CN220471634U - Combined incineration device for acrylonitrile waste gas and waste liquid - Google Patents
Combined incineration device for acrylonitrile waste gas and waste liquid Download PDFInfo
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- CN220471634U CN220471634U CN202223094698.7U CN202223094698U CN220471634U CN 220471634 U CN220471634 U CN 220471634U CN 202223094698 U CN202223094698 U CN 202223094698U CN 220471634 U CN220471634 U CN 220471634U
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- 239000002699 waste material Substances 0.000 title claims abstract description 71
- 239000007788 liquid Substances 0.000 title claims abstract description 69
- 239000002912 waste gas Substances 0.000 title claims abstract description 69
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 title claims abstract description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 72
- 230000003647 oxidation Effects 0.000 claims abstract description 61
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 61
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000003546 flue gas Substances 0.000 claims abstract description 34
- 238000002485 combustion reaction Methods 0.000 claims abstract description 32
- 150000003839 salts Chemical class 0.000 claims abstract description 17
- 239000002351 wastewater Substances 0.000 claims abstract description 15
- 239000000446 fuel Substances 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 92
- 238000006722 reduction reaction Methods 0.000 claims description 66
- 239000007921 spray Substances 0.000 claims description 63
- 239000001301 oxygen Substances 0.000 claims description 27
- 229910052760 oxygen Inorganic materials 0.000 claims description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 26
- 239000000779 smoke Substances 0.000 claims description 16
- 229910021529 ammonia Inorganic materials 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 8
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 claims description 6
- 239000000376 reactant Substances 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 4
- 238000005496 tempering Methods 0.000 claims description 4
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 238000011144 upstream manufacturing Methods 0.000 abstract description 10
- 238000001816 cooling Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 18
- 238000010586 diagram Methods 0.000 description 8
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 3
- 150000002897 organic nitrogen compounds Chemical class 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
The application discloses acrylonitrile waste gas waste liquid jointly burns device includes: a burner for treating fuel and waste liquid with high calorific value; the high-temperature reduction zone is used for treating high-heat-value waste liquid and a small amount of low-heat-value waste water and preparing preheated combustion air or a small amount of preheated waste gas; the low-temperature reduction zone is used for treating low-heat-value wastewater and preparing preheated combustion air or a small amount of preheated waste gas; the high-temperature mixer is provided with a preheated air distributor, a preheated waste gas distributor and an ammonia gas distribution pipe; a high-temperature oxidation zone for providing a space for upstream reduction flue gas or waste gas to carry out chemical reaction; the medium-temperature mixer is provided with a normal-temperature air distributor, a preheating waste gas distributor and an ammonia gas distribution pipe; a low-temperature oxidation zone for providing a space for upstream flue gas or waste gas to carry out chemical reaction; a low-temperature mixer provided with a normal-temperature air distributor; the salt fixing temperature adjusting area provides a space for cooling the upstream flue gas and uniformly distributing the flow velocity of the flue gas. The scheme of this application can reach the purpose of control fuel type NOx, and flue gas dwell time is longer and the mixing effect is better.
Description
Technical Field
The application relates to the technical field of acrylonitrile waste gas and waste liquid, in particular to an acrylonitrile waste gas and waste liquid combined incineration device.
Background
The Japanese BHK company has the patent technology of multistage sectional incineration, waste gas and waste liquid are treated simultaneously, waste gas and waste liquid generated in the production process of an acrylonitrile device are introduced into an incinerator, and the waste gas and the waste liquid are sprayed by a multistage nozzle in a proportion suitable for combustion, so that the temperature in the incinerator always keeps the optimal ignition temperature of combustible substances in the waste gas and the waste liquid, the combustion-supporting fuel consumption can be reduced, the excessive rise of the incineration temperature can be effectively controlled, and the generation of NOx can be restrained; simultaneously, CN-contained in waste gas and waste liquid is used for reducing NOx generated in the incineration process into N 2 The generation of NOx is reduced. The similar technical scheme is that the patent of an acrylonitrile production waste liquid and waste gas incinerator is put forward by Ningbo institute, and the scheme is similar to BHK company, and waste gas and waste liquid are treated by adopting a sectional fuel method, wherein the difference is that the BHK company adopts bottom burning positive pressure operation and the Ningbo institute adopts top burning negative pressure operation.
However, the operation process parameters of the scheme do not meet the technical performance index requirements of national standard GB 1884 hazardous waste incineration pollution control Standard issued in 2020 of China, and no obvious high-temperature residence time is available, namely, residence time is more than 1100 ℃ for 2s, so that the method cannot be applied in China at present.
At present, the main flow technical scheme of acrylonitrile waste gas and waste liquid meeting national standard requirements adopts waste gas and waste liquid to treat respectively, and two sets of devices are arranged separately, so that the engineering occupation is large, the device performance is single, the main device can be stopped when any equipment breaks down, and the emergency adjustment capability is not provided.
Disclosure of Invention
The purpose of the application is to develop an incineration device suitable for simultaneously treating or respectively incinerating acrylonitrile waste gas and liquid. The acrylonitrile waste gas and waste liquid combined incinerator can effectively solve the defects, and the concentration of NOx at the outlet of the incinerator can reach below 150mg/Nm < 3 > (3%v of oxygen group) under the condition of meeting national environmental protection standards.
