement of the selective catalytic reduction reactor, when the outlet gas temperature is higher than the set temperature, the outlet gas temperature of the selective catalytic reduction reactor is controlled by adjusting the air volume of the selective catalytic reduction reactor sent into by the air supply system.
Generally, the inlet gas temperature and the outlet gas temperature of the selective catalytic reduction reactor are both required by the cooperative regulation of the air quantity fed into the selective catalytic reduction reactor by the air supply system and the heat extraction quantity of the two-stage heat recovery device.
The main working flow of the system is as follows: the tail gas containing a large amount of VOCs is firstly separated from free water through a gas-liquid separation tank, is mixed with primary air supplement provided by an air supplement fan, enters a gas-gas plate type heat exchanger for preheating, is heated by an electric heater, the heated tail gas enters a first-stage reactor, part of organic matters in the tail gas are combusted and reacted into water and carbon dioxide under the action of a catalyst, and a large amount of heat is released to raise the temperature of the tail gas, the tail gas enters a first-stage steamer to generate steam, the temperature of the tail gas entering a second-stage catalytic reactor is controlled by adjusting the steam yield and a bypass valve, the tail gas enters the second-stage reactor to perform catalytic reaction, the heat is released, the high-temperature tail gas passes through the second-stage evaporator to generate steam, the temperature of the tail gas entering a denitration reactor is controlled by adjusting the steam. And the tail gas after waste heat recovery enters an SCR denitration reactor, nitrogen oxide in the tail gas and a proper amount of ammonia gas are subjected to chemical reaction under the action of a denitration catalyst, the nitrogen oxide is reduced into nitrogen gas and water, the reaction gas flowing out of the denitration reactor exchanges heat through a gas-gas plate type heat exchanger, the inlet gas of a section of reactor is heated, and finally the tail gas reaching the standard is discharged into the atmosphere through a chimney.
Through secondary air supplement, a large amount of dilution air in the traditional process is reduced by about 70-80%, the fan investment is reduced, and the operation energy consumption is saved.
The outlet temperature of the first stage reactor can be controlled by controlling the primary air supply amount to the gas-liquid separation tank.
Through one section evaporimeter, control steam output and bypass control valve's regulation, the temperature of control entering two-stage reactor, different changes of VOCs in this design can the adaptation tail gas.
The catalyst and the VOCs in the second-stage reactor can fully react through the second-stage air supplement, and the range temperature of the second-stage reactor can be properly reduced.
Through two-stage process evaporimeter, can adjust the temperature that gets into denitration reactor, this design can adapt to different reaction temperature's denitration catalyst.
The two-stage reactor is adopted, and different oxidation catalysts can be selectively installed because of the large adjustable temperature range.
Compared with other existing tail gas treatment devices adopting the traditional technology, the tail gas treatment system has the advantages of improved steam yield, high device adjustability, stable operation and stable operation.
The following is an engineering example applying the utility model:
the acrylonitrile production project related to the engineering example is subjected to excavation and transformation, the formed production capacity is 10.6 ten thousand tons/year, the production process adopts a propylene ammoxidation technology, propylene and ammonia are used as main raw materials, acrylonitrile and other byproducts are generated by reaction under the action of a catalyst, then an acrylonitrile product is obtained by the process flows of quenching, recovery, refining and the like, an acrylonitrile absorption tower is arranged in the recovery process, the main components in the tail gas at the top of the absorption tower are nitrogen, water vapor and carbon dioxide, and simultaneously, a small amount of carbon monoxide, acrylonitrile, propylene, propane, trace hydrogen cyanide and the like are contained, wherein the components harmful to the environment are mainly non-methane total hydrocarbon and nitrogen oxide,the actually measured pollutant concentrations are respectively 5261.95-13520.46 mg/Nm of non-methane total hydrocarbon concentration3The concentration of nitrogen oxides is 596.38-598.82 mg/Nm3Acrylonitrile concentration 300mg/Nm3Hydrogen cyanide concentration 50mg/Nm3The heat value of the tail gas is about 820-343 kJ/Nm3Much less than 7880kJ/Nm3And cannot be discharged into a flare system. Through the utility model discloses a system treatment back, these four pollutants reach the emission standard that "petrochemical industry pollutant emission standard" (GB 31571-2015) stipulate, and system operation energy consumption is 480 kW, and the adaptive reaction temperature range is 200 ~ 750 ℃, and the tonifying qi volume is less than 21000Nm3And the processing system can ensure the stable operation of the system process, the byproduct steam pressure and the temperature, and can smoothly and automatically adapt to the change and the switching of the load no matter in the lowest load or highest load operation state.
