Oxygen-enriched combustion control method and system for high-water-content organic waste liquid

Abstract

The invention relates to the field of waste liquid treatment control, in particular to an oxygen-enriched combustion control method and system for high-water-content organic waste liquid. The method comprises the following steps: obtaining high-water-content organic waste liquid; concentrating the high-content organic waste liquid to obtain a concentrated solution containing the concentrated organic waste liquid; adding pulverized coal into the concentrated solution, and stirring to obtain mixed slurry; atomizing the mixed slurry to obtain atomized liquid; the oxygen-enriched air and the oxygen concentration thereof are obtained; judging whether the oxygen content in the oxygen-enriched air is appropriate or not according to the oxygen concentration; if yes, introducing oxygen-enriched air into the atomized liquid in N times, and then combusting until the combustion is complete; the system comprises: a waste liquid storage unit; a waste liquid concentration unit; the stirring and mixing unit comprises a pulverized coal feeding part and a slurrying part; the combustion unit comprises a combustion furnace and an atomizer; the air inlet unit comprises an air blower, a heat exchanger and N sections of ventilation pipelines; the oxygen injection unit comprises an oxygen injection part, a pipeline valve group and an oxygen content sensor group; a control unit; the rigorous follow-up control on the oxygen content is realized.

Description

Technical Field

[0001] The invention relates to the field of organic waste liquid treatment control, and in particular to an oxygen-enriched combustion control method and system for organic waste liquid with high water content. Background Art

[0002] A large part of the industrial waste liquid is organic waste liquid, especially in the papermaking, pharmaceutical, pesticide, petrochemical, textile and other industries. The waste liquid discharged during the production process of these industries often has the characteristics of high organic concentration, complex composition, high difficulty in treatment and high treatment cost. The characteristic of organic waste liquid is that the biochemical oxygen demand (BOD) is greater than 100 mg·L -1 , Chemical Oxygen Demand (COD) is greater than 2000 mg·L -1 .

[0003] Generally, organic waste liquid contains C, H, O, N, S, etc., which have certain calorific values. Waste liquid with higher calorific value is combustible and can be used as fuel alone, while waste liquid with lower calorific value can also be burned after concentration or adding auxiliary fuel. However, at present, the combustion stage of organic fertilizer waste liquid generally adopts air combustion directly, which may lead to incomplete combustion of some organic waste liquid. If oxygen is introduced to assist combustion, the treatment cost of organic waste liquid will increase. Therefore, how to accurately control the oxygen content in the treatment stage of organic waste liquid is a technical problem that needs to be solved urgently. Summary of the invention

[0004] The present invention provides an oxygen-enriched combustion control method and system for organic waste liquid with high water content, so as to solve the technical problem that the oxygen content in the organic waste liquid treatment stage in the prior art cannot be accurately controlled.

[0005] In order to achieve the above object, the present invention adopts the following technical solution: A method for controlling oxygen-enriched combustion of organic waste liquid with high water content, the method comprising: Obtaining organic waste liquid with high water content; Concentrating the high-content organic waste liquid to obtain a concentrated liquid containing concentrated organic waste liquid; adding coal powder into the concentrated liquid and stirring to obtain a mixed slurry containing water, coal and waste liquid; Atomizing the mixed slurry to obtain an atomized liquid; Obtaining oxygen-enriched air and the oxygen concentration of the oxygen-enriched air; According to the oxygen concentration of the oxygen-enriched air, judging whether the oxygen content in the oxygen-enriched air is appropriate; If yes, the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; wherein N≥3 and N is an integer.

[0006] A further improvement of the present invention is that judging whether the oxygen content in the oxygen-enriched air is appropriate according to the oxygen concentration of the oxygen-enriched air specifically includes: Obtaining a standard oxygen concentration according to the total weight of the pulverized coal and the organic waste liquid in the atomized liquid; According to the oxygen concentration and the standard oxygen concentration, judging whether the oxygen content in the oxygen-enriched air is appropriate; If the oxygen concentration is greater than or equal to the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is appropriate, and the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; If the oxygen concentration is ≥ the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is inappropriate, and oxygen is added before making another judgment; Wherein, N≥3 and N is an integer.

[0007] A further improvement of the present invention is that the standard oxygen concentration is 24% to 35%; The air coefficient of the oxygen-enriched air is 1.05-1.25.

[0008] A further improvement of the present invention is that the oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 45% to 55% of the total amount of oxygen flow, the second oxygen flow rate accounts for 35% to 45% of the total amount of oxygen flow, and the third oxygen flow rate accounts for 5% to 15% of the total amount of oxygen flow.

[0009] A further improvement of the present invention is that the ratio of the heat input power of the concentrated liquid to the heat input power of the coal powder is 1:2-5; And / or, the ratio of the flow rate of the concentrated liquid to the flow rate of the coal powder is 2-10:1.

[0010] A further improvement of the present invention is that the water content of the high-water content organic waste liquid is greater than 70%, and the water content of the concentrated liquid is 10% to 20%.

[0011] An oxygen-enriched combustion control system for organic waste liquid with high water content, the system is applicable to the method described, and the system comprises: A waste liquid storage unit for storing organic waste liquid with high water content; A waste liquid concentration unit, wherein the liquid outlet of the waste liquid storage unit is connected to the liquid inlet of the waste liquid concentration unit, and is used to convert the organic waste liquid with high water content into a concentrated liquid containing concentrated organic waste liquid; A stirring and mixing unit, wherein the liquid outlet of the waste liquid concentration unit is connected to the liquid inlet of the stirring and mixing unit, so as to fully mix the coal powder and the concentrated liquid; the stirring and mixing unit comprises a coal powder feeding section and a pulping section, wherein the pulping section comprises a first feeding section and a second feeding section, the discharge port of the waste liquid concentration unit is connected to the first feeding section of the pulping section, and the discharge port of the coal powder feeding section is connected to the second feeding section of the pulping section; A combustion unit, wherein the feed port of the combustion unit is connected to the discharge port of the pulping part, the combustion unit comprises a combustion furnace and an atomizer, the feed port of the atomizer is connected to the discharge port of the pulping part, and the atomizer is arranged in the combustion furnace and is used to atomize and burn the mixed slurry; An air inlet unit, wherein the air outlet of the air inlet unit is connected to the air inlet of the combustion unit, and is used to provide the combustion unit with air required for combustion; the air inlet unit comprises a blower, a heat exchanger and N sections of ventilation ducts, the heat exchanger comprises a first air inlet and a second air inlet, the air outlet of the blower is connected to the first air inlet of the heat exchanger, the air outlet of the combustion furnace is connected to the second air inlet of the heat exchanger, the air outlet of the heat exchanger is connected to the air inlet of the N sections of ventilation ducts, and the air outlet of the N sections of ventilation ducts is connected to the air inlet of the combustion furnace, wherein N ≥ 3 and N is an integer; An oxygen injection unit, the oxygen injection unit comprises an oxygen injection part, a pipeline valve group and an oxygen content sensor group, the oxygen content sensor group is respectively arranged in the oxygen injection part and in the pipeline valve group, the air inlet of the oxygen injection part is connected to the air outlet of the heat exchanger through the pipeline valve group, and the air outlet of the oxygen injection part is connected to the air inlet of the N-section ventilation duct through the pipeline valve group; A control unit is connected to the pipeline valve group and the oxygen content sensor group respectively through electrical signals, and is used to control the oxygen content of the air entering the combustion furnace.

