A combined incineration device for acrylonitrile waste gas and waste liquid

Abstract

This application discloses a co-incineration device for acrylonitrile waste gas and waste liquid, comprising: a burner for treating fuel and high-calorific-value waste liquid; a high-temperature reduction zone for treating high-calorific-value waste liquid and a small amount of low-calorific-value wastewater, equipped with preheated combustion air or a small amount of preheated waste gas; a low-temperature reduction zone for treating low-calorific-value wastewater, equipped with preheated combustion air or a small amount of preheated waste gas; a high-temperature mixer equipped with a preheated air distributor, a preheated waste gas distributor, and an ammonia distribution pipe; a high-temperature oxidation zone providing space for upstream reduction flue gas or waste gas to undergo chemical reactions; a medium-temperature mixer equipped with a room-temperature air distributor, a preheated waste gas distributor, and an ammonia distribution pipe; a low-temperature oxidation zone providing space for upstream flue gas or waste gas to undergo chemical reactions; a low-temperature mixer equipped with a room-temperature air distributor; and a solid salt temperature regulation zone providing space for cooling upstream flue gas and uniformly distributing flue gas flow rate. The solution of this application can achieve the purpose of controlling fuel-type NOx, with a longer flue gas residence time and better mixing effect.

Description

Technical Field

[0001] This application relates to the technical field of acrylonitrile waste gas and waste liquid, and in particular to a combined incineration device for acrylonitrile waste gas and waste liquid. Background Technology

[0002] BHK Corporation of Japan possesses a patented multi-stage incineration technology that simultaneously treats waste gas and waste liquid. This technology introduces waste gas and waste liquid generated during acrylonitrile production into the incinerator, where they are injected through multi-stage nozzles at a suitable combustion ratio. This maintains the furnace temperature at the optimal ignition temperature for the combustible substances in the waste gas and waste liquid, reducing fuel consumption and effectively controlling excessive temperature rise during incineration, thus suppressing NOx formation. Simultaneously, the CN- contained in the waste gas and waste liquid reduces NOx generated during incineration to N2, further reducing NOx formation. A similar technical solution is found in the patent "Acrylonitrile Production Waste Liquid and Waste Gas Incinerator" proposed by Ningbo Institute of Technology. This solution is similar to BHK's, also employing a staged fuel method to treat waste gas and waste liquid. The difference lies in that BHK uses bottom-fired positive pressure operation, while Ningbo Institute of Technology uses top-fired negative pressure operation.

[0003] However, the operating process parameters of the above scheme do not meet the technical performance requirements of the national standard GB 18484 Hazardous Waste Incineration Pollution Control Standard issued in my country in 2020. It does not have a significant high-temperature residence time - that is, a residence time of >1100℃ for 2 seconds, which makes it impossible to apply in my country at present.

[0004] The current mainstream technical solutions for acrylonitrile waste gas and waste liquid that meet national standards adopt separate treatment of waste gas and waste liquid, with two separate sets of equipment. This results in a large project footprint, limited equipment performance, and the inability to shut down the main unit due to failure of any equipment, and lacks the ability to make emergency adjustments. Summary of the Invention

[0005] The purpose of this application is to develop an incineration device suitable for simultaneously or separately treating acrylonitrile waste gas and waste liquid. This combined incineration device for acrylonitrile waste gas and waste liquid can effectively solve the above-mentioned defects, and achieve a NOx concentration at the incinerator outlet of less than 150 mg / Nm3 (oxygen 3% v) while meeting national environmental protection standards.

[0006] In a first aspect, an acrylonitrile waste gas and waste liquid co-incineration device is provided, comprising:

[0007] The burner, first reduction zone, second reduction zone, first mixer, first oxidation zone, second mixer, second oxidation zone, selective non-catalytic reduction (SNCR) zone, third mixer, and solid salt temperature control zone are connected in sequence.

[0008] The burner is used to treat fuel and waste liquid under the action of air, the first waste liquid including hydrogen cyanide waste liquid;

[0009] The first reduction zone is used to treat waste liquids with different calorific values ​​under the action of air. The volume of the first reduction zone meets the requirements that the flue gas residence time is >1s under the combined operation of waste gas and waste liquid, and the flue gas residence time is >0.5s under the condition of waste liquid alone.

[0010] The second reduction zone is used to treat waste liquid under the action of air. The calorific value of the waste liquid treated in the second reduction zone is lower than that of the waste liquid treated in the first reduction zone. The volume of the second reduction zone meets the requirement that the flue gas residence time is >1s under the combined operation of waste gas and waste liquid, and >0.5s under the operation of waste liquid alone.

[0011] The first mixer is used to mix air, exhaust gas, ammonia, and reactants from the second reduction zone, and to pass the mixed mixture into the first oxidation zone;

[0012] The first oxidation zone is used to process the mixture from the first mixer. The volume of the first oxidation zone satisfies the following conditions: flue gas residence time > 1s under combined waste gas and waste liquid conditions, and flue gas residence time > 1.35s under waste liquid-only conditions.