Description of the treatment procedure:
acrylonitrile tail gas discharged from the top of the absorption tower is firstly separated into free water through a gas-liquid separation tank V-201 for gas-liquid separation, the free water is mixed with combustion-supporting air provided by a blower C-201 serving as an air supply fan, the mixture enters a gas-gas plate type heat exchanger E-203 serving as a main heater of a preheating device for preheating, the heated tail gas enters a section of catalytic oxidation reactor (CO reactor) R-201A, and partial organic matters in the tail gas are combusted and reacted into water and CO under the action of a catalyst2Then the waste heat enters a waste heat boiler B-202A used as a primary heat recovery device to recover heat, the heat passes through the waste heat boiler and then enters a secondary catalytic oxidation reactor R-201B together with air from a blower C-201 in sequence to convert the residual organic matters into water and CO2And then sequentially carrying out heat release on a two-section waste heat boiler B-202B and a steam superheater E-202, enabling steam of the waste heat boiler B-202A, B-202B to pass through the steam superheater E-202 to form superheated steam which can be connected into a steam pipe network for utilization, enabling tail gas after waste heat recovery to enter a selective catalytic reduction reactor (SCR reactor) R-202, and enabling NO in the tail gas to enter a catalystXThe reaction gas flows out of the SCR reactor R-202 to be used as a heat medium of a gas-gas plate type heat exchanger E-203, and partial heat is exchangedAnd after the gas is fed into the inlet of the gas-feeding plate type heat exchanger E-203, residual waste heat is recovered by a subsequent tail gas waste heat recoverer B-201, and the tail gas reaching the standard is discharged into the atmosphere through a chimney H-201.
Description of process parameter control:
the tail gas treatment system mainly comprises a catalytic oxidation reactor R-201A, R-201B for removing organic matters and carbon monoxide, an SCR reactor R-202 for removing NOx and a heat recovery system.
The catalytic oxidation reactors R-201A and R-201B can stably and efficiently oxidize CO, HCN and C in the exhaust gas for a long time in the reaction temperature range of 200-750 ℃ (the catalyst adopts a metal honeycomb noble metal catalytic oxidation catalyst of noble metal company in Japan) or 270-600 ℃ (the catalyst adopts a noble metal catalytic oxidation catalyst of BASF/southern chemistry)3H6、C3H8And other organics to CO2And water, thereby ensuring that the volatile organic compounds, HCN and the like for the tail gas can reach the standard and be discharged.
Under the premise that ammonia is supplied according to the chemical proportion in the SCR reactor at the reaction temperature of 300-400 ℃ (TOPSOE DNX-929A is adopted as a catalyst) or 420-570 ℃ (BASF high-temperature SCR catalyst is adopted as a catalyst), NOx and added NH in tail gas are added under the action of the catalyst3Carrying out catalytic reaction to generate harmless N2And water, the catalyst has high-efficiency purification rate and stability, and can ensure that the tail gas can reach the standard for a long time.
The ammonia gas is injected into the ammonia-air mixer through the flow control valve after being metered, is mixed with the dilution air and is directly sprayed into a pipeline positioned at the upstream of the SCR reactor through the ammonia spraying grid.
The heat of the tail gas after the reaction is recovered by a heat recovery system, and 2-10 tons/hour of 1.3 MPa steam at 220 ℃ can be byproduct.