In a first aspect, there is provided an acrylonitrile waste gas and liquid combined incineration device, comprising:
the device comprises a combustor, a first reduction zone, a second reduction zone, a first mixer, a first oxidation zone, a second mixer, a second oxidation zone, a selective non-catalytic reduction SNCR zone, a third mixer and a solid salt temperature adjustment zone which are connected in sequence;
the burner is used for treating fuel and waste liquid under the action of air, and the first waste liquid comprises hydrocyanic acid waste liquid;
the first reduction zone is used for treating waste liquid with different heat values under the action of air, the volume of the first reduction zone is satisfied, the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 0.5s under the independent working condition of waste liquid;
the second reduction zone is used for treating waste liquid under the action of air, the heat value of the waste liquid treated by the second reduction zone is lower than that of the waste liquid treated by the first reduction zone, the volume of the second reduction zone is satisfied, the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 0.5s under the independent working condition of waste liquid;
the first mixer is used for mixing air, waste gas, ammonia gas and reactants from the second reduction zone, and introducing the mixed mixture into the first oxidation zone;
the first oxidation zone is used for treating the mixture from the first mixer, the volume of the first oxidation zone is satisfied, the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 1.35s under the single working condition of waste liquid;
the second mixer is used for mixing air, waste gas, ammonia gas and reactants from the first oxidation zone, and introducing the mixed mixture into the second oxidation zone;
the second oxidation zone is for treating the mixture from the second mixer, the volume of the second oxidation zone satisfying a flue gas residence time >0.5s;
the volume of the SNCR zone satisfies a flue gas residence time of >0.5s;
the third mixer is used for mixing air and reactants from the SNCR zone and introducing the mixed mixture into the salt fixing temperature adjustment zone;
the volume of the solid salt temperature adjustment area meets the requirement that the residence time of the flue gas is more than 0.5s.
Compared with the prior art, the scheme provided by the application at least comprises the following beneficial technical effects:
according to the method, the furnace body is divided into a plurality of functional areas, and process streams such as waste gas, waste liquid and the like with different types and flow rates are respectively processed, so that the requirements of national standard correspondence, in particular the requirements of residence time and incineration temperature are met. And simultaneously controlling the generation and emission of NOx, wherein the waste liquid contains a large amount of organic nitrogen compounds, and the waste gas carries 400-600 mg/Nm < 3 > of NOx and a small amount of organic nitrogen compounds. The burner may provide the initial heat source required for the incineration device.
The first reduction zone and the second reduction zone provide necessary chemical reaction spaces. The first mixer realizes the switching and injection of the process gas flow under different working conditions, and the process gas flow is quickly mixed with upstream reduction flue gas for reaction, and the temperature and oxygen content of the high-temperature oxidation zone are regulated. The first reduction zone and the second reduction zone provide the necessary chemical reaction space. The first mixer realizes the switching and injection of the process gas flow under different working conditions, and the fast mixing reaction with the upstream reduction flue gas, and the temperature and oxygen content of the low-temperature oxidation zone are regulated. The first oxidation zone provides a space for the upstream reduction flue gas or exhaust gas to undergo a chemical reaction at a suitable temperature and oxygen content. The second mixer realizes the switching and injection of the process gas flow under different working conditions, and the process gas flow is quickly mixed with upstream flue gas for reaction, and the temperature and oxygen content of the low-temperature oxidation zone are regulated. The second oxidation zone provides a space for the upstream flue gas or exhaust gas to undergo chemical reactions at the appropriate temperature and oxygen content. The SNCR zone provides a space for the upstream reduction flue gas to undergo chemical reactions at the appropriate temperature and oxygen content. The third mixer realizes the rapid cooling of the flue gas temperature. The salt fixing and temperature adjusting area provides a space for cooling the upstream flue gas and uniformly distributing the flow rate of the flue gas.
With reference to the first aspect, in certain implementations of the first aspect, the burner, the first reduction zone, the second reduction zone, the first mixer, the first portion of the first oxidation zone are arranged along a first direction, the second portion of the first oxidation zone, the second mixer, the second oxidation zone, the SNCR zone, the third mixer, the fixed salt attemperation zone are arranged along a second direction, and the first direction and the second direction are perpendicular to each other.
With reference to the first aspect, in certain implementations of the first aspect, an inlet of the second portion of the first oxidation zone is provided with a throttle ring having an inner diameter that is 0.75 to 0.8 times the inner diameter of the first oxidation zone.
With reference to the first aspect, in certain implementation manners of the first aspect, the first reduction zone is provided with a waste liquid gun, a first waste water gun and a first distributor, the first distributor is provided with a plurality of first spray pipes, the first spray pipes are used for introducing air and/or waste gas, the waste liquid gun and the first waste water gun are arranged in the first spray pipes, and the flow rate of the first spray pipes is 35-50 m/s.
With reference to the first aspect, in certain implementation manners of the first aspect, the second reduction zone is provided with a second distributor and a second waste water gun, the second distributor is provided with a plurality of second spray pipes, the second spray pipes are used for introducing air and/or waste gas, the second waste water gun is arranged in the second spray pipes, and the flow rate of the second spray pipes is 35-50 m/s.
With reference to the first aspect, in certain implementations of the first aspect, the first mixer is provided with a first air register, a first exhaust gas register, a first ammonia gas distributor, and a first mixer flow channel;
the first air register is arranged at the periphery of the first exhaust gas register in an annular cavity structure, and is provided with a plurality of first primary air spray pipes and a plurality of first secondary air spray pipes;
the first exhaust gas register is in a ring cavity structure and is arranged on the periphery of the furnace shell, the first exhaust gas register is divided into two parallel cavities by a partition plate, the first exhaust gas register is provided with a plurality of first-stage exhaust gas spray pipes and a plurality of first-stage exhaust gas spray pipes, the first-stage exhaust gas spray pipes and the first-stage exhaust gas spray pipes are respectively arranged in the two cavities, the first-stage air spray pipes are arranged in the centers of the first-stage exhaust gas spray pipes, the first-stage exhaust gas spray pipes are perpendicular to the flow channel center line of the first mixer, and the included angle between the first-stage exhaust gas spray pipes and the flow channel center line of the first mixer is 30-45 degrees;
the first ammonia gas distributor is arranged in a first exhaust gas register inlet of the first exhaust gas register and is positioned below the partition plate;
the first mixer runner is venturi, and the inlet and outlet opening angle is 60-90 degrees.