[0012] A further improvement of the present invention is that the N-section ventilation duct includes a first ventilation duct, a second ventilation duct and a third ventilation duct, the air inlets of the first ventilation duct, the second ventilation duct and the third ventilation duct are all connected to the air outlet of the oxygen injection part, and the air outlets of the first ventilation duct, the second ventilation duct and the third ventilation duct are all connected to the air inlet of the combustion furnace.

[0013] A further improvement of the present invention is that the oxygen injection part comprises an oxygen tank and an oxygen injection valve, the oxygen injection valve is provided with a first air inlet and a second air inlet, the first air inlet of the oxygen injection valve is connected to the air outlet of the heat exchanger, the second air inlet of the oxygen injection valve is connected to the air outlet of the oxygen tank, and the air outlet of the oxygen injection valve is connected to the air inlet of the combustion furnace; The pipeline valve group includes a first pipeline valve, a second pipeline valve and a third pipeline valve, and the oxygen content sensor group includes a first oxygen content sensor, a second oxygen content sensor and a third oxygen content sensor; The first oxygen content sensor and the first pipeline valve are both arranged in the gas outlet of the oxygen tank, and the first oxygen content sensor is arranged upstream of the first pipeline valve along the oxygen delivery direction; The second oxygen content sensor and the second pipeline valve are arranged in the second air inlet of the oxygen injection valve, and the second oxygen content sensor is arranged upstream of the second pipeline valve along the air delivery direction; The third oxygen content sensor and the third pipeline valve are arranged in the air outlet of the oxygen injection valve, and the third oxygen content sensor is arranged downstream of the third pipeline valve along the oxygen-enriched air delivery direction.

[0014] A further improvement of the present invention is that the system also includes an exhaust gas treatment unit, the heat exchanger includes a first air outlet and a second air outlet, the first air outlet of the heat exchanger is connected to the air inlet of the N-section ventilation duct, and the second air outlet of the heat exchanger is connected to the exhaust gas treatment unit.

[0015] Compared with the prior art, the present invention has at least the following beneficial technical effects: The present invention provides an oxygen-enriched combustion control method and system for organic waste liquid with high water content. The organic waste liquid is first concentrated, and then coal powder is added to the concentrated organic waste liquid to form a mixed slurry containing water, coal and waste liquid, thereby introducing coal powder as a combustion aid. Since the calorific value of coal powder and the oxygen value required for combustion are both easy to measure, the amount of required oxygen can be roughly estimated through the calorific values ​​of coal powder and organic waste liquid. Then, by judging and supplementing oxygen for the air entering the combustion stage, the oxygen content of the oxygen-enriched air can be effectively controlled, thereby achieving precise control of the oxygen content in the organic waste liquid treatment stage. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0017] Figure 1 A schematic diagram of a flow chart of a method provided by an embodiment of the present invention; Figure 2 A detailed flowchart of the method provided by the embodiment of the present invention; Figure 3A schematic diagram of the logical structure of a system provided by an embodiment of the present invention; Figure 4 A schematic diagram of the physical structure of a system provided by an embodiment of the present invention; Description of reference numerals: 1-waste liquid storage unit, 2-waste liquid concentration unit, 3-stirring and mixing unit, 31-coal powder feeding section, 32-pulping section, 4-combustion unit, 41-combustion furnace, 42-atomizer, 5-air inlet unit, 51-blower, 52-heat exchanger, 53-N section ventilation duct, 531-first ventilation duct, 532-second ventilation duct, 533-third ventilation duct, 6-oxygen injection unit, 61-oxygen injection section, 611-oxygen tank, 612-oxygen injection valve, 62-pipeline valve group, 621-first pipeline valve, 622-second pipeline valve, 623-third pipeline valve, 63-oxygen content sensor group, 631-first oxygen content sensor, 632-second oxygen content sensor, 633-third oxygen content sensor, 7-control unit, 8-exhaust gas treatment unit. DETAILED DESCRIPTION

[0018] In the following, only some exemplary embodiments are briefly described. As those skilled in the art will appreciate, the described embodiments may be modified in various ways without departing from the spirit or scope of the present invention. Therefore, the drawings and descriptions are considered to be exemplary and non-restrictive in nature.

[0019] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0020] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0021] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection, an electrical connection, or a communication; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0022] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may include that the first and second features are in direct contact, or may include that the first and second features are not in direct contact but are in contact through another feature between them. Moreover, a first feature being "above", "above" and "above" a second feature includes that the first feature is directly above and obliquely above the second feature, or simply indicates that the first feature is higher in level than the second feature. A first feature being "below", "below" and "below" a second feature includes that the first feature is directly above and obliquely above the second feature, or simply indicates that the first feature is lower in level than the second feature.

[0023] It should also be understood that the terms used in the present specification are only for the purpose of describing specific embodiments and are not intended to limit the present invention. As used in the present specification and the appended claims, unless the context clearly indicates otherwise, the singular forms "a", "an" and "the" are intended to include plural forms.

[0024] It should be further understood that the term "and / or" used in the present description and the appended claims refers to any and all possible combinations of one or more of the associated listed items, and includes these combinations.