[0013] The second mixer is used to mix air, exhaust gas, ammonia, and reactants from the first oxidation zone, and to pass the mixed mixture into the second oxidation zone;

[0014] The second oxidation zone is used to process the mixture from the second mixer, and the volume of the second oxidation zone satisfies the requirement that the flue gas residence time is >0.5s;

[0015] The volume of the SNCR zone satisfies a flue gas residence time > 0.5s;

[0016] The third mixer is used to mix air and reactants from the SNCR zone, and to pass the mixed mixture into the solid salt temperature control zone;

[0017] The volume of the solid salt temperature regulation zone meets the requirement that the flue gas residence time is >0.5s.

[0018] Compared with the prior art, the solution provided in this application has at least the following beneficial technical effects:

[0019] This application divides the furnace body into multiple functional zones to separately treat different types and flow rates of waste gas and waste liquid process streams, in order to meet the corresponding requirements of national standards, especially the requirements for residence time and incineration temperature. It simultaneously controls the generation and emission of NOx, with the waste liquid containing a large amount of organic nitrogen compounds and the waste gas carrying 400-600 mg / Nm3 of NOx and a small amount of organic nitrogen compounds. The burner can provide the initial heat source required by the incineration unit.

[0020] The first and second reduction zones provide the necessary space for chemical reactions. The first mixer switches and injects process gas streams under different operating conditions, rapidly mixes and reacts with the upstream reduction flue gas, and regulates the temperature and oxygen content of the high-temperature oxidation zone. The first and second reduction zones provide the necessary space for chemical reactions. The first mixer switches and injects process gas streams under different operating conditions, rapidly mixes and reacts with the upstream reduction flue gas, and regulates the temperature and oxygen content of the low-temperature oxidation zone. The first oxidation zone provides space for the upstream reduction flue gas or waste gas to undergo chemical reactions at appropriate temperature and oxygen content. The second mixer switches and injects process gas streams under different operating conditions, rapidly mixes and reacts with the upstream flue gas, and regulates the temperature and oxygen content of the low-temperature oxidation zone. The second oxidation zone provides space for the upstream flue gas or waste gas to undergo chemical reactions at appropriate temperature and oxygen content. The SNCR zone provides space for the upstream reduction flue gas to undergo chemical reactions at appropriate temperature and oxygen content. The third mixer rapidly cools the flue gas. The solid salt temperature regulation zone provides space for cooling the upstream flue gas and uniformly distributing the flue gas velocity.

[0021] In conjunction with the first aspect, in some implementations of the first aspect, the burner, the first reduction zone, the second reduction zone, the first mixer, and the first portion of the first oxidation zone are arranged along a first direction, and the second portion of the first oxidation zone, the second mixer, the second oxidation zone, the SNCR zone, the third mixer, and the solid salt temperature control zone are arranged along a second direction, wherein the first direction and the second direction are perpendicular to each other.

[0022] In conjunction with the first aspect, in some implementations of the first aspect, a throttling ring is provided at the inlet of the second part of the first oxidation zone, and the inner diameter of the throttling ring is 0.75 to 0.8 times the inner diameter of the first oxidation zone.

[0023] In conjunction with the first aspect, in some implementations 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 nozzles. The first nozzles are used to introduce air and / or waste gas. The waste liquid gun and the first waste water gun are placed inside the first nozzles. The flow velocity of the first nozzle is 35 to 50 m / s.

[0024] In conjunction with the first aspect, in some implementations of the first aspect, the second reduction zone is provided with a second distributor and a second wastewater gun. The second distributor is provided with a plurality of second nozzles. The second nozzles are used to introduce air and / or waste gas. The second wastewater gun is placed inside the second nozzles. The flow velocity of the second nozzles is 35 to 50 m / s.

[0025] In conjunction with the first aspect, in some implementations of the first aspect, the first mixer is provided with a first air register, a first exhaust gas register, a first ammonia distributor, and a first mixer channel;

[0026] The first air register is arranged in a ring cavity structure around the first exhaust gas register. The first air register is provided with multiple first-stage air nozzles and multiple first-second-stage air nozzles.

[0027] The first exhaust gas register is arranged in a ring structure around the furnace shell and is divided into two parallel chambers by a partition plate. The first exhaust gas register is equipped with multiple first-stage exhaust gas nozzles and multiple first-stage exhaust gas nozzles. The first-stage exhaust gas nozzles and the first-stage exhaust gas nozzles are placed in the two chambers respectively. The first-stage air nozzle is located at the center of the first-stage exhaust gas nozzle, and the first-stage air nozzle is located at the center of the first-stage exhaust gas nozzle. The first-stage exhaust gas nozzle is perpendicular to the center line of the first mixer channel, and the angle between the first-stage exhaust gas nozzle and the center line of the first mixer channel is 30° to 45°.

[0028] The first ammonia distributor is placed inside the first waste gas register inlet of the first waste gas register, below the partition plate;

[0029] The first mixer has a venturi-shaped flow channel with an inlet and outlet angle of 60° to 90°.

[0030] In conjunction with the first aspect, in some implementations of the first aspect, the flow velocity of the first primary air nozzle, the first secondary air nozzle, the first primary exhaust gas nozzle, and the first secondary exhaust gas nozzle is 40 to 60 m / s.