With reference to the first aspect, in certain implementations of the first aspect, the first primary air nozzle, the first secondary air nozzle, the first primary exhaust nozzle, and the first secondary exhaust nozzle have a flow rate of 40 to 60m/s.
With reference to the first aspect, in certain implementation manners of the first aspect, axes of the plurality of first primary exhaust nozzles are common with a radius r 1 Is tangent to a circle, r 1 The value of (2) is smaller than or equal to the radius R of the cross section of the inner cavity of the first exhaust gas register 1 1/6 of (2);
the axes of the first secondary exhaust gas spray pipes are commonly combined with the radius r 2 Is tangent to a circle, r 2 Is the radius R of the section of the inner cavity of the first exhaust gas register 1 1/3 to 1/2 of the total weight of the product.
With reference to the first aspect, in certain implementation manners of the first aspect, a plurality of first ammonia gas nozzles are disposed in an axial direction of the first ammonia gas distributor, two first ammonia gas nozzles are disposed corresponding to each axial position, axes of the two first ammonia gas nozzles intersect with an axis of the first ammonia gas distributor, and an included angle between axes of the two first ammonia gas nozzles is 90 °.
With reference to the first aspect, in certain implementations of the first aspect, the second mixer is provided with a second exhaust gas register, a second ammonia gas distributor, a plurality of first air nozzles, and a second mixer flow channel;
the second exhaust gas register is arranged at the periphery of the furnace shell in an annular cavity structure, and is provided with a plurality of second-stage exhaust gas spray pipes and a plurality of second-stage exhaust gas spray pipes;
the second ammonia gas distributor is arranged in a second exhaust gas register inlet of the second exhaust gas register;
the plurality of first air spray pipes are arranged between the second-stage exhaust spray pipes and penetrate through the second exhaust register;
the second mixer runner is venturi, and the inlet and outlet opening angle is 60-90 degrees.
With reference to the first aspect, in certain implementation manners of the first aspect, a flow velocity of the second stage exhaust gas nozzle and the second stage exhaust gas nozzle is 40-60 m/s, and a flow velocity of the first air nozzle is 30-40 m/s.
With reference to the first aspect, in certain implementations of the first aspect, axes of the plurality of second stage exhaust nozzles are common with a radius r 3 Is tangent to a circle, r 3 The value of (2) is smaller than or equal to the radius R of the section of the inner cavity of the second exhaust gas register 2 1/6 of (2);
the axes of the second-stage exhaust gas spray pipes are commonly combined with the radius r 4 Is tangent to a circle, r 4 Is the value of the section radius R of the inner cavity of the second exhaust gas register 2 1/3 of (C);
the axes of the first air spray pipes are commonly combined with the radius r 5 Is tangent to a circle, r 5 Is the radius of the section of the inner cavity of the second exhaust gas registerR 2 1/2 of (C).
With reference to the first aspect, in certain implementation manners of the first aspect, a plurality of second ammonia gas nozzles are disposed in an axial direction of the second ammonia gas distributor, two second ammonia gas nozzles are disposed corresponding to each axial position, axes of the two second ammonia gas nozzles intersect with an axis of the second ammonia gas distributor, and an included angle between axes of the two second ammonia gas nozzles is 90 °.
With reference to the first aspect, in certain implementations of the first aspect, the third mixer is provided with a second air register and a third mixer runner;
the second air register is arranged at the periphery of the furnace shell in an annular cavity structure, is provided with a second air spray pipe, and is perpendicular to the center line of the third mixer flow channel;
the third mixer runner is in a contracted shape, and the inlet opening angle is 60-90 degrees.
With reference to the first aspect, in certain implementation manners of the first aspect, a plurality of second air nozzles are respectively arranged on a plane with a plurality of axial positions along an axial direction of the third mixer flow channel, and axes of the plurality of second air nozzles near an inlet of the third mixer flow channel are together with a radius r 6 Is tangent to the circle, and the axes of the second air spray pipes near the outlet of the third mixer flow passage are commonly connected with the radius r 7 Is tangent to a circle, r 6 ＜r 7 。
With reference to the first aspect, in certain implementations of the first aspect, a flow rate of the second air nozzle closest to the outlet of the third mixer flow channel is 40-60 m/s.
With reference to the first aspect, in certain implementation manners of the first aspect, air introduced into the burner, the first reduction zone, the second reduction zone, and the first mixer is preheated air, and air introduced into the second mixer and the third mixer is normal-temperature air.
With reference to the first aspect, in certain implementations of the first aspect, tangential jet swirls generated by the first mixer, the second mixer, and the third mixer are all the same.
With reference to the first aspect, in certain implementations of the first aspect, the apparatus satisfies at least one of:
the residual oxygen coefficient of the burner is 0.75-0.85;
the residual oxygen coefficient of the first reduction zone is 0.75-0.85;
the combustion temperature of the first reduction zone is 1100-1500 ℃;
the first reduction zone flue gas residence time is >1s;
the residual oxygen coefficient of the second reduction zone is 0.75-0.85;
the combustion temperature of the second reduction zone is 1100-1250 ℃;
the second reduction zone flue gas residence time is >1s;
the oxygen content of the first oxidation zone is 0.3-0.4;
the combustion temperature of the first oxidation zone is 900-1200 ℃;
the first oxidation zone flue gas residence time is >1s;
the oxygen content of the second oxidation zone is 0.2-0.6;
the combustion temperature of the second oxidation zone is 800-950 ℃;
the oxygen content of the SNCR zone is 0.2-0.3;
the combustion temperature of the SNCR zone is 800-950 ℃;
the combined flue gas residence time of the second oxidation zone and the SNCR zone is >1s;
the combustion temperature of the solid salt temperature adjusting area is 600-700 ℃.