[0025] Various structural schematic diagrams of the embodiments disclosed in the present invention are shown in the accompanying drawings. These figures are not drawn to scale, and some details are magnified and some details may be omitted for the purpose of clear expression. The shapes of various regions and layers shown in the figures and the relative sizes and positional relationships therebetween are only exemplary, and may deviate in practice due to manufacturing tolerances or technical limitations, and those skilled in the art may additionally design regions / layers with different shapes, sizes, and relative positions according to actual needs.

[0026] The embodiments of the present invention are described in detail below with reference to the accompanying drawings.

[0027] In one embodiment of the present invention, Figure 1 As shown, a method for controlling oxygen-enriched combustion of organic waste liquid with high water content is provided, the method comprising: S1. Obtaining organic waste liquid with high water content; S2. The high-content organic waste liquid is concentrated to obtain a concentrated liquid containing concentrated organic waste liquid; S3. The pulverized coal is added to the concentrate and stirred to obtain a mixed slurry containing water, coal and waste liquid; S4. atomizing the mixed slurry to obtain an atomized liquid; S5. Obtain oxygen-enriched air and the oxygen concentration of oxygen-enriched air; S6. According to the oxygen concentration of the oxygen-enriched air, determining whether the oxygen content in the oxygen-enriched air is appropriate; If yes, the oxygen content in the oxygen-enriched air is appropriate, and the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; Wherein, N≥3 and N is an integer.

[0028] In some optional embodiments, such as Figure 2 As shown, judging whether the oxygen content in the oxygen-enriched air is appropriate according to the oxygen concentration of the oxygen-enriched air specifically includes: S61. Obtaining a standard oxygen concentration according to the total weight of the pulverized coal and the organic waste liquid in the atomized liquid; S62. Determine whether the oxygen content in the oxygen-enriched air is appropriate based on the oxygen concentration and the standard oxygen concentration; If the oxygen concentration is greater than or equal to the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is appropriate, and the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; If the oxygen concentration is ≥ the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is inappropriate, and oxygen is added before making another judgment; Wherein, N≥3 and N is an integer.

[0029] In the present invention, the total weight of the coal powder and the organic waste liquid in the atomized liquid can be used to roughly estimate the oxygen content required for complete combustion, and then the standard oxygen concentration can be derived, which facilitates the control of the oxygen content in the air, thereby achieving the purpose of accurately controlling the oxygen content.

[0030] In some optional embodiments, the standard oxygen concentration is 24% to 35%; The air coefficient of the oxygen-enriched air is 1.05-1.25.

[0031] In the present invention, the positive effect of the standard oxygen concentration of 24% to 35% is that within this concentration range, the atomized liquid can be guaranteed to be completely burned, thereby ensuring that the oxygen is completely consumed; when the concentration value is greater than the maximum value of the endpoint of the range, the adverse effect that will result is that the excessively large oxygen volume concentration will cause insufficient oxygen consumption during the combustion stage, thereby failing to effectively control the oxygen content; when the concentration value is less than the minimum value of the endpoint of the range, the adverse effect that will result is that too low a concentration will cause the concentrated liquid containing concentrated organic waste liquid to be unable to be fully burned, thereby resulting in incomplete oxygen consumption, affecting the control of the oxygen content.

[0032] The positive effect of the air coefficient of oxygen-enriched air being 1.05~1.25 is that under the condition of this air coefficient, the concentrated liquid containing concentrated organic waste liquid can be fully burned, thereby ensuring that the oxygen is fully consumed; when the air coefficient is greater than the maximum value at the endpoint of the range, the adverse effect will be that the too high air coefficient indicates that too much air is introduced, which will lead to too low oxygen content in the air, resulting in incomplete combustion, excessive oxygen consumption, and thus a large amount of heat loss; when the air coefficient is less than the minimum value at the endpoint of the range, the adverse effect will be that the too low air coefficient indicates that insufficient air is introduced, resulting in excessive oxygen content in the air, and a large amount of oxygen remains after combustion, which makes it impossible to effectively control the oxygen content during the treatment of organic waste liquid.

[0033] In some optional embodiments, the oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount, and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 45% to 55% of the total amount of oxygen flow, the second oxygen flow rate accounts for 35% to 45% of the total amount of oxygen flow, and the third oxygen flow rate accounts for 5% to 15% of the total amount of oxygen flow.

[0034] In the present invention, the positive effect of the first oxygen flow rate accounting for 45% to 55% of the total input amount is that within the range of this proportion, it can ensure that the mixed slurry including the water-coal-waste liquid complex is initially burned under suitable oxygen content conditions, and the oxygen is fully consumed; when the proportion is greater than the maximum value of the endpoint of the range, the adverse effect will be that too much first oxygen flow will cause the mixed slurry to burn too fully, affecting the combustion process and insufficient oxygen consumption; when the proportion is less than the minimum value of the endpoint of the range, the adverse effect will be that too low a first oxygen flow rate will not be able to promote the initial combustion of the mixed slurry, affecting oxygen consumption.

[0035] The positive effect of the second oxygen flow rate being 35% to 45% of the total input amount is that within the range of this proportion, it can ensure that the mixed slurry including the water-coal-waste liquid complex can further burn on the basis of preliminary combustion, and facilitate the sufficient consumption of oxygen in the further combustion; when the proportion is greater than the maximum value of the endpoint of this range, the adverse effect will be that too much second oxygen flow will cause the mixed slurry to burn too fully, affecting the progress of combustion and insufficient oxygen consumption; when the proportion is less than the minimum value of the endpoint of this range, the adverse effect will be that too low a second oxygen flow rate will not promote further combustion of the mixed slurry, affecting oxygen consumption.

[0036] The positive effect of the third oxygen flow rate being 5% to 15% of the total input amount is that within the range of this proportion, it can ensure that the mixed slurry including the water-coal-waste liquid complex is fully burned and promotes sufficient consumption of oxygen; when the proportion is greater than the maximum value of the endpoint of this range, the adverse effect will be that too much third oxygen flow will cause the temperature of the mixed slurry to be too low, and at the same time, too much third oxygen flow will take away part of the heat, affecting the combustion and insufficient oxygen consumption; when the proportion is less than the minimum value of the endpoint of this range, the adverse effect will be that too low a third oxygen flow rate will fail to promote sufficient combustion of the mixed slurry, affecting oxygen consumption.