[0031] In conjunction with the first aspect, in some implementations of the first aspect, the axes of the plurality of first-stage exhaust gas nozzles are tangent to a circle with radius r1, where the value of r1 is less than or equal to 1 / 6 of the radius R1 of the inner cavity of the first exhaust gas register.

[0032] The axes of the multiple first and second stage exhaust gas nozzles are all tangent to a circle with a radius of r2, where r2 is 1 / 3 to 1 / 2 of the radius R1 of the inner cavity of the first exhaust gas register.

[0033] In conjunction with the first aspect, in some implementations of the first aspect, the first ammonia distributor is provided with a plurality of first ammonia nozzles along its axial direction, with two first ammonia nozzles provided at each axial position, the axes of the two first ammonia nozzles intersecting the axis of the first ammonia distributor, and the included angle between the axes of the two first ammonia nozzles being 90°.

[0034] In conjunction with the first aspect, in some implementations of the first aspect, the second mixer is provided with a second exhaust gas register, a second ammonia distributor, a plurality of first air nozzles and a second mixer channel;

[0035] The second exhaust gas register is arranged in an annular cavity structure around the furnace shell. The second exhaust gas register is equipped with multiple second-stage exhaust gas nozzles and multiple second-stage exhaust gas nozzles.

[0036] The second ammonia distributor is placed inside the inlet of the second exhaust gas register of the second exhaust gas register;

[0037] The plurality of first air nozzles are positioned between the second primary exhaust gas nozzle and the second secondary exhaust gas nozzle, and pass through the second exhaust gas register;

[0038] The second mixer has a Venturi-shaped flow channel with an inlet and outlet angle of 60° to 90°.

[0039] In conjunction with the first aspect, in some implementations of the first aspect, the flow velocity of the second-stage exhaust gas nozzle and the second-secondary exhaust gas nozzle is 40-60 m / s, and the flow velocity of the first air nozzle is 30-40 m / s.

[0040] In conjunction with the first aspect, in some implementations of the first aspect, the axes of the plurality of second-stage exhaust gas nozzles are tangent to a circle with a radius of r3, where the value of r3 is less than or equal to 1 / 6 of the radius R2 of the inner cavity of the second exhaust gas register.

[0041] The axes of the multiple second and second stage exhaust gas nozzles are all tangent to a circle with a radius of r4, where r4 is 1 / 3 of the radius R2 of the inner cavity of the second exhaust gas register.

[0042] The axes of the plurality of first air nozzles are all tangent to a circle with a radius of r5, where r5 is half the radius R2 of the inner cavity of the second exhaust gas register.

[0043] In conjunction with the first aspect, in some implementations of the first aspect, the second ammonia distributor is provided with a plurality of second ammonia nozzles along its axial direction, with two second ammonia nozzles provided at each axial position, the axes of the two second ammonia nozzles intersecting the axis of the second ammonia distributor, and the included angle between the axes of the two second ammonia nozzles being 90°.

[0044] In conjunction with the first aspect, in some implementations of the first aspect, the third mixer is provided with a second air register and a third mixer channel;

[0045] The second air register is arranged in a ring cavity structure around the furnace shell. The second air register is equipped with a second air nozzle, which is perpendicular to the center line of the flow channel of the third mixer.

[0046] The third mixer has a converging flow channel with an inlet angle of 60° to 90°.

[0047] In conjunction with the first aspect, in some implementations of the first aspect, multiple second air nozzles are arranged on planes at multiple axial positions along the axial direction of the third mixer channel. The axes of the multiple second air nozzles near the inlet of the third mixer channel are tangent to a circle with radius r6, and the axes of the multiple second air nozzles near the outlet of the third mixer channel are tangent to a circle with radius r7, where r6 < r7.

[0048] In conjunction with the first aspect, in some implementations of the first aspect, the flow velocity of the second air nozzle closest to the outlet of the third mixer channel is 40 to 60 m / s.

[0049] In conjunction with the first aspect, in some implementations of the first aspect, the air introduced into the burner, the first reduction zone, the second reduction zone, and the first mixer is preheated air, and the air introduced into the second mixer and the third mixer is ambient temperature air.

[0050] In conjunction with the first aspect, in some implementations of the first aspect, the tangential jets generated by the first mixer, the second mixer, and the third mixer all have the same swirl direction.

[0051] In conjunction with the first aspect, in certain implementations of the first aspect, the apparatus satisfies at least one of the following:

[0052] The residual oxygen coefficient of the burner is 0.75 to 0.85;

[0053] The residual oxygen coefficient in the first reduction zone is 0.75–0.85;

[0054] The combustion temperature in the first reduction zone is 1100–1500℃;

[0055] The residence time of flue gas in the first reduction zone is >1 second;

[0056] The residual oxygen coefficient in the second reduction zone is 0.75–0.85;

[0057] The combustion temperature in the second reduction zone is 1100–1250°C;

[0058] The residence time of flue gas in the second reduction zone is >1 second;

[0059] The oxygen content of the first oxidation zone is 0.3 to 0.4.

[0060] The combustion temperature of the first oxidation zone is 900–1200°C;

[0061] The residence time of flue gas in the first oxidation zone is >1 second;

[0062] The oxygen content of the second oxidation zone is 0.2–0.6.