The application adopts a waste liquid reduction oxidation incineration method to achieve the purpose of controlling fuel NOx. The waste liquid in the reduction zone is subjected to under-oxygen combustion, most organic nitrogen compounds are converted into N2, and a large amount of reducing atmosphere is generated to enter the oxidation zone so as to reduce the generation of thermal NOx in the oxidation zone.
The application adopts a direct ammonia injection method for waste gas, thereby achieving the purpose of controlling self-carried NOx. NH3 gas and waste gas are quickly mixed and cooled through a mixer and reduced flue gas, so that the optimal reaction temperature is achieved, and compared with the traditional SNCR technology, the method has longer residence time and better mixing effect.
Drawings
Fig. 1 is a schematic structural view of the incineration apparatus of the present application.
Fig. 2 is a block diagram of a high temperature reduction zone.
Fig. 3 is a diagram showing the structure of the low-temperature reduction zone.
Fig. 4 is a structural diagram of a high temperature mixer.
Fig. 5 is another structural diagram of the high temperature mixer.
Fig. 6 is a structural diagram of a moderate temperature mixer.
Fig. 7 is another structural diagram of a moderate temperature mixer.
Fig. 8 is a block diagram of a cryogenic mixer.
Fig. 9 is a structural diagram of an ammonia sparger.
Detailed Description
The present application is described in further detail below with reference to the drawings and specific examples.
The incineration device can be linear or L-shaped as required, and the L-shaped incineration device is shown in FIG. 1.
The incineration device basic structure of this application includes: the device comprises a combustor 1, a high-temperature reduction zone 2, a low-temperature reduction zone 3, a high-temperature mixer 4, a high-temperature oxidation zone 5, a medium-temperature mixer 6, a low-temperature oxidation zone 7, a selective non-catalytic reduction (SNCR) zone 8, a low-temperature mixer 9, a solid salt temperature adjustment zone 10 and the like which are sequentially connected.
The burner 1 processes fuel and waste liquid of high calorific value, including hydrocyanic acid waste liquid, and is configured with preheated combustion air to provide a stable heat source for the incineration device. The fuel may be, for example, natural gas or diesel fuel.
As shown in fig. 2, the high-temperature reduction zone 2 is provided with a high-heat-value waste liquid gun 21, a low-heat-value waste water gun 22 and a preheated combustion air/waste gas distributor 23, the preheated combustion air/waste gas distributor 23 is provided with a plurality of air/waste gas spray pipes 231, the high-heat-value waste liquid gun 21 and the low-heat-value waste water gun 22 are arranged in the air/waste gas spray pipes 231, and the flow rate of the air/waste gas spray pipes 231 is 35-50 m/s. The volume of the high-temperature reduction zone 2 ensures that the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 0.5s under the independent working condition of waste liquid.
The low-temperature reduction zone 3 is provided with a preheated air/waste gas distributor 31 and a low-heat value waste water gun 32, the preheated air/waste gas distributor 31 is provided with a plurality of air/waste gas spray pipes 311, the low-heat value waste water gun 32 is arranged in the air/waste gas spray pipes 311, and the flow rate of the air/waste gas spray pipes 311 is 35-50 m/s. The volume of the low-temperature reduction zone 3 ensures that the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 0.5s under the independent working condition of waste liquid.
The high temperature mixer 4 is provided with a preheated air register 41, an exhaust gas register 42, an ammonia gas distributor 43 and a high temperature mixer flow passage 44. The preheated air register 41 is arranged on the periphery of the exhaust gas register 42 in a ring cavity structure, and is provided with a plurality of primary air spray pipes 411 and a plurality of secondary air spray pipes 412. The exhaust gas register 42 is arranged at the periphery of the furnace shell in a ring cavity structure and is divided into two parallel cavities by a division plate 421. The exhaust register 42 is provided with a plurality of primary exhaust nozzles 422 and a plurality of secondary exhaust nozzles 423. The primary exhaust nozzle 422 and the secondary exhaust nozzle 423 are disposed in two chambers. The primary air nozzle 411 is centered on the primary exhaust nozzle 422 and the secondary air nozzle 412 is centered on the secondary exhaust nozzle 423. Referring to fig. 4 and 9, the ammonia sparger 43 is positioned within the exhaust register inlet 424 below the divider plate 421 for use with the secondary exhaust nozzle 422. The high temperature mixer flow passage 44 is venturi (i.e., waist-shaped) with an inlet/outlet opening angle selected from 60 deg. to 90 deg..
The primary air spray pipe 411 and the secondary air spray pipe 412 are designed to have the flow rate of 40-60 m/s. As shown in fig. 5, a plurality of primary exhaust nozzles 422 may be circumferentially distributed about the exhaust register 42. The axes of the plurality of primary exhaust nozzles 422 may be co-located with a radius r 1 Is tangent to a circle. r is (r) 1 For example, can be less than or equal to the radius R of the cross-section of the cavity of the exhaust gas register 42 1 1/6 of (C).