[0037] In some optional embodiments, the ratio of the heat input power of the concentrated liquid to the heat input power of the coal powder is 1:2-5; And / or, the ratio of the flow rate of the concentrated liquid to the flow rate of the coal powder is 2-10:1.

[0038] In the present invention, the positive effect of the ratio of the heat input power of the concentrated liquid containing concentrated organic waste liquid to the heat input power of the coal powder being 1:2~5 is that within this ratio range, it can be ensured that the organic waste liquid and the coal powder can be fully burned under oxygen-rich conditions, thereby ensuring that the organic waste liquid is fully burned and the oxygen is completely consumed, thereby achieving precise control of the oxygen content; when the ratio is greater than or less than the endpoint value of the range, the adverse effect that will result is that the coal powder and the organic waste liquid cannot be fully burned, resulting in a large amount of oxygen remaining, and precise control of the oxygen content cannot be achieved.

[0039] The positive effect of the ratio of the flow rate of the concentrated liquid containing concentrated organic waste liquid to the flow rate of coal powder being 2~10:1 is that within this ratio range, the organic waste liquid and coal powder can be fully mixed, while ensuring the subsequent sufficient combustion and sufficient consumption of oxygen; when the ratio is greater than or less than the endpoint value of this range, the adverse effect that will result is the inability to fully mix the organic waste liquid and coal powder, resulting in incomplete combustion and affecting the consumption of oxygen.

[0040] In some optional embodiments, the moisture content of the high-water content organic waste liquid is greater than 70%, and the moisture content of the concentrated liquid is 10% to 20%.

[0041] In the present invention, the positive effect of the moisture content of the concentrated organic waste liquid being 10% to 20% is to ensure that the moisture content in the concentrated liquid containing the concentrated organic waste liquid is within a suitable range, thereby ensuring that the organic waste liquid can be burned and promoting the full consumption of oxygen; when the moisture content is greater than the maximum value of the endpoint of the range, the adverse effect that will result is that too much moisture will cause the organic waste liquid to be unable to be fully burned, affecting the consumption of oxygen; when the moisture content is less than the minimum value of the endpoint of the range, the adverse effect that will result is that too low moisture will cause the heat after the organic waste liquid is burned to be unable to be converted, thereby requiring further consumption of oxygen and being unable to accurately control the oxygen consumption.

[0042] In one embodiment of the present invention, Figure 3 and Figure 4 As shown, an oxygen-enriched combustion control system for organic waste liquid with high water content is provided, the system is applicable to the method, and the system comprises: A waste liquid storage unit 1, used for storing organic waste liquid with high water content; A waste liquid concentration unit 2, wherein the liquid outlet of the waste liquid storage unit 1 is connected to the liquid inlet of the waste liquid concentration unit 2, and is used to convert the organic waste liquid with high water content into a concentrated liquid containing concentrated organic waste liquid; A stirring and mixing unit 3, wherein the liquid outlet of the waste liquid concentration unit 2 is connected to the liquid inlet of the stirring and mixing unit 3, so as to fully mix the coal powder and the concentrated liquid; the stirring and mixing unit 3 comprises a coal powder feeding section 31 and a pulping section 32, wherein the pulping section 32 comprises a first feeding section and a second feeding section, the discharge port of the waste liquid concentration unit 2 is connected to the first feeding port of the pulping section 32, and the discharge port of the coal powder feeding section 31 is connected to the second feeding port of the pulping section 32; A combustion unit 4, wherein the feed port of the combustion unit 4 is connected to the discharge port of the pulping section 32, the combustion unit 4 comprises a combustion furnace 41 and an atomizer 42, the feed port of the atomizer 42 is connected to the discharge port of the pulping section 32, the atomizer 42 is arranged in the combustion furnace 41, and is used to atomize and burn the mixed slurry; An air inlet unit 5, wherein the air outlet of the air inlet unit 5 is connected to the air inlet of the combustion unit 4, and is used to provide the combustion unit 4 with air required for combustion; the air inlet unit 5 comprises a blower 51, a heat exchanger 52 and N sections of ventilation ducts 53, wherein the heat exchanger 52 comprises a first air inlet and a second air inlet, the air outlet of the blower 51 is connected to the first air inlet of the heat exchanger 52, the air outlet of the combustion furnace 41 is connected to the second air inlet of the heat exchanger 52, the air outlet of the heat exchanger 52 is connected to the air inlet of the N sections of ventilation ducts 53, and the air outlet of the N sections of ventilation ducts 53 is connected to the air inlet of the combustion furnace 41, wherein N≥3 and N is an integer; An oxygen injection unit 6, the oxygen injection unit 6 comprises an oxygen injection portion 61, a pipeline valve group 62 and an oxygen content sensor group 63, the oxygen content sensor group 63 is respectively arranged in the oxygen injection portion 61 and in the pipeline valve group 62, the air inlet of the oxygen injection portion 61 is connected to the air outlet of the heat exchanger 52 through the pipeline valve group 62, and the air outlet of the oxygen injection portion 61 is connected to the air inlet of the N-section ventilation duct 53 through the pipeline valve group 62; The control unit 7 is connected to the pipeline valve group 62 and the oxygen content sensor group 63 respectively through electrical signals, and is used to control the oxygen content of the air entering the combustion furnace 41, wherein the control unit 7 can be a controller, and the controller is a KM-XF-12 touch controller.

[0043] In some optional embodiments, the N-segment ventilation duct 53 includes a first ventilation duct 531, a second ventilation duct 532 and a third ventilation duct 533, and the air inlets of the first ventilation duct 531, the second ventilation duct 532 and the third ventilation duct 533 are all connected to the air outlet of the oxygen injection part 61, and the air outlets of the first ventilation duct 531, the second ventilation duct 532 and the third ventilation duct 533 are all connected to the air inlet of the combustion furnace 41.

[0044] In the present invention, N sections of ventilation ducts 53 including a first ventilation duct 531, a second ventilation duct 532 and a third ventilation duct 533 are used to control different ventilation ducts to achieve different degrees of combustion of organic waste liquid. For example, when the atomized liquid enters the combustion furnace 41, the first ventilation duct 531 is opened to allow oxygen-rich air to enter, which can not only make the atomized liquid diffuse quickly, but also burn the atomized liquid to achieve preliminary combustion of the organic waste liquid. Then the second ventilation duct 532 is opened, and the first ventilation duct 531 can be closed or kept open according to actual conditions, so that the mixed slurry can be further burned after preliminary combustion, and then the third ventilation duct 533 is opened, and the first ventilation duct 531 and the second ventilation duct 532 can be closed or kept open according to actual conditions, so that the organic waste liquid can be completely burned, and different degrees of oxygen consumption can be achieved by using ventilation ducts of different sections.