[0063] The combustion temperature in the second oxidation zone is 800–950°C;

[0064] The oxygen content in the SNCR region is 0.2–0.3.

[0065] The combustion temperature of the SNCR zone is 800–950°C;

[0066] The combined flue gas residence time of the second oxidation zone and the SNCR zone is >1 second;

[0067] The combustion temperature of the solid salt temperature regulation zone is 600-700℃.

[0068] This application employs a waste liquid reduction oxidation incineration method to control fuel-type NOx. In the reduction zone, the waste liquid undergoes anaerobic combustion, converting most of the organic nitrogen compounds into N2. Simultaneously, a large amount of reducing atmosphere is generated and enters the oxidation zone to reduce the formation of thermal NOx in the oxidation zone.

[0069] This application employs a direct ammonia injection method into the exhaust gas to control inherent NOx. NH3 gas and exhaust gas are rapidly mixed and cooled with the reduction flue gas through a mixer to achieve the optimal reaction temperature. Compared to traditional SNCR technology, this method offers a longer residence time and better mixing effect. Attached Figure Description

[0070] Figure 1 This is a schematic structural diagram of the incineration device of this application.

[0071] Figure 2 This is a structural diagram of the high-temperature reduction zone.

[0072] Figure 3 This is a structural diagram of the low-temperature reduction region.

[0073] Figure 4 This is a structural diagram of a high-temperature mixer.

[0074] Figure 5 This is another structural diagram of a high-temperature mixer.

[0075] Figure 6 This is a structural diagram of a medium-temperature mixer.

[0076] Figure 7 This is another structural diagram of a medium-temperature mixer.

[0077] Figure 8 This is a structural diagram of a cryogenic mixer.

[0078] Figure 9 This is a structural diagram of an ammonia gas distributor. Detailed Implementation

[0079] The present application will now be described in further detail with reference to the accompanying drawings and specific embodiments.

[0080] The incineration device described in this application can be either linear or L-shaped, depending on the requirements. Figure 1 The diagram shows an L-shape.

[0081] The basic structure of the incineration device of this application includes: a burner 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 control zone 10, etc., which are connected in sequence.

[0082] Burner 1 processes fuel and high-calorific-value waste liquid, including hydrogen cyanide waste liquid, and is equipped with preheated combustion air to provide a stable heat source for the incineration unit. The fuel can be, for example, natural gas or diesel.

[0083] like Figure 2 As shown, the high-temperature reduction zone 2 is equipped with a high-calorific-value waste liquid gun 21, a low-calorific-value wastewater gun 22, and a preheating combustion air / exhaust gas distributor 23. The preheating combustion air / exhaust gas distributor 23 is equipped with multiple air / exhaust gas nozzles 231. The high-calorific-value waste liquid gun 21 and the low-calorific-value wastewater gun 22 are placed inside the air / exhaust gas nozzles 231, and the flow velocity of the air / exhaust gas nozzles 231 is 35-50 m / s. The volume of the high-temperature reduction zone 2 ensures that the flue gas residence time is >1s under the combined operation of waste gas and waste liquid, and >0.5s under the condition of waste liquid alone.

[0084] The low-temperature reduction zone 3 is equipped with a preheated air / exhaust gas distributor 31 and a low-calorific-value wastewater gun 32. The preheated air / exhaust gas distributor 31 has multiple air / exhaust gas nozzles 311, and the low-calorific-value wastewater gun 32 is placed inside the air / exhaust gas nozzles 311. The flow velocity of the air / exhaust gas nozzles 311 is 35-50 m / s. The volume of the low-temperature reduction zone 3 ensures that the flue gas residence time is >1s under combined waste gas and waste liquid conditions, and >0.5s under waste liquid-only conditions.

[0085] The high-temperature mixer 4 includes a preheated air register 41, an exhaust gas register 42, an ammonia distributor 43, and a high-temperature mixer flow channel 44. The preheated air register 41, in a ring-shaped structure, is located around the exhaust gas register 42 and is equipped with multiple primary air nozzles 411 and multiple secondary air nozzles 412. The exhaust gas register 42, also in a ring-shaped structure, is located around the furnace shell and is divided into two parallel chambers by a partition plate 421. The exhaust gas register 42 is equipped with multiple primary exhaust gas nozzles 422 and multiple secondary exhaust gas nozzles 423. The primary exhaust gas nozzles 422 and 423 are located in the two chambers respectively. The primary air nozzles 411 are located at the center of the primary exhaust gas nozzles 422, and the secondary air nozzles 412 are located at the center of the secondary exhaust gas nozzles 423. Figure 4 and Figure 9 The ammonia distributor 43 is located inside the exhaust gas register inlet 424, below the partition plate 421, and is used by the secondary exhaust gas nozzle 422. The high-temperature mixer channel 44 is venturi-shaped (i.e., waist-shaped), and the inlet and outlet angles can be selected between 60° and 90°.