The primary exhaust gas jet pipe 422 and the secondary exhaust gas jet pipe 423 are designed to have the flow rate of 40-60 m/s. The primary exhaust nozzle 422 is perpendicular to the centerline of the high temperature mixer flow passage 44. The included angle between the secondary exhaust gas spray pipe 423 and the central line of the high-temperature mixer runner 44 is 30-45 degrees. As shown in the figure5, a plurality of secondary exhaust nozzles 423 may be circumferentially distributed on the exhaust register 42. The axes of the plurality of secondary exhaust nozzles 423 may be co-located with a radius r 2 Is tangent to a circle. r is (r) 2 Can be greater than r 1 。r 2 For example, the value of (a) may be the radius R of the cross section of the cavity of the exhaust gas register 42 1 1/3 to 1/2 of the total weight of the product. The secondary exhaust nozzle 423 and the corresponding primary exhaust nozzle 422 are rotated in the same direction.
In the embodiment shown in fig. 9, a plurality of ammonia gas nozzles 431 are provided in the axial direction of the ammonia gas distributor 43. 2 ammonia gas nozzles 431 may be provided corresponding to each axial position, the axes of the two ammonia gas nozzles 431 intersect with the axis of the ammonia gas distributor 43, and the included angle of the axes of the two ammonia gas nozzles 431 may be 60 to 120 °, for example, the included angle is 90 °.
The high-temperature oxidation zone 5 is provided with a throttling ring 51 for the L-shaped furnace body, and the inner diameter of the throttling ring 51 is 0.75-0.8 times of the inner diameter of the furnace; the throttle ring 51 may be omitted for a straight furnace. The volume of the high-temperature oxidation zone 5 ensures that the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 1.35s under the independent working condition of waste liquid.
The intermediate-temperature mixer 6 is provided with an exhaust gas register 61, an ammonia gas distributor 62, a plurality of normal-temperature air nozzles 63, and an intermediate-temperature mixer flow passage 64. The exhaust gas register 61 is arranged on the periphery of the furnace shell in a ring cavity structure, and is provided with a plurality of primary exhaust gas spray pipes 611 and a plurality of secondary exhaust gas spray pipes 612. Referring to fig. 7 and 9, an ammonia sparger 62 is positioned within the exhaust register inlet 613. A plurality of cryogenic air jets 63 are disposed between the primary exhaust jet 611 and the secondary exhaust jet 612 throughout the exhaust register 61. The medium temperature mixer runner 64 is venturi-type, and the opening angle of the inlet and the outlet can be selected from 60 degrees to 90 degrees.
As shown in FIG. 7, the primary exhaust gas spray pipe 611 is designed to have a flow rate of 40-60 m/s, the primary exhaust gas spray pipe 611 is perpendicular to the central line of the flow channel 64 of the medium-temperature mixer, and a plurality of primary exhaust gas spray pipes 611 can be uniformly distributed on the exhaust gas register 61 in a circumferential direction. The axes of the plurality of primary exhaust nozzles 611 may be co-located with a radius r 3 Is tangent to a circle. r is (r) 3 For example, the value of (a) can be smaller than or equal to the radius R of the section of the inner cavity of the exhaust gas register 61 2 1/6 of (C).
As shown in FIG. 7, the design flow rate of the secondary exhaust gas spray pipe 612 is 40-60 m/s, and the included angle between the secondary exhaust gas spray pipe 612 and the central line of the medium-temperature mixer runner 64 is 15-30 degrees. A plurality of secondary exhaust nozzles 612 may be circumferentially distributed about the exhaust register 61. The axes of the plurality of secondary exhaust nozzles 612 may be co-located with a radius r 4 Is tangent to a circle. r is (r) 4 Can be greater than r 3 。r 4 For example, the value of (a) may be the radius R of the cross section of the inner cavity of the exhaust gas register 61 2 1/3 of (C). The secondary exhaust nozzle 612 and the corresponding primary exhaust nozzle 611 are rotated in the same direction.
As shown in FIG. 7, the low temperature air nozzle 63 is designed to have a flow rate of 30 to 40m/s. A plurality of low temperature air nozzles 63 may be circumferentially distributed on the exhaust gas register 61. The axes of the plurality of cryogenic air jets 63 may be co-located with a radius r 5 Is tangent to a circle. r is (r) 5 Can be greater than r 4 。r 5 For example, the value of (a) may be the radius R of the cross section of the inner cavity of the exhaust gas register 61 2 1/2 of (C). The number of the plurality of low temperature air nozzles 63 may be smaller than the number of the plurality of primary exhaust nozzles 611.
In the embodiment shown in fig. 9, a plurality of ammonia gas nozzles 621 are provided in the axial direction of the ammonia gas distributor 62. There may be 2 ammonia gas nozzles 621 for each axial position, the axes of the two ammonia gas nozzles 621 intersect with the axis of the ammonia gas distributor 62, and the included angle of the axes of the two ammonia gas nozzles 621 may be 60 to 120 °, for example, the included angle is 90 °.
The volume of the low temperature oxidation zone 7 ensures a flue gas residence time of >0.5s under any operating conditions.
The SNCR spray gun 81 is arranged at the inlet end of the SNCR zone 8, and the volume of the SNCR zone 8 ensures that the smoke residence time is more than 0.5s under any working condition.
The low-temperature mixer 9 is provided with a normal-temperature air register 91 and a low-temperature mixer runner 92; the normal temperature air register 91 is arranged at the periphery of the furnace shell in a ring cavity structure and is provided with an air spray pipe 911; the low-temperature mixer runner 92 is in a contracted shape, and the inlet opening angle can be selected from 60 degrees to 90 degrees; the air jet 911 is perpendicular to the centerline of the cryogenic mixer flow channel 92.