Because the oxygen content in the treated tail gas is insufficient, additional air supplement is needed to ensure the purification rate of the waste gas:
1) when the concentration of residual oxygen in the flue gas is more than 3.0 percent, the adiabatic temperature rise under the lowest load working condition is 205 ℃, and 17328kg/h of air needs to be supplemented; the adiabatic temperature rise under the highest load working condition is 386 ℃, and 26430kg/h of air needs to be supplemented;
2) when the concentration of residual oxygen in the flue gas is more than 4.0 percent, the adiabatic temperature rise under the lowest load working condition is 194 ℃, and 22705kg/h of air needs to be supplemented; the adiabatic temperature rise under the highest load working condition is 365 ℃, and air needs to be supplemented for 32800 kg/h;
under the lowest load condition: in order to ensure the quality of byproduct steam and the purification rate of waste gas, the temperature of the outlet gas of the CO reactor is required to be ensured to be above 400 ℃, and the project is implemented by the following measures:
1) adjusting a control valve and a bypass control valve TCV-203A/B of the gas-gas heat exchanger E-203, or starting an electric heater E-201 and the like to enable the temperature of the inlet gas of the catalytic oxidation reactor to be about 200 ℃ (a metal honeycomb noble metal catalytic oxidation catalyst of noble metal company in Japan field);
2) the steam production of the waste heat boiler B-202A/B is controlled by adjusting a control valve of the waste heat boiler and a bypass control valve TCV-205A/B, so that the inlet temperature of the SCR reactor is controlled within a set range, and meanwhile, the constant inlet gas temperature of a heat release medium of the gas-gas heat exchanger E-203 is ensured.
Under the highest load condition: in order to ensure the safety of equipment and catalyst, the temperature of the outlet of the CO reactor needs to be controlled below 750 ℃, and the method is implemented by the following measures:
1) and (3) regulating a damper TCV-203A/B of a bypass of the gas-gas heat exchanger E-203, and reducing the temperature of the inlet gas of the CO reactor to a lower allowable value.
2) The steam production of the waste heat boiler B-202A/B is controlled by adjusting a control valve of the waste heat boiler and a bypass control valve TCV-205A/B, so that the inlet gas temperature of a heat release medium of a gas-gas heat exchanger E-203 is controlled;
3) properly adjusting the amount of air to be supplemented;
4) in an emergency (the catalytic oxidation reactor is over-heated), an emergency direct-exhaust bypass valve of the system is gradually opened, and an air inlet valve of the system is closed.
Description of process control:
the system adopts full-automatic control, and performs logic or PID regulation through a control valve (a shut-off valve or a regulating valve) to control the flow of main materials.
1) Adjusting the supply amount of ammonia (ammonia injection amount) through the concentration value PID of NOx at the inlet of the SCR reactor;
2) setting interlocking control to ensure the safe and stable operation of the system;
3) a bypass system is arranged, and the operation of an upstream main device is not influenced when the system is in a fault or maintenance state;
the engineering example has the characteristics that:
1) the operation energy consumption is low (480 Kw), the adaptive reaction temperature range is large (200-750 ℃), and the gas supplement amount is small (less than 21000Nm 3/h);
2) the system can be ensured to stably operate in the lowest or highest load operation state, and the byproduct steam pressure and temperature are ensured to be stable;
3) the change and switching of the load can be stably and automatically adapted;
4) the process, flow and equipment can also be suitable for other various catalysts;
5) for the catalytic oxidation reactor, the scheme has the functions and the technical process of selecting a proper catalytic oxidation catalyst (reducing the inlet temperature and improving the outlet temperature of the reactor) or setting internal circulating dilution air and reducing the outlet temperature of the reactor, so that the catalytic oxidation system can normally work under the lowest load (adiabatic temperature rise 205 ℃) and the highest load (adiabatic temperature rise 386 ℃), the inlet temperature of the SCR denitration reactor is stable in a selected temperature range, and the running parameters of a downstream process are stable.