[0086] The design flow velocity for the primary air nozzle 411 and the secondary air nozzle 412 is 40–60 m / s. For example... Figure 5 As shown, multiple primary exhaust gas nozzles 422 can be evenly distributed circumferentially on the exhaust gas register 42. The axes of the multiple primary exhaust gas nozzles 422 can all be tangent to a circle with radius r1. The value of r1 can be, for example, less than or equal to 1 / 6 of the radius R1 of the inner cavity of the exhaust gas register 42.

[0087] The design flow velocities for the primary exhaust gas nozzle 422 and the secondary exhaust gas nozzle 423 are 40–60 m / s. The primary exhaust gas nozzle 422 is perpendicular to the centerline of the high-temperature mixer channel 44. The angle between the secondary exhaust gas nozzle 423 and the centerline of the high-temperature mixer channel 44 is 30°–45°. Figure 5 As shown, multiple secondary exhaust gas nozzles 423 can be evenly distributed circumferentially on the exhaust gas register 42. The axes of the multiple secondary exhaust gas nozzles 423 can all be tangent to a circle with radius r2. The value of r2 can be greater than r1. For example, the value of r2 can be 1 / 3 to 1 / 2 of the radius R1 of the inner cavity of the exhaust gas register 42. The secondary exhaust gas nozzles 423 and their corresponding primary exhaust gas nozzles 422 have the same rotation direction.

[0088] exist Figure 9 In the illustrated embodiment, a plurality of ammonia nozzles 431 are arranged along the axial direction of the ammonia distributor 43. Two ammonia nozzles 431 can be arranged for each axial position, the axes of the two ammonia nozzles 431 intersect the axis of the ammonia distributor 43, and the included angle between the axes of the two ammonia nozzles 431 can be 60 to 120°, for example, 90°.

[0089] For L-shaped furnaces, the high-temperature oxidation zone 5 is equipped with a throttling ring 51, the inner diameter of which is 0.75 to 0.8 times the inner diameter of the furnace; for linear furnaces, the throttling ring 51 may not be present. The volume of the high-temperature oxidation zone 5 ensures that the flue gas residence time is >1s under combined waste gas and waste liquid conditions, and >1.35s under waste liquid-only conditions.

[0090] The intermediate-temperature mixer 6 includes an exhaust gas register 61, an ammonia distributor 62, multiple ambient-temperature air nozzles 63, and an intermediate-temperature mixer flow channel 64. The exhaust gas register 61, in an annular structure, is located around the furnace shell and is equipped with multiple primary exhaust gas nozzles 611 and multiple secondary exhaust gas nozzles 612. Combined with... Figure 7 and Figure 9 The ammonia distributor 62 is located inside the exhaust gas register inlet 613. Multiple cryogenic air nozzles 63 are located between the primary exhaust gas nozzle 611 and the secondary exhaust gas nozzle 612, passing through the exhaust gas register 61. The medium-temperature mixer channel 64 is venturi-shaped, and the inlet and outlet angles can be selected between 60° and 90°.

[0091] like Figure 7 As shown, the primary exhaust gas nozzle 611 is designed to have a flow velocity of 40–60 m / s. The nozzle 611 is perpendicular to the centerline of the intermediate temperature mixer channel 64. Multiple primary exhaust gas nozzles 611 can be evenly distributed circumferentially on the exhaust gas register 61. The axes of the multiple primary exhaust gas nozzles 611 can all be tangent to a circle with radius r3. The value of r3 can, for example, be less than or equal to 1 / 6 of the radius R2 of the inner cavity of the exhaust gas register 61.

[0092] like Figure 7 As shown, the secondary exhaust gas nozzle 612 is designed to have a flow velocity of 40–60 m / s, and the angle between the secondary exhaust gas nozzle 612 and the centerline of the intermediate temperature mixer channel 64 is 15°–30°. Multiple secondary exhaust gas nozzles 612 can be evenly distributed circumferentially on the exhaust gas register 61. The axes of the multiple secondary exhaust gas nozzles 612 can all be tangent to a circle with radius r4. The value of r4 can be greater than r3. For example, the value of r4 can be 1 / 3 of the radius R2 of the inner cavity of the exhaust gas register 61. The secondary exhaust gas nozzles 612 and their corresponding primary exhaust gas nozzles 611 have the same rotation direction.

[0093] like Figure 7 As shown, the cryogenic air nozzle 63 is designed to have a flow velocity of 30–40 m / s. Multiple cryogenic air nozzles 63 can be evenly distributed circumferentially on the exhaust gas register 61. The axes of the multiple cryogenic air nozzles 63 can all be tangent to a circle of radius r5. The value of r5 can be greater than r4. For example, the value of r5 can be half of the radius R2 of the inner cavity of the exhaust gas register 61. The number of multiple cryogenic air nozzles 63 can be less than the number of multiple first-stage exhaust gas nozzles 611.

[0094] exist Figure 9In the illustrated embodiment, a plurality of ammonia nozzles 621 are arranged along the axial direction of the ammonia distributor 62. Two ammonia nozzles 621 can be arranged for each axial position, the axes of the two ammonia nozzles 621 intersect the axis of the ammonia distributor 62, and the included angle between the axes of the two ammonia nozzles 621 can be 60 to 120°, for example, the included angle is 90°.