Along the axial direction of the cryomixer flow passage 92,the plurality of air nozzles 911 are arranged on a plane on which the plurality of axial positions are located, respectively, and the plurality of air nozzles 911 at each axial position may be uniformly arranged around the axis of the low temperature mixer flow passage 92. The axes of the plurality of air jets 911 near the entrance of the cryogenic mixer flow path 92 may be co-located with a radius r 6 The axes of the plurality of air jets 911 near the outlet of the cryogenic mixer flow path 92 may be co-located with a radius r 7 Is tangent to a circle, r 6 ＜r 7 . The flow rate of the air jet 911 closest to the outlet of the cryogenic mixer flow path 92 is 40-60 m/s.
The tangential jet flow rotation directions generated by the high-temperature mixer 4, the medium-temperature mixer 6 and the low-temperature mixer 9 are the same. That is, the plurality of primary air nozzles 411, the plurality of secondary air nozzles 412, the plurality of primary exhaust gas nozzles 611, the plurality of secondary exhaust gas nozzles 612, the plurality of cryogenic air nozzles 63, and the plurality of air nozzles 911 are aligned in rotation.
The volume of the salt fixing temperature adjusting area 10 ensures that the smoke residence time is more than 0.5s under any working condition.
Example 1
The device burns waste gas and waste liquid, the burner 1 processes fuel and high heat value waste liquid, and the Yu Yang coefficient is 0.75-0.85; the high-temperature reduction zone 2 is used for treating waste liquid and a small amount of waste water, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is 1350-1500 ℃, and the retention time is more than 1s; the low-temperature reduction zone 3 is used for treating a small amount of waste gas, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is 1100-1250 ℃, and the residence time is more than 1s; the high-temperature mixer 4 is filled with preheated air, a large amount of preheated waste gas and ammonia; the oxygen content of the high-temperature oxidation zone 5 is 0.3-0.4, the combustion temperature is 900-1000 ℃, and the residence time is more than 1s; the medium-temperature mixer 6 is filled with a large amount of preheated waste gas and ammonia; oxygen content of the low-temperature oxidation zone 7 and the SNCR zone 8 is 0.2-0.3, combustion temperature is 800-850 ℃, and total residence time is more than 1s; the low-temperature mixer 9 is filled with normal-temperature air; the temperature of the salt fixing tempering zone 10 is reduced to about 650 ℃ with a residence time >0.5s.
Example 2
The device burns waste liquid, the burner 1 processes fuel and high calorific value waste liquid, and the Yu Yang coefficient is 0.75-0.85; the high-temperature reduction zone 2 is used for treating waste liquid and a small amount of waste water, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is 1350-1500 ℃, and the retention time is more than 0.5s; the low-temperature reduction zone 3 is used for treating a large amount of wastewater, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is 1100-1250 ℃, and the residence time is more than 0.5s; the high-temperature mixer 4 is only filled with preheated air; the oxygen content of the high-temperature oxidation zone 5 is 0.3-0.4, the combustion temperature is more than 1100 ℃, and the residence time is more than 1.35s; the medium-temperature mixer 6 is filled with normal-temperature air; the oxygen content of the low-temperature oxidation zone 7 is more than 0.6, the combustion temperature is about 950 ℃, and the residence time is more than 0.5s; SNCR zone 8 opens SNCR lance 81 with a combustion temperature of about 950 ℃ and a residence time of >0.5s; the low-temperature mixer 9 is filled with normal-temperature air; the temperature of the salt fixing tempering zone 10 is reduced to about 650 ℃ with a residence time >0.5s.
Example 3
The device burns waste gas, the burner 1 processes fuel, and the residual oxygen coefficient is 0.75-0.85; the high-temperature reduction zone 2 is used for treating a small amount of waste gas, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is more than 1100 ℃, and the residence time is more than 1s; the low-temperature reduction zone 3 is used for treating a small amount of waste gas, the Yu Yang coefficient is 0.75-0.85, the combustion temperature is more than 1100 ℃, and the residence time is more than 1s; the high-temperature mixer 4 is filled with preheated air, a large amount of preheated waste gas and ammonia; the oxygen content of the high-temperature oxidation zone 5 is 0.3-0.4, the combustion temperature is 900-1000 ℃, and the residence time is more than 1s; the medium-temperature mixer 6 is filled with a large amount of preheated waste gas and ammonia; oxygen content of the low-temperature oxidation zone 7 and the SNCR zone 8 is 0.2-0.3, combustion temperature is 800-850 ℃, and total residence time is more than 1s; the low-temperature mixer 9 is filled with normal-temperature air; the temperature of the salt fixing tempering zone 10 is reduced to about 650 ℃ with a residence time >0.5s.
While the preferred embodiment has been described, it is not intended to limit the utility model thereto, and any person skilled in the art may make variations and modifications without departing from the spirit and scope of the present utility model, so that the scope of the present utility model shall be defined by the claims.