[0045] In some optional embodiments, the oxygen injection part 61 includes an oxygen tank 611 and an oxygen injection valve 612, the oxygen injection valve 612 is provided with a first air inlet and a second air inlet, the first air inlet of the oxygen injection valve 612 is connected to the air outlet of the heat exchanger 52, the second air inlet of the oxygen injection valve 612 is connected to the air outlet of the oxygen tank 611, and the air outlet of the oxygen injection valve 612 is connected to the air inlet of the combustion furnace 41; The pipeline valve group 62 includes a first pipeline valve 621, a second pipeline valve 622 and a third pipeline valve 623, and the oxygen content sensor group 63 includes a first oxygen content sensor 631, a second oxygen content sensor 632 and a third oxygen content sensor 633; The first oxygen content sensor 631 and the first pipeline valve 621 are both arranged in the gas outlet of the oxygen tank 611, and the first oxygen content sensor 631 is arranged upstream of the first pipeline valve 621 along the oxygen delivery direction; The second oxygen content sensor 632 and the second pipeline valve 622 are arranged in the second air inlet of the oxygen injection valve 612, and the second oxygen content sensor 632 is arranged upstream of the second pipeline valve 622 along the air delivery direction; The third oxygen content sensor 633 and the third pipeline valve 623 are arranged in the air outlet of the oxygen injection valve 612, and the third oxygen content sensor 633 is arranged downstream of the third pipeline valve 623 along the oxygen-enriched air delivery direction; Among them, the first oxygen content sensor 631, the second oxygen content sensor 632 and the third oxygen content sensor 633 all use S4OXV type oxygen sensors, and the first pipeline valve 621, the second pipeline valve 622 and the third pipeline valve 623 all use Z941H-40 type electric valves.

[0046] In the present invention, by adopting the oxygen injection part 61 including the oxygen tank 611 and the oxygen injection valve 612, and then by using the pipeline valve group 62 including the first pipeline valve 621, the second pipeline valve 622 and the third pipeline valve 623 and the oxygen content sensor group 63 including the first oxygen content sensor 631, the second oxygen content sensor 632 and the third oxygen content sensor 633, by using the one-to-one corresponding setting relationship between the oxygen content sensor group 63 and the pipeline valve group 62, the oxygen content data in the oxygen tank 611, the oxygen content of the air before entering the oxygen injection and the oxygen content of the oxygen-enriched air before entering the combustion furnace 41 are respectively collected by the oxygen content sensor group 63, and then the pipeline valve group 62 is used to control the flow rate of the pipeline air, so that the oxygen content data can be analyzed in real time by the oxygen content sensor group 63, and then the mixing degree of air and oxygen is controlled by the pipeline valve group 62, so that the oxygen content in the air before entering the combustion furnace 41 can be accurately controlled.

[0047] In some optional embodiments, the system also includes an exhaust gas treatment unit 8, the heat exchanger 52 includes a first air outlet and a second air outlet, the first air outlet of the heat exchanger 52 is connected to the air inlet of the N-section ventilation duct 53, and the second air outlet of the heat exchanger 52 is connected to the exhaust gas treatment unit 8.

[0048] In the present invention, by adopting the tail gas treatment unit 8, the waste gas after the combustion of the organic waste liquid is discharged through the waste gas treatment unit, thereby ensuring that water vapor or combustion waste gas is discharged through the tail gas treatment unit 8, achieving energy saving and environmental protection.

[0049] Example 1 like Figure 1 and Figure 2 As shown, a method for controlling oxygen-enriched combustion of organic waste liquid with high water content comprises: S1. Obtaining organic waste liquid with high water content; S2. The high-content organic waste liquid is concentrated to obtain a concentrated liquid containing concentrated organic waste liquid; S3. The pulverized coal is added to the concentrate and stirred to obtain a mixed slurry containing water, coal and waste liquid; S4. atomizing the mixed slurry to obtain an atomized liquid; S5. Obtain oxygen-enriched air and the oxygen concentration of oxygen-enriched air; S61. Obtaining a standard oxygen concentration according to the total weight of pulverized coal and organic waste liquid in the atomized liquid; S62. Determine whether the oxygen content in the oxygen-enriched air is appropriate based on the oxygen concentration and the standard oxygen concentration; If the oxygen concentration is ≥ the standard oxygen concentration, the oxygen content in the oxygen-enriched air is determined to be appropriate, and the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; If the oxygen concentration is ≥ the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is inappropriate, and oxygen is added before making another judgment; Wherein, N≥3 and N is an integer.

[0050] The standard oxygen concentration is 30%; The air factor of oxygen-enriched air is 1.1.

[0051] The oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount, and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 50% of the total oxygen flow rate, the second oxygen flow rate accounts for 40% of the total oxygen flow rate, and the third oxygen flow rate accounts for 10% of the total oxygen flow rate.

[0052] The ratio of heat input power of concentrate to that of pulverized coal is 1:3; The ratio of the flow rate of the concentrate to the flow rate of the pulverized coal is 6:1.

[0053] The moisture content of high-water content organic waste liquid is greater than 70%, and the moisture content of the concentrate is 15%.