[0095] The volume of the low-temperature oxidation zone 7 ensures that the flue gas residence time is >0.5s under any operating condition.

[0096] The inlet of SNCR zone 8 is equipped with an SNCR spray gun 81. The volume of SNCR zone 8 ensures that the flue gas residence time is >0.5s under any operating condition.

[0097] The cryogenic mixer 9 is equipped with a room temperature air register 91 and a cryogenic mixer flow channel 92. The room temperature air register 91 is a ring cavity structure placed around the furnace shell and is equipped with an air nozzle 911. The cryogenic mixer flow channel 92 is a contraction type, and the inlet angle can be selected between 60° and 90°. The air nozzle 911 is perpendicular to the center line of the cryogenic mixer flow channel 92.

[0098] Multiple air nozzles 911 are arranged on a plane at multiple axial positions along the axial direction of the cryogenic mixer channel 92. The multiple air nozzles 911 at each axial position can be evenly distributed around the axial direction of the cryogenic mixer channel 92. The axes of the multiple air nozzles 911 near the inlet of the cryogenic mixer channel 92 can be tangent to a circle with radius r6, and the axes of the multiple air nozzles 911 near the outlet of the cryogenic mixer channel 92 can be tangent to a circle with radius r7, where r6 < r7. The flow velocity of the air nozzle 911 closest to the outlet of the cryogenic mixer channel 92 is 40–60 m / s.

[0099] The tangential jets generated by the high-temperature mixer 4, the medium-temperature mixer 6, and the low-temperature mixer 9 all have the same swirl direction. That is to say, the swirl direction of the multiple primary air nozzles 411, multiple secondary air nozzles 412, multiple primary exhaust gas nozzles 611, multiple secondary exhaust gas nozzles 612, multiple low-temperature air nozzles 63, and multiple air nozzles 911 is consistent.

[0100] The volume of the solid salt temperature regulation zone 10 ensures that the flue gas residence time is >0.5s under any operating condition.

[0101] Example 1

[0102] The device incinerates waste gas and waste liquid. Burner 1 treats fuel and high-calorific-value waste liquid with a residual oxygen coefficient of 0.75–0.85. High-temperature reduction zone 2 treats waste liquid and a small amount of wastewater with a residual oxygen coefficient of 0.75–0.85, a combustion temperature of 1350–1500℃, and a residence time >1s. Low-temperature reduction zone 3 treats a small amount of waste gas with a residual oxygen coefficient of 0.75–0.85, a combustion temperature of 1100–1250℃, and a residence time >1s. High-temperature mixer 4 introduces preheated air… Large amounts of preheated waste gas and ammonia are introduced; in the high-temperature oxidation zone 5, the oxygen content is 0.3-0.4, the combustion temperature is 900-1000℃, and the residence time is >1s; in the medium-temperature mixer 6, a large amount of preheated waste gas and ammonia are introduced; in the low-temperature oxidation zone 7 and SNCR zone 8, the oxygen content is 0.2-0.3, the combustion temperature is 800-850℃, and the total residence time is >1s; in the low-temperature mixer 9, room temperature air is introduced; in the solid salt temperature regulation zone 10, the temperature is reduced to about 650℃, and the residence time is >0.5s.

[0103] Example 2

[0104] The unit incinerates waste liquid. Burner 1 treats fuel and high-calorific-value waste liquid with a residual oxygen coefficient of 0.75–0.85. High-temperature reduction zone 2 treats waste liquid and a small amount of wastewater with a residual oxygen coefficient of 0.75–0.85, a combustion temperature of 1350–1500℃, and a residence time >0.5s. Low-temperature reduction zone 3 treats a large amount of wastewater with a residual oxygen coefficient of 0.75–0.85, a combustion temperature of 1100–1250℃, and a residence time >0.5s. High-temperature mixer 4 only introduces preheated air. In the oxidation zone 5, the oxygen content is 0.3-0.4%, the combustion temperature is >1100℃, and the residence time is >1.35s; ambient temperature air is introduced into the medium-temperature mixer 6; in the low-temperature oxidation zone 7, the oxygen content is >0.6%, the combustion temperature is about 950℃, and the residence time is >0.5s; in the SNCR zone 8, the SNCR spray gun 81 is turned on, the combustion temperature is about 950℃, and the residence time is >0.5s; ambient temperature air is introduced into the low-temperature mixer 9; in the solid salt temperature regulation zone 10, the temperature is reduced to about 650℃, and the residence time is >0.5s.

[0105] Example 3

[0106] The device incinerates waste gas. Burner 1 treats fuel with a residual oxygen coefficient of 0.75–0.85. High-temperature reduction zone 2 treats a small amount of waste gas with a residual oxygen coefficient of 0.75–0.85, combustion temperature >1100℃, and residence time >1s. Low-temperature reduction zone 3 treats a small amount of waste gas with a residual oxygen coefficient of 0.75–0.85, combustion temperature >1100℃, and residence time >1s. High-temperature mixer 4 introduces preheated air, a large amount of preheated waste gas, and ammonia. High-temperature oxidation zone 5 has an oxygen content of 0.3–0.4%, a combustion temperature of 900–1000℃, and a residence time >1s. Medium-temperature mixer 6 introduces a large amount of preheated waste gas and ammonia. Low-temperature oxidation zone 7 and SNCR zone 8 have an oxygen content of 0.2–0.3%, a combustion temperature of 800–850℃, and a combined residence time >1s. Low-temperature mixer 9 introduces ambient temperature air. Solid salt temperature regulation zone 10 reduces the temperature to approximately 650℃ and has a residence time >0.5s.