6) Waste heat boilers are respectively arranged between the two sections of catalytic oxidation reactors and between the catalytic oxidation reactor and the SCR reactor for recovering the heat of the flue gas, and corresponding bypasses are arranged for adjusting the temperature of the inlet air of each reactor, so that the inlet air temperature of each reactor can be relatively stable under different production loads;
7) the catalytic oxidation reactor has the function similar to a windproof lighter, and prevents the sudden change of the upstream production working condition (such as the change of the purity of the raw material propylene from 96 percent to 99.5 percent per gas switching in the process of starting).
The preferred and optional technical means disclosed in the present invention can be combined arbitrarily to form a plurality of different technical solutions, except for the specific description and the further limitation that one preferred or optional technical means is another technical means.
Claims (10)
1. A catalytic incineration treatment system suitable for treating volatile organic compound tail gas is characterized by comprising:
the gas-liquid separation tank is used for separating water from waste gas, and is provided with a waste gas inlet, a waste gas outlet and a sewage discharge port, wherein the waste gas inlet is used for connecting a waste gas input pipeline of the system, and the sewage discharge port is provided with a sewage discharge valve for controlling sewage discharge;
the gas-gas heat exchanger is used as a main heater of the preheating device and used for preheating the waste gas by taking the waste gas discharged by the selective catalytic reduction reactor as a heat release medium, and is provided with a heat release medium inlet and a heat release medium outlet, and the inlet of the gas-gas heat exchanger is connected with the waste gas outlet of the gas-liquid separation tank;
the first-stage catalytic oxidation reactor is used for the catalytic oxidation reaction of the preheated waste gas, and an inlet of the first-stage catalytic oxidation reactor is connected with an outlet of the gas-gas heat exchanger;
the first-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the first-stage catalytic oxygen reaction as a heat release medium to reduce the temperature of the waste gas, and an inlet of the heat release medium is connected with an outlet of the first-stage catalytic oxidation reactor;
the second-stage catalytic oxidation reactor is used for carrying out catalytic oxidation reaction on the waste gas after the first-stage catalytic oxidation reaction, and an inlet of the second-stage catalytic oxidation reactor is connected with a heat release medium outlet of the first-stage heat recovery device;
the second-stage heat recovery device is used for performing heat recovery and utilization by taking the waste gas after the second-stage catalytic oxygen reaction as a heat release medium to reduce the temperature of the waste gas, and the heat release medium inlet of the second-stage heat recovery device is connected with the outlet of the second-stage catalytic oxidation reactor;
the selective catalytic reduction reactor is used for performing selective catalytic reduction reaction on the waste gas after the second-stage catalytic oxidation reaction by taking ammonia as a reducing agent, and is provided with an ammonia spraying system, the inlet of the ammonia spraying system is connected with the heat release medium outlet of the second-stage heat recovery device, and the outlet of the ammonia spraying system is connected with the heat release medium inlet of the gas-gas heat exchanger.
2. The system of claim 1, wherein an electric heater is arranged between the outlet of the gas-gas heat exchanger and the inlet of the first catalytic oxidation reactor or not, the electric heater is used for performing supplementary heating on the exhaust gas heated by the gas-gas heat exchanger, the inlet of the electric heater is connected with the outlet of the gas-gas heat exchanger, the outlet of the electric heater is connected with the inlet of the first catalytic oxidation reactor, and therefore the inlet of the first catalytic oxidation reactor is connected with the outlet of the gas-gas heat exchanger.
3. The system according to claim 1, wherein the primary heat recovery device comprises a primary evaporator, the primary evaporator uses the exhaust gas as an exothermic medium, an inlet of the primary evaporator is connected with an outlet of the primary catalytic oxidation reactor, an outlet of the primary evaporator is connected with an inlet of the secondary catalytic oxidation reactor, the secondary heat recovery device comprises a secondary evaporator, the secondary evaporator uses the exhaust gas as an exothermic medium, an inlet of the secondary evaporator is connected with an outlet of the secondary catalytic oxidation reactor, and an outlet of the secondary evaporator is connected with an inlet of the selective catalytic reduction reactor.
4. The system of claim 3, wherein the vapor outlet of the first stage evaporator and the vapor outlet of the second stage evaporator both open into a drum.