Claims (19)
1. An acrylonitrile waste gas and waste liquid combined incineration device, which is characterized by comprising:
the device comprises a combustor (1), a first reduction zone (2), a second reduction zone (3), a first mixer (4), a first oxidation zone (5), a second mixer (6), a second oxidation zone (7), a selective non-catalytic reduction SNCR zone (8), a third mixer (9) and a solid salt temperature regulation zone (10) which are connected in sequence;
the burner (1) is used for treating fuel and waste liquid under the action of air, and the waste liquid comprises hydrocyanic acid waste liquid;
the first reduction zone (2) is used for treating waste liquid and/or waste gas with different heat values under the action of air, the volume of the first reduction zone (2) is satisfied, the smoke residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the smoke residence time is more than 0.5s under the independent working condition of waste liquid;
the second reduction zone (3) is used for treating waste liquid and/or waste gas under the action of air, the heat value of the waste liquid treated by the second reduction zone (3) is lower than that of the waste liquid treated by the first reduction zone (2), the volume of the second reduction zone (3) is satisfied, the flue gas and waste liquid stay time is more than 1s under the combined working condition of the waste gas and the waste liquid, and the flue gas stay time is more than 0.5s under the independent working condition of the waste liquid;
the first mixer (4) is used for mixing reactants from the second reduction zone (3) and one or more of air, waste gas and ammonia gas, and introducing the mixed mixture into the first oxidation zone (5);
the first oxidation zone (5) is used for treating the mixture from the first mixer (4), the volume of the first oxidation zone (5) is satisfied, the flue gas residence time is more than 1s under the combined working condition of waste gas and waste liquid, and the flue gas residence time is more than 1.35s under the single working condition of waste liquid;
the second mixer (6) is used for mixing reactants from the first oxidation zone (5) and one or more of air, waste gas and ammonia gas, and introducing the mixed mixture into the second oxidation zone (7);
-the second oxidation zone (7) is for treating the mixture coming from the second mixer (6), the volume of the second oxidation zone (7) being such that the flue gas residence time is >0.5s;
the volume of the SNCR zone (8) satisfies a flue gas residence time of >0.5s;
the third mixer (9) is used for mixing air and reactants from the SNCR zone (8) and introducing the mixed mixture into the solid salt temperature adjustment zone (10);
the volume of the solid salt temperature adjustment zone (10) satisfies the flue gas residence time of >0.5s.
2. The apparatus according to claim 1, characterized in that the burner (1), the first reduction zone (2), the second reduction zone (3), the first mixer (4), the first part of the first oxidation zone (5) are arranged in a first direction, the second part of the first oxidation zone (5), the second mixer (6), the second oxidation zone (7), the SNCR zone (8), the third mixer (9), the fixed salt tempering zone (10) are arranged in a second direction, the first direction and the second direction being mutually perpendicular.
3. The apparatus according to claim 2, characterized in that the inlet of the second part of the first oxidation zone (5) is provided with a throttle ring (51), the inner diameter of the throttle ring (51) being 0.75-0.8 times the inner diameter of the first oxidation zone (5).
4. A device according to any one of claims 1-3, characterized in that the first reduction zone (2) is provided with a waste lance (21), a first waste lance (22) and a first distributor (23), the first distributor (23) is provided with a plurality of first nozzles (231), the first nozzles (231) are used for introducing air and/or waste gas, the waste lance (21) and the first waste lance (22) are placed in the first nozzles (231), and the first nozzles (231) have a flow rate of 35-50 m/s.
5. A device according to any one of claims 1-3, characterized in that the second reduction zone (3) is provided with a second distributor (31) and a second waste water gun (32), the second distributor (31) being provided with a plurality of second nozzles (311), the second nozzles (311) being for air and/or exhaust gas to be introduced, the second waste water gun (32) being placed in the second nozzles (311), the second nozzles (311) having a flow rate of 35-50 m/s.
6. A device according to any one of claims 1 to 3, characterized in that the first mixer (4) is provided with a first air register (41), a first exhaust gas register (42), a first ammonia distributor (43) and a first mixer flow channel (44);
the first air register (41) is arranged at the periphery of the first exhaust gas register (42) in a ring cavity structure, and the first air register (41) is provided with a plurality of first primary air spray pipes (411) and a plurality of first secondary air spray pipes (412);
the first exhaust gas register (42) is arranged on the periphery of the furnace shell in an annular cavity structure, is divided into two parallel cavities by a partition plate (421), the first exhaust gas register (42) is provided with a plurality of first primary exhaust gas spray pipes (422) and a plurality of first secondary exhaust gas spray pipes (423), the first primary exhaust gas spray pipes (422) and the first secondary exhaust gas spray pipes (423) are respectively arranged in the two cavities, the first primary air spray pipes (411) are arranged at the center of the first primary exhaust gas spray pipes (422), the first secondary air spray pipes (412) are arranged at the center of the first secondary exhaust gas spray pipes (423), the first primary exhaust gas spray pipes (422) are perpendicular to the center line of the first mixer runner (44), and the included angle between the first secondary exhaust gas spray pipes (423) and the center line of the first mixer runner (44) is 30-45 degrees;
the first ammonia gas distributor (43) is arranged in a first exhaust gas register inlet (424) of the first exhaust gas register (42) and is positioned below the partition plate (421);
the first mixer runner (44) is venturi, and the inlet and outlet opening angle is 60-90 degrees.
7. The device according to claim 6, characterized in that the flow rate of the first primary air lance (411), the first secondary air lance (412), the first primary exhaust gas lance (422) and the first secondary exhaust gas lance (423) is 40-60 m/s.
8. The apparatus of claim 6, wherein the axes of the plurality of first primary exhaust nozzles (422) are co-located with a radius r 1 Is tangent to a circle, r 1 The value of (2) is smaller than or equal to the radius R of the cross section of the inner cavity of the first waste gas register (42) 1 1/6 of (2);
the axes of the first plurality of secondary exhaust nozzles (423) are co-located with a radius r 2 Is tangent to a circle, r 2 Is the value of the section radius R of the inner cavity of the first waste gas register (42) 1 1/3 to 1/2 of the total weight of the product.
9. The device according to claim 6, characterized in that the first ammonia gas distributor (43) is provided with a plurality of first ammonia gas nozzles (431) in the axial direction, two first ammonia gas nozzles (431) are provided for each axial position, the axes of the two first ammonia gas nozzles (431) intersect the axis of the first ammonia gas distributor (43), and the included angle of the axes of the two first ammonia gas nozzles (431) is 90 °.