[0107] Although this application discloses preferred embodiments as described above, it is not intended to limit this application. Any person skilled in the art can make possible changes and modifications without departing from the spirit and scope of this application. Therefore, the scope of protection of this application should be determined by the scope defined in the claims of this application.

Claims

1. A co-incineration device for acrylonitrile waste gas and waste liquid, characterized in that, include: A burner (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 control zone (10) are connected in sequence; the first part of the burner (1), the first reduction zone (2), the second reduction zone (3), the first mixer (4), and the first oxidation zone (5) are arranged along a first direction, and 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), and the solid salt temperature control zone (10) are arranged along a second direction, and the first direction and the second direction are perpendicular to each other; The burner (1) is used to treat fuel and waste liquid under the action of air, the waste liquid including hydrogen cyanide waste liquid; The first reduction zone (2) is used to treat waste liquids and / or waste gases with different calorific values ​​under the action of air. The volume of the first reduction zone (2) satisfies that the flue gas residence time is >1s under the combined working condition of waste gas and waste liquid, and the flue gas residence time is >0.5s under the working condition of waste liquid alone. The second reduction zone (3) is used to treat waste liquid and / or waste gas under the action of air. The calorific 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) satisfies that the flue gas residence time is >1s under the combined working condition of waste gas and waste liquid, and the flue gas residence time is >0.5s under the working condition of waste liquid alone. The first mixer (4) is used to mix reactants from the second reduction zone (3) with one or more of air, exhaust gas, and ammonia, and to pass the mixed mixture into the first oxidation zone (5); The first oxidation zone (5) is used to process the mixture from the first mixer (4). The volume of the first oxidation zone (5) satisfies that the flue gas residence time is >1s under the combined operation of waste gas and waste liquid, and the flue gas residence time is >1.35s under the separate operation of waste liquid. The second mixer (6) is used to mix reactants from the first oxidation zone (5) with one or more of air, exhaust gas, and ammonia, and to pass the mixed mixture into the second oxidation zone (7). The second oxidation zone (7) is used to process the mixture from the second mixer (6), and the volume of the second oxidation zone (7) satisfies the flue gas residence time > 0.5s; The volume of the SNCR zone (8) satisfies the requirement that the flue gas residence time is >0.5s; The third mixer (9) is used to mix air and reactants from the SNCR zone (8) and to pass the mixed mixture into the solid salt temperature control zone (10). The volume of the solid salt temperature regulation zone (10) satisfies the requirement that the flue gas residence time is >0.5s.

2. The apparatus according to claim 1, characterized in that, The inlet of the second part of the first oxidation zone (5) is provided with a throttling ring (51), the inner diameter of which is 0.75 to 0.8 times the inner diameter of the first oxidation zone (5).

3. The apparatus according to any one of claims 1 to 2, characterized in that, The first reduction zone (2) is equipped with a waste liquid gun (21), a first waste water gun (22) and a first distributor (23). The first distributor (23) is equipped with multiple first nozzles (231). The first nozzles (231) are used to introduce air and / or waste gas. The waste liquid gun (21) and the first waste water gun (22) are placed inside the first nozzles (231). The flow rate of the first nozzles (231) is 35~50 m / s.

4. The apparatus according to any one of claims 1 to 2, characterized in that, The second reduction zone (3) is provided with a second distributor (31) and a second wastewater gun (32). The second distributor (31) is provided with multiple second nozzles (311). The second nozzles (311) are used to introduce air and / or exhaust gas. The second wastewater gun (32) is placed inside the second nozzles (311). The flow rate of the second nozzles (311) is 35~50 m / s.

5. The apparatus according to any one of claims 1 to 2, 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 channel (44). The first air register (41) is arranged in a ring cavity structure around the first exhaust gas register (42). The first air register (41) is provided with a plurality of first-stage air nozzles (411) and a plurality of first-stage and second-stage air nozzles (412). The first exhaust gas register (42) is arranged in a ring structure around the furnace shell and is divided into two parallel chambers by a partition plate (421). The first exhaust gas register (42) is provided with multiple first-stage exhaust gas nozzles (422) and multiple first-stage exhaust gas nozzles (423). The first-stage exhaust gas nozzles (422) and the first-stage exhaust gas nozzles (423) are respectively placed in the two chambers. The first-stage air nozzle (411) is placed in the center of the first-stage exhaust gas nozzle (422), and the first-stage air nozzle (412) is placed in the center of the first-stage exhaust gas nozzle (423). The first-stage exhaust gas nozzle (422) is perpendicular to the center line of the first mixer channel (44). The angle between the first-stage exhaust gas nozzle (423) and the center line of the first mixer channel (44) is 30°~45°. The first ammonia distributor (43) is placed inside the first exhaust gas register inlet (424) of the first exhaust gas register (42), below the partition plate (421); The first mixer channel (44) is Venturi-shaped, with an inlet and outlet angle of 60°~90°.