[0054] like Figure 3 and Figure 4 As shown, an oxygen-enriched combustion control system for organic waste liquid with high water content, the system is applicable to the method of the first aspect, comprising: A waste liquid storage unit 1, used for storing organic waste liquid with high water content; The waste liquid concentration unit 2, the liquid outlet of the waste liquid storage unit 1 is connected to the liquid inlet of the waste liquid concentration unit 2, and is used to convert the organic waste liquid with high water content into a concentrated liquid containing concentrated organic waste liquid; The stirring and mixing unit 3, the liquid outlet of the waste liquid concentration unit 2 is connected to the liquid inlet of the stirring and mixing unit 3, so as to fully mix the coal powder and the concentrated liquid; the stirring and mixing unit 3 includes a coal powder feeding part 31 and a pulping part 32, the pulping part 32 includes a first feeding part and a second feeding part, the discharge port of the waste liquid concentration unit 2 is connected to the first feeding port of the pulping part 32, and the discharge port of the coal powder feeding part 31 is connected to the second feeding port of the pulping part 32; A combustion unit 4, wherein the feed port of the combustion unit 4 is connected to the discharge port of the pulping section 32, the combustion unit 4 comprises a combustion furnace 41 and an atomizer 42, the feed port of the atomizer 42 is connected to the discharge port of the pulping section 32, and the atomizer 42 is disposed in the combustion furnace 41 for atomizing and burning the mixed slurry; The air inlet unit 5, the air outlet of the air inlet unit 5 is connected to the air inlet of the combustion unit 4, and is used to provide the air required for the combustion unit 4 to perform combustion; the air inlet unit 5 includes a blower 51, a heat exchanger 52 and N sections of ventilation ducts 53, the heat exchanger 52 includes a first air inlet and a second air inlet, the air outlet of the blower 51 is connected to the first air inlet of the heat exchanger 52, the air outlet of the combustion furnace 41 is connected to the second air inlet of the heat exchanger 52, the air outlet of the heat exchanger 52 is connected to the air inlet of the N sections of ventilation ducts 53, and the air outlet of the N sections of ventilation ducts 53 is connected to the air inlet of the combustion furnace 41, wherein N≥3 and N is an integer; The oxygen injection unit 6 includes an oxygen injection portion 61, a pipeline valve group 62 and an oxygen content sensor group 63. The oxygen content sensor group 63 is respectively arranged in the oxygen injection portion 61 and the pipeline valve group 62. The air inlet of the oxygen injection portion 61 is connected to the air outlet of the heat exchanger 52 through the pipeline valve group 62. The air outlet of the oxygen injection portion 61 is connected to the air inlet of the N-section ventilation duct 53 through the pipeline valve group 62. The control unit 7 is connected to the pipeline valve group 62 and the oxygen content sensor group 63 through electrical signals, so as to control the oxygen content of the air entering the combustion furnace 41.

[0055] The N-section ventilation duct 53 includes a first ventilation duct 531, a second ventilation duct 532 and a third ventilation duct 533. The air inlets of the first ventilation duct 531, the second ventilation duct 532 and the third ventilation duct 533 are all connected to the air outlet of the oxygen injection part 61, and the air outlets of the first ventilation duct 531, the second ventilation duct 532 and the third ventilation duct 533 are all connected to the air inlet of the combustion furnace 41.

[0056] The oxygen injection part 61 includes an oxygen tank 611 and an oxygen injection valve 612. The oxygen injection valve 612 is provided with a first air inlet and a second air inlet. The first air inlet of the oxygen injection valve 612 is connected to the air outlet of the heat exchanger 52. The second air inlet of the oxygen injection valve 612 is connected to the air outlet of the oxygen tank 611. The air outlet of the oxygen injection valve 612 is connected to the air inlet of the combustion furnace 41. The pipeline valve group 62 includes a first pipeline valve 621, a second pipeline valve 622 and a third pipeline valve 623, and the oxygen content sensor group 63 includes a first oxygen content sensor 631, a second oxygen content sensor 632 and a third oxygen content sensor 633; The first oxygen content sensor 631 and the first pipeline valve 621 are both arranged in the gas outlet of the oxygen tank 611, and the first oxygen content sensor 631 is arranged upstream of the first pipeline valve 621 along the oxygen delivery direction; The second oxygen content sensor 632 and the second pipeline valve 622 are arranged in the second air inlet of the oxygen injection valve 612, and the second oxygen content sensor 632 is arranged upstream of the second pipeline valve 622 along the air delivery direction; The third oxygen content sensor 633 and the third pipeline valve 623 are arranged in the air outlet of the oxygen injection valve 612, and the third oxygen content sensor 633 is arranged downstream of the third pipeline valve 623 along the oxygen-enriched air delivery direction.

[0057] The system also includes an exhaust gas treatment unit 8 , and the heat exchanger 52 includes a first air outlet and a second air outlet. The first air outlet of the heat exchanger 52 is connected to the air inlet of the N-section ventilation duct 53 , and the second air outlet of the heat exchanger 52 is connected to the exhaust gas treatment unit 8 .

[0058] Example 2 Comparing Example 2 with Example 1, the difference between Example 2 and Example 1 is: The standard oxygen concentration is 24%; The air coefficient of oxygen-enriched air is 1.05.

[0059] The oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount, and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 45% of the total oxygen flow rate, the second oxygen flow rate accounts for 40% of the total oxygen flow rate, and the third oxygen flow rate accounts for 15% of the total oxygen flow rate.

[0060] The ratio of heat input power of concentrate to that of pulverized coal is 1:5; The ratio of the flow rate of the concentrate to the flow rate of the pulverized coal is 2:1.

[0061] The moisture content of the concentrate is 10%.

[0062] Example 3 Comparing Example 3 with Example 1, the difference between Example 3 and Example 1 is: The standard oxygen concentration is 35%; The air factor of oxygen-enriched air is 1.25.

[0063] The oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount, and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 55% of the total oxygen flow rate, the second oxygen flow rate accounts for 40% of the total oxygen flow rate, and the third oxygen flow rate accounts for 5% of the total oxygen flow rate.

[0064] The ratio of heat input power of the concentrate to that of the pulverized coal is 1:2; The ratio of the flow rate of the concentrate to the flow rate of the pulverized coal is 10:1.

[0065] The moisture content of the concentrate is 20%.

[0066] Comparative Example 1 Comparing Comparative Example 1 with Example 1, the difference between Comparative Example 1 and Example 1 is: The pipeline valve group 62 and the sensor group are not used.

[0067] Comparative Example 2 Comparing Comparative Example 2 with Example 1, the difference between Comparative Example 2 and Example 1 is: The standard oxygen concentration is 23%; The air factor of oxygen-enriched air is 1.

[0068] In terms of mass fraction, the first oxygen flow rate accounts for 45% of the total oxygen flow rate, the second oxygen flow rate accounts for 35% of the total oxygen flow rate, and the third oxygen flow rate accounts for 20% of the total oxygen flow rate.

[0069] The ratio of heat input power of concentrate to that of pulverized coal is 1:8; The ratio of the flow rate of the concentrate to the flow rate of the pulverized coal is 1:1.

[0070] The moisture content of the concentrate is 5%.