10. A device according to any one of claims 1 to 3, characterized in that the second mixer (6) is provided with a second exhaust gas register (61), a second ammonia distributor (62), a plurality of first air jets (63) and a second mixer flow channel (64);
the second exhaust gas register (61) is arranged at the periphery of the furnace shell in a ring cavity structure, and the second exhaust gas register (61) is provided with a plurality of second-stage exhaust gas spray pipes (611) and a plurality of second-stage exhaust gas spray pipes (612);
the second ammonia gas distributor (62) is disposed within a second exhaust gas register inlet (613) of the second exhaust gas register (61);
the plurality of first air nozzles (63) are arranged between the second-stage exhaust gas nozzles (611) and the second-stage exhaust gas nozzles (612) and penetrate through the second exhaust gas register (61);
the second mixer runner (64) is venturi, and the inlet and outlet opening angle is 60-90 degrees.
11. The device according to claim 10, characterized in that the flow rate of the second primary exhaust gas lance (611), the second secondary exhaust gas lance (612) is 40-60 m/s and the flow rate of the first air lance (63) is 30-40 m/s.
12.The apparatus of claim 10, wherein the axes of the plurality of second stage exhaust nozzles (611) are co-located with a radius r 3 Is tangent to a circle, r 3 Is smaller than or equal to the radius R of the cross section of the inner cavity of the second exhaust gas register (61) 2 1/6 of (2);
the axes of the plurality of second-stage exhaust gas nozzles (612) are commonly aligned with a radius r 4 Is tangent to a circle, r 4 Is the value of the section radius R of the inner cavity of the second waste gas register (61) 2 1/3 of (C);
the axes of the first air nozzles (63) are common with a radius r 5 Is tangent to a circle, r 5 Is the value of the section radius R of the inner cavity of the second waste gas register (61) 2 1/2 of (C).
13. The device according to claim 10, characterized in that a plurality of second ammonia gas nozzles (621) are axially arranged in the second ammonia gas distributor (62), two second ammonia gas nozzles (621) are arranged corresponding to each axial position, the axes of the two second ammonia gas nozzles (621) intersect with the axes of the second ammonia gas distributor (62), and the included angle of the axes of the two second ammonia gas nozzles (621) is 90 °.
14. A device according to any one of claims 1 to 3, characterized in that the third mixer (9) is provided with a second air register (91) and a third mixer flow channel (92);
the second air register (91) is arranged on the periphery of the furnace shell in a ring cavity structure, the second air register (91) is provided with a second air spray pipe (911), and the second air spray pipe (911) is perpendicular to the central line of the third mixer runner (92);
the third mixer runner (92) is in a contracted shape, and the inlet opening angle is 60-90 degrees.
15. The apparatus according to claim 14, wherein a plurality of second air jets (911) are respectively arranged in a plane of a plurality of axial positions along an axial direction of the third mixer flow path (92), adjacent to the third mixingThe axes of the plurality of second air nozzles (911) at the inlet of the combiner runner (92) are common with a radius r 6 Is tangent to a circle, and the axes of the second air nozzles (911) near the outlet of the third mixer flow passage (92) are together with a radius r 7 Is tangent to a circle, r 6 ＜r 7 。
16. The apparatus according to claim 14, characterized in that the second air jet (911) closest to the outlet of the third mixer flow channel (92) has a flow rate of 40-60 m/s.
17. A device according to any one of claims 1 to 3, characterized in that the air introduced into the burner (1), the first reduction zone (2), the second reduction zone (3), the first mixer (4) is preheated air, and the air introduced into the second mixer (6), the third mixer (9) is ambient temperature air.
18. A device according to any one of claims 1 to 3, characterized in that the tangential jet swirls produced by the first mixer (4), the second mixer (6) and the third mixer (9) are all identical.
19. A device according to any one of claims 1 to 3, wherein the device meets at least one of the following:
the residual oxygen coefficient of the burner (1) is 0.75-0.85;
the residual oxygen coefficient of the first reduction zone (2) is 0.75-0.85;
the combustion temperature of the first reduction zone (2) is 1100-1500 ℃;
the first reduction zone (2) has a flue gas residence time of >1s;
the residual oxygen coefficient of the second reduction zone (3) is 0.75-0.85;
the combustion temperature of the second reduction zone (3) is 1100-1250 ℃;
the second reduction zone (3) has a flue gas residence time of >1s;
the oxygen content of the first oxidation zone (5) is 0.3-0.4;
the combustion temperature of the first oxidation zone (5) is 900-1200 ℃;
the first oxidation zone (5) has a flue gas residence time of >1s;
the oxygen content of the second oxidation zone (7) is 0.2-0.6;
the combustion temperature of the second oxidation zone (7) is 800-950 ℃;
the oxygen content of the SNCR zone (8) is 0.2-0.3;
the combustion temperature of the SNCR zone (8) is 800-950 ℃;
-the combined flue gas residence time of the second oxidation zone (7) and the SNCR zone (8) is >1s;
the combustion temperature of the solid salt temperature adjustment area (10) is 600-700 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223094698.7U CN220471634U (en) | 2022-11-21 | 2022-11-21 | Combined incineration device for acrylonitrile waste gas and waste liquid |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223094698.7U CN220471634U (en) | 2022-11-21 | 2022-11-21 | Combined incineration device for acrylonitrile waste gas and waste liquid |
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| CN220471634U true CN220471634U (en) | 2024-02-09 |
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| CN202223094698.7U Active CN220471634U (en) | 2022-11-21 | 2022-11-21 | Combined incineration device for acrylonitrile waste gas and waste liquid |
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| Country | Link |
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| CN (1) | CN220471634U (en) |
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