6. The apparatus according to claim 5, characterized in that, The flow velocity of the first primary air nozzle (411), the first secondary air nozzle (412), the first primary exhaust gas nozzle (422), and the first secondary exhaust gas nozzle (423) is 40~60m / s.

7. The apparatus according to claim 5, characterized in that, The axes of the multiple first-stage exhaust gas nozzles (422) are all tangent to a circle with radius r1, and the value of r1 is less than or equal to 1 / 6 of the radius R1 of the inner cavity of the first exhaust gas register (42). The axes of the multiple first and second stage exhaust gas nozzles (423) are all tangent to a circle with a radius of r2, where r2 is 1 / 3 to 1 / 2 of the radius R1 of the inner cavity of the first exhaust gas register (42).

8. The apparatus according to claim 5, characterized in that, The first ammonia distributor (43) is provided with a plurality of first ammonia nozzles (431) along its axial direction. Two first ammonia nozzles (431) are provided at each axial position. The axes of the two first ammonia nozzles (431) intersect the axis of the first ammonia distributor (43), and the included angle between the axes of the two first ammonia nozzles (431) is 90°.

9. The apparatus according to any one of claims 1 to 2, characterized in that, The second mixer (6) is provided with a second exhaust gas register (61), a second ammonia distributor (62), multiple first air nozzles (63) and a second mixer channel (64). The second exhaust gas register (61) is arranged in an annular cavity structure around the furnace shell. The second exhaust gas register (61) is provided with multiple second-stage exhaust gas nozzles (611) and multiple second-stage exhaust gas nozzles (612). The second ammonia distributor (62) is placed inside the second exhaust gas register inlet (613) of the second exhaust gas register (61); The plurality of first air nozzles (63) are positioned between the second first-stage exhaust gas nozzle (611) and the second second-stage exhaust gas nozzle (612), and pass through the second exhaust gas register (61). The second mixer channel (64) is Venturi-shaped, with an inlet and outlet angle of 60°~90°.

10. The apparatus according to claim 9, characterized in that, The flow velocity of the second-stage exhaust gas nozzle (611) and the second-stage exhaust gas nozzle (612) is 40~60m / s, and the flow velocity of the first air nozzle (63) is 30~40m / s.

11. The apparatus according to claim 9, characterized in that, The axes of the multiple second-stage exhaust gas nozzles (611) are all tangent to a circle with a radius of r3, where the value of r3 is less than or equal to 1 / 6 of the radius R2 of the inner cavity of the second exhaust gas register (61). The axes of the multiple second and second stage exhaust gas nozzles (612) are all tangent to a circle with a radius of r4, where r4 is 1 / 3 of the radius R2 of the inner cavity of the second exhaust gas register (61). The axes of the plurality of first air nozzles (63) are tangent to a circle with a radius of r5, where r5 is half the radius R2 of the inner cavity of the second exhaust gas register (61).

12. The apparatus according to claim 9, characterized in that, The second ammonia distributor (62) is provided with a plurality of second ammonia nozzles (621) along its axial direction. Two second ammonia nozzles (621) are provided for each axial position. The axes of the two second ammonia nozzles (621) intersect the axis of the second ammonia distributor (62), and the included angle between the axes of the two second ammonia nozzles (621) is 90°.

13. The apparatus according to any one of claims 1 to 2, characterized in that, The third mixer (9) is provided with a second air register (91) and a third mixer channel (92). The second air register (91) is arranged in a ring cavity structure around the furnace shell. The second air register (91) is provided with a second air nozzle (911), which is perpendicular to the center line of the third mixer channel (92). The third mixer channel (92) is constricted, with an inlet angle of 60°~90°.

14. The apparatus according to claim 13, characterized in that, Along the axial direction of the third mixer channel (92), multiple second air nozzles (911) are arranged on planes at multiple axial positions. The axes of the multiple second air nozzles (911) near the inlet of the third mixer channel (92) are tangent to a circle with radius r6, and the axes of the multiple second air nozzles (911) near the outlet of the third mixer channel (92) are tangent to a circle with radius r7, where r6 < r7.

15. The apparatus according to claim 13, characterized in that, The flow velocity of the second air nozzle (911) closest to the outlet of the third mixer channel (92) is 40~60m / s.

16. The apparatus according to any one of claims 1 to 2, characterized in that, The air introduced into the burner (1), the first reduction zone (2), the second reduction zone (3), and the first mixer (4) is preheated air, while the air introduced into the second mixer (6) and the third mixer (9) is ambient temperature air.

17. The apparatus according to any one of claims 1 to 2, characterized in that, The tangential jets generated by the first mixer (4), the second mixer (6), and the third mixer (9) all have the same swirl direction.

18. The apparatus according to any one of claims 1 to 2, characterized in that, The device satisfies 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 residence time of flue gas in the first reduction zone (2) is >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 residence time of flue gas in the second reduction zone (3) is >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 residence time of flue gas in the first oxidation zone (5) is >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 region (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 regulation zone (10) is 600~700℃.

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