[0071] Comparative Example 3 Comparing Comparative Example 3 with Example 1, the difference between Comparative Example 3 and Example 1 is: The standard oxygen concentration is 40%; The air factor of oxygen-enriched air is 1.5.

[0072] In terms of mass fraction, the first oxygen flow rate accounts for 63% of the total oxygen flow rate, the second oxygen flow rate accounts for 35% of the total oxygen flow rate, and the third oxygen flow rate accounts for 2% of the total oxygen flow rate.

[0073] The ratio of heat input power of the concentrate to that of the pulverized coal is 1:1; The ratio of the flow rate of the concentrate to the flow rate of the pulverized coal is 11:1.

[0074] The moisture content of the concentrate is 25%.

[0075] Related experiments: The oxygen concentration in the tail gas during the operation phase of the methods and systems of Examples 1-3 and Comparative Examples 1-3 was counted respectively, and the oxygen utilization rate was calculated. The results are shown in Table 1.

[0076] Determination methods of related experiments: Oxygen utilization rate: According to the concentration of oxygen in the exhaust gas and the data of the oxygen content sensor group 63, the oxygen content of the air entering the combustion furnace 41 is obtained, and the oxygen utilization rate is calculated as: oxygen utilization rate = (oxygen content of the air entering the combustion furnace 41 - oxygen concentration in the exhaust gas) / oxygen content of the air entering the combustion furnace 41.

[0077] Table 1

[0078] The detailed analysis of Table 1 is as follows: Oxygen utilization rate refers to the utilization degree of oxygen introduced into the system during the combustion stage, and also reflects the degree of control of the system over the oxygen content. The higher the oxygen utilization rate, the higher the degree of oxygen utilization by the system, and the better the degree of control of the system over the oxygen content.

[0079] From the data of Examples 1-3, it can be seen that: If the method and system provided by the present invention are adopted, the oxygen injection stage of the air is controlled in the oxygen injection unit 6, so that the oxygen content of the oxygen-enriched air entering the combustion furnace 41 can be effectively controlled, thereby fully controlling the combustion and achieving precise control of the oxygen content.

[0080] From the data of Comparative Examples 1-3, it can be seen that: If the oxygen content of the oxygen-enriched air entering the combustion furnace 41 is not controlled or the process conditions provided by the present invention are not adopted, the oxygen utilization rate will be low.

[0081] One or more technical solutions in the embodiments of the present invention have at least the following technical effects or advantages: (1) The method provided in the embodiment of the present invention first concentrates the organic waste liquid and then adds coal powder to the concentrated organic waste liquid to form a mixed slurry containing water, coal and waste liquid, thereby introducing coal powder as a combustion aid. Since the calorific value of coal powder and the oxygen value required for combustion are both easy to measure, the amount of oxygen required can be roughly estimated based on the calorific value of coal powder and organic waste liquid. Then, by judging and supplementing the air entering the combustion stage, the oxygen content of the oxygen-enriched air can be effectively controlled, thereby achieving precise control of the oxygen content in the organic waste liquid treatment stage.

[0082] (2) The method provided in the embodiment of the present invention uses coal powder as an auxiliary fuel. Since most of the coal powder in my country is low-quality coal or surface coal, converting it into coal powder can increase the effective utilization of low-quality coal or surface coal.

[0083] (3) The system provided in the embodiment of the present invention can effectively provide and regulate oxygen-enriched air during the combustion of organic waste liquid by adopting N-section ventilation ducts 53 including a first ventilation duct 531, a second ventilation duct 532 and a third ventilation duct 533, thereby controlling the oxygen content in the combustion stage in stages to ensure sufficient combustion of the organic waste liquid.

[0084] (4) The system provided in the embodiment of the present invention controls the heat of the air entering the combustion furnace 41 through the heat exchanger 52, which can further improve the degree of heat recovery and utilization and save production costs.

[0085] The above shows and describes the basic principles and main features of the present invention and the advantages of the present invention. It is obvious to those skilled in the art that the present invention is not limited to the details of the above exemplary embodiments, and the present invention can be implemented in other specific forms without departing from the spirit or basic features of the present invention. Therefore, no matter from which point of view, the embodiments should be regarded as exemplary and non-restrictive. The scope of the present invention is defined by the attached claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims are included in the present invention. Any figure mark in the claims should not be regarded as limiting the claims involved.

[0086] In addition, it should be understood that although this specification is described in accordance with the implementation modes, not every implementation mode contains only one independent technical solution. This description of the specification is only for the sake of clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment can also be appropriately combined to form other implementation modes that can be understood by those skilled in the art. The above content is only to illustrate the technical idea of ​​the present invention, and cannot be used to limit the protection scope of the present invention. Any changes made on the basis of the technical solution according to the technical idea proposed by the present invention shall fall within the protection scope of the claims of the present invention.

Claims

1. A method for controlling oxygen-enriched combustion of organic waste liquid with high water content, characterized in that: The method comprises: Obtaining organic waste liquid with high water content; Concentrating the high-content organic waste liquid to obtain a concentrated liquid containing concentrated organic waste liquid; adding coal powder into the concentrated liquid and stirring to obtain a mixed slurry containing water, coal and waste liquid; Atomizing the mixed slurry to obtain an atomized liquid; Obtaining oxygen-enriched air and the oxygen concentration of the oxygen-enriched air; According to the oxygen concentration of the oxygen-enriched air, judging whether the oxygen content in the oxygen-enriched air is appropriate; If yes, the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; wherein N≥3 and N is an integer.

2. The method according to claim 1, characterized in that The determining, based on the oxygen concentration of the oxygen-enriched air, whether the oxygen content in the oxygen-enriched air is appropriate specifically includes: Obtaining a standard oxygen concentration according to the total weight of the pulverized coal and the organic waste liquid in the atomized liquid; According to the oxygen concentration and the standard oxygen concentration, judging whether the oxygen content in the oxygen-enriched air is appropriate; If the oxygen concentration is greater than or equal to the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is appropriate, and the oxygen-enriched air is introduced into the atomized liquid N times, and then burned to obtain a completely burned organic waste liquid; If the oxygen concentration is ≥ the standard oxygen concentration, it is determined that the oxygen content in the oxygen-enriched air is inappropriate, and oxygen is added before making another judgment; Wherein, N≥3 and N is an integer.