5. The system of claim 4, wherein the secondary heat recovery device comprises or does not comprise a steam superheater, the steam superheater is used for heating steam to a superheated temperature by using exhaust gas as an exothermic medium, a steam inlet of the steam superheater is connected with a steam outlet of the steam drum, a steam outlet of the steam superheater is connected with a steam pipe network through a steam output pipeline, an inlet of the steam pipe network is connected with an outlet of the primary evaporator, an outlet of the steam pipe network is connected with an inlet of the selective catalytic reduction reactor, and therefore the outlet of the secondary evaporator is connected with the inlet of the selective catalytic reduction reactor.
6. The system according to claim 1, wherein the ammonia injection system of the scr reactor comprises an ammonia air mixer and an ammonia injection grid, the ammonia injection grid is located in the ammonia injection section of the pipeline on the inlet side of the scr reactor and is provided with a plurality of ammonia injection ports, the ammonia air mixer is provided with an air inlet, an ammonia gas inlet and an ammonia air mixture outlet, the air inlet of the ammonia air mixer is connected with the air outlet of the air supply system, the ammonia gas inlet is connected with the ammonia supply pipeline of the system, the ammonia air mixture outlet is connected with the ammonia injection grid through an ammonia air mixture delivery pipeline, the ammonia air mixture delivery pipeline is provided with an ammonia delivery main pipe and an ammonia delivery branch pipe, the outer end of the ammonia delivery branch pipe is connected with the ammonia delivery main pipe, and the inner end of the ammonia delivery branch pipe is connected with the corresponding pipeline on the ammonia injection grid.
7. The system of claim 6, wherein the air supply system comprises an air filter and an air supply blower, an inlet of the air filter is used for being connected with an air supply pipeline or a compressed air supply pipeline, an outlet of the air filter is connected with an inlet of the air supply blower, and an outlet of the air supply blower forms an air outlet of the air supply system and is respectively connected with an air inlet of the ammonia-air mixer, an inlet of the gas-liquid separation tank and an inlet of the two-stage catalytic oxidation reactor through pipelines.
8. The system according to any one of claims 1 to 7, wherein the preheating device is provided with a preheating bypass line, the preheating bypass line is provided with a preheating bypass control valve, both ends of the preheating bypass line are respectively connected to an inlet line and an outlet line of the primary heater in the preheating device to form a bypass to the primary heater of the preheating device, and the primary heater of the preheating device is provided with a primary heating control valve.
9. The system according to any one of claims 1 to 7, wherein the first heat recovery device is provided with a first heat recovery bypass pipeline, the first heat recovery bypass pipeline is provided with a first heat recovery bypass control valve, two ends of the first heat recovery bypass pipeline are respectively connected to the inlet pipeline and the outlet pipeline of the first heat recovery device or the inlet pipeline and the outlet pipeline of the main heat recovery equipment in the first heat recovery device to form a bypass for the first heat recovery device or the main heat recovery equipment thereof, and the first heat recovery device or the main heat recovery equipment in the first heat recovery device is provided with a first heat recovery control valve.
10. The system according to any one of claims 1 to 7, wherein the second-stage heat recovery device is provided with a second-stage heat recovery bypass pipeline, a second-stage heat recovery bypass control valve is arranged on the second-stage heat recovery bypass pipeline, two ends of the second-stage heat recovery bypass pipeline are respectively connected to an inlet pipeline and an outlet pipeline of the second-stage heat recovery device or an inlet pipeline and an outlet pipeline of main heat recovery equipment in the second-stage heat recovery device to form a bypass for the second-stage heat recovery device or the main heat recovery equipment in the second-stage heat recovery device, and the second-stage heat recovery device or the main heat recovery equipment in the second-stage heat recovery device is provided with a second-stage heat recovery control valve.
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Address after: 100005-101-100, No.5 Jianguomen North Street, Dongcheng District, Beijing Patentee after: Sinochem environmental and atmospheric treatment Co.,Ltd. Address before: 100070, No. 3, No. 1, No. 188, South Fourth Ring Road, Fengtai District, Beijing Patentee before: BEIJING CEC ENVIRONMENT ENGINEERING CO.,LTD. |