3. The method according to claim 2, characterized in that The standard oxygen concentration is 24% to 35%; The air coefficient of the oxygen-enriched air is 1.05-1.

25.

4. The method according to claim 1, characterized in that The oxygen-enriched air is introduced three times, and the total amount of oxygen-enriched air introduced includes a first oxygen supply amount, a second oxygen supply amount, and a third oxygen supply amount; In terms of mass fraction, the first oxygen flow rate accounts for 45% to 55% of the total amount of oxygen flow, the second oxygen flow rate accounts for 35% to 45% of the total amount of oxygen flow, and the third oxygen flow rate accounts for 5% to 15% of the total amount of oxygen flow.

5. The method according to claim 1, characterized in that The ratio of the heat input power of the concentrated liquid to the heat input power of the coal powder is 1:2-5; And / or, the ratio of the flow rate of the concentrated liquid to the flow rate of the coal powder is 2-10:

1.

6. The method according to claim 1, characterized in that The moisture content of the high-water content organic waste liquid is greater than 70%, and the moisture content of the concentrated liquid is 10% to 20%.

7. An oxygen-enriched combustion control system for organic waste liquid with high water content, characterized in that: The system is applicable to the method according to any one of claims 1 to 6, and the system comprises: A waste liquid storage unit (1), used for storing organic waste liquid with high water content; A waste liquid concentration unit (2), wherein the liquid outlet of the waste liquid storage unit (1) is connected to the liquid inlet of the waste liquid concentration unit (2), and is used to convert the organic waste liquid with high water content into a concentrated liquid containing concentrated organic waste liquid; A stirring and mixing unit (3), wherein the liquid outlet of the waste liquid concentration unit (2) is connected to the liquid inlet of the stirring and mixing unit (3), and is used to fully mix the coal powder and the concentrated liquid; the stirring and mixing unit (3) comprises a coal powder feeding section (31) and a pulping section (32), the pulping section (32) comprises a first feeding section and a second feeding section, the discharge port of the waste liquid concentration unit (2) is connected to the first feeding section of the pulping section (32), and the discharge port of the coal powder feeding section (31) is connected to the second feeding section of the pulping section (32); A combustion unit (4), wherein the feed port of the combustion unit (4) is connected to the discharge port of the pulping section (32), the combustion unit (4) comprises a combustion furnace (41) and an atomizer (42), the feed port of the atomizer (42) is connected to the discharge port of the pulping section (32), and the atomizer (42) is arranged in the combustion furnace (41) and is used to atomize and burn the mixed slurry; An air inlet unit (5), wherein an air outlet of the air inlet unit (5) is connected to an air inlet of the combustion unit (4), and is used to provide the combustion unit (4) with air required for combustion; the air inlet unit (5) comprises a blower (51), a heat exchanger (52), and N sections of ventilation ducts (53); the heat exchanger (52) comprises a first air inlet and a second air inlet; the air outlet of the blower (51) is connected to the first air inlet of the heat exchanger (52); the air outlet of the combustion furnace (41) is connected to the second air inlet of the heat exchanger (52); the air outlet of the heat exchanger (52) is connected to the air inlet of the N sections of ventilation ducts (53); and the air outlet of the N sections of ventilation ducts (53) is connected to the air inlet of the combustion furnace (41), wherein N ≥ 3 and N is an integer; an oxygen injection unit (6), the oxygen injection unit (6) comprising an oxygen injection portion (61), a pipeline valve group (62) and an oxygen content sensor group (63), the oxygen content sensor group (63) being arranged in the oxygen injection portion (61) and in the pipeline valve group (62), respectively; an air inlet of the oxygen injection portion (61) being connected to an air outlet of the heat exchanger (52) via the pipeline valve group (62), and an air outlet of the oxygen injection portion (61) being connected to an air inlet of the N-section ventilation pipeline (53) via the pipeline valve group (62); A control unit (7), the control unit (7) being connected to the pipeline valve group (62) and the oxygen content sensor group (63) respectively through electrical signals, and being used to control the oxygen content of the air entering the combustion furnace (41).

8. The system according to claim 7, characterized in that The N-section ventilation duct (53) comprises a first ventilation duct (531), a second ventilation duct (532) and a third ventilation duct (533); the air inlets of the first ventilation duct (531), the second ventilation duct (532) and the third ventilation duct (533) are all connected to the air outlet of the oxygen injection section (61); and the air outlets of the first ventilation duct (531), the second ventilation duct (532) and the third ventilation duct (533) are all connected to the air inlet of the combustion furnace (41).

9. The system according to claim 7, characterized in that The oxygen injection part (61) comprises an oxygen tank (611) and an oxygen injection valve (612), the oxygen injection valve (612) being provided with a first air inlet and a second air inlet, the first air inlet of the oxygen injection valve (612) being connected to the air outlet of the heat exchanger (52), the second air inlet of the oxygen injection valve (612) being connected to the air outlet of the oxygen tank (611), and the air outlet of the oxygen injection valve (612) being connected to the air inlet of the combustion furnace (41); The pipeline valve group (62) comprises a first pipeline valve (621), a second pipeline valve (622) and a third pipeline valve (623); the oxygen content sensor group (63) comprises a first oxygen content sensor (631), a second oxygen content sensor (632) and a third oxygen content sensor (633); The first oxygen content sensor (631) and the first pipeline valve (621) are both arranged in the gas outlet of the oxygen tank (611), and the first oxygen content sensor (631) is arranged upstream of the first pipeline valve (621) along the oxygen delivery direction; The second oxygen content sensor (632) and the second pipeline valve (622) are arranged in the second air inlet of the oxygen injection valve (612), and the second oxygen content sensor (632) is arranged upstream of the second pipeline valve (622) along the air delivery direction; The third oxygen content sensor (633) and the third pipeline valve (623) are arranged in the air outlet of the oxygen injection valve (612), and the third oxygen content sensor (633) is arranged downstream of the third pipeline valve (623) along the oxygen-enriched air delivery direction.

10. The system according to claim 7, characterized in that The system further comprises an exhaust gas treatment unit (8), the heat exchanger (52) comprising a first air outlet and a second air outlet, the first air outlet of the heat exchanger (52) being connected to an air inlet of the N-section ventilation duct (53), and the second air outlet of the heat exchanger (52) being connected to the exhaust gas treatment unit (8).

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