A cyclone dust removal dry quenching boiler system based on full-fin tube evaporator

Abstract

The utility model embodiment provides a kind of based on full finned tube evaporator's cyclone dust collection dry quenching boiler system, including dry quenching furnace, dry quenching boiler and cyclone primary dust collector.Dry quenching boiler has flue gas heat exchange pipeline, first evaporator and second evaporator are sequentially arranged in pipeline along flue gas flow direction, both first evaporator and second evaporator are finned tube evaporator, the working heat exchange temperature where first evaporator is t1, the working heat exchange temperature where second evaporator is t2, 570 ℃≤t1≤610 ℃, t1>t2.Cyclone primary dust collector's dust removal efficiency is ≥90% and after filtration, coke powder particle size d is ≤0.25mm.Residual fine dust greatly weakens the scouring caused to first evaporator, first evaporator is set to finned tube evaporator and can also be well operated, since finned tube evaporator compared with light tube evaporator heat exchange area is large, this system can reduce pipeline consumption under the condition of keeping equal heat exchange capacity.

Description

Technical Field

[0001] This utility model relates to the field of dry quenching technology, and in particular to a cyclone dust removal dry quenching boiler system based on a full-fin tube evaporator. Background Technology

[0002] In the dry quenching coke process system, the high-temperature flue gas generated during the operation of the dry quenching furnace usually carries a large amount of coke powder, with a coke powder content of about 20g / Nm³.

[0003] To reduce the dust content in flue gas and ensure the operational stability of subsequent equipment, when a gravity dust collector is used in the primary dust collector of a conventional dry quenching coke boiler system, the heating surface of the evaporator typically adopts a combination of bare tubes and finned tubes. However, when a cyclone-type primary dust collector is used, the combination of bare tubes and finned tubes is poorly compatible with the cyclone-type primary dust collector, easily leading to dust accumulation problems. Utility Model Content

[0004] The purpose of this utility model embodiment is to provide a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator, so as to reduce material consumption and achieve investment savings. The specific technical solution is as follows:

[0005] A cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator includes:

[0006] Dry quenching furnace;

[0007] A dry quenching coke boiler includes: a flue gas heat exchange pipe, a first evaporator, and a second evaporator. The first evaporator and the second evaporator are sequentially arranged inside the flue gas heat exchange pipe along the flue gas flow direction. The operating heat exchange temperature of the first evaporator is t1, and the operating heat exchange temperature of the second evaporator is t2. 570℃≤t1≤610℃, t1>t2. Both the first evaporator and the second evaporator are finned tube evaporators.

[0008] A cyclone primary dust collector is provided, wherein the inlet of the cyclone primary dust collector is connected to the high-temperature flue gas outlet of the dry quenching furnace, and the outlet of the cyclone primary dust collector is connected to the flue gas inlet of the flue gas heat exchange pipe. The dust removal efficiency of the cyclone primary dust collector is ≥90%, and the particle size of the coke powder filtered by the cyclone primary dust collector is d, where d≤0.25mm.

[0009] In some embodiments, the cyclone primary dust collector is a cyclone water-cooled dust collector.

[0010] In some embodiments, 480℃≤t2≤520℃.

[0011] In some embodiments, the finned tube evaporator includes a tube body and spiral fins, the spiral fins being disposed on the outer wall of the tube body.

[0012] In some embodiments, the pipe body is a carbon steel pipe.

[0013] In some embodiments, the spiral fins are made of 08Al carbon steel sheet.

[0014] In some embodiments, the aperture area of ​​the flue gas heat exchange pipe and the cross-sectional area of ​​the first evaporator satisfy the following: under the working state of the cyclone dust removal dry quenching boiler system based on the full finned tube evaporator, the flue gas velocity at the location of the first evaporator is V, 9m / s≤V≤12m / s.

[0015] In some embodiments, the dust concentration in the flue gas filtered by the cyclone primary dust collector is less than or equal to 2 g / Nm³.

[0016] In some embodiments, it also includes:

[0017] Soot blowers are respectively installed above the first evaporator and the second evaporator.

[0018] In some embodiments, the sidewall of the flue gas heat exchange duct is a membrane water-cooled wall.

[0019] This application proposes a cyclone dust removal dry quenching coke boiler system based on a fully finned tube evaporator, comprising a dry quenching furnace, a dry quenching boiler, and a cyclone primary dust collector. The dry quenching boiler has a flue gas heat exchange duct, within which a first evaporator and a second evaporator are sequentially arranged along the flue gas flow direction. Both the first and second evaporators are finned tube evaporators, with the first evaporator operating at a heat exchange temperature of t1 and the second evaporator operating at a heat exchange temperature of t2, where 570℃≤t1≤610℃ and t1>t2. The inlet of the cyclone primary dust collector is connected to the high-temperature flue gas outlet of the dry quenching furnace, and the outlet of the cyclone primary dust collector is connected to the inlet of the flue gas heat exchange duct. The dust removal efficiency of the cyclone primary dust collector is ≥90%, and the particle size d of the filtered coke powder is ≤0.25mm.

[0020] In this technical solution, the cyclone primary dust collector works in conjunction with the all-finned tube evaporators (first evaporator and second evaporator). After the cyclone dust collector efficiently removes large coke particles, it can remove more than 90% of particulate matter, leaving residual fine dust particles with a diameter of less than or equal to 0.25 mm. During the operation of the cyclone dust collector-based dry quenching coke boiler system based on the all-finned tube evaporator, the scouring effect of residual fine dust on the first evaporator is significantly reduced compared to a gravity primary dust collector. Therefore, the first evaporator can operate well even when configured as a finned tube evaporator, and is less prone to bending or breakage. Compared with existing technologies, because the finned tube evaporator has a larger heat exchange area than the bare tube evaporator, this system can reduce the amount of piping required while maintaining the same heat exchange capacity.

[0021] Of course, any product implementing this utility model does not necessarily need to achieve all of the advantages described above at the same time. Attached Figure Description

[0022] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings.

[0023] Figure 1 A partial structural schematic diagram of a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator provided in this application embodiment;

[0024] Figure 2 for Figure 1 The diagram shows a partial structural schematic of the finned tube evaporator in a cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator.

[0025] Figure 3 for Figure 1 The diagram shows a partial layout of the finned tube evaporator in a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator.

[0026] The attached figures are labeled as follows:

[0027] Flue gas heat exchange pipe 1, membrane water-cooled wall 11, first evaporator 2, second evaporator 3, soot blower 4, tube body 21, first tube body 211, second tube body 212, spiral fin 22, first spiral fin 221, second spiral fin 222. Detailed Implementation

[0028] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art based on this application are within the protection scope of the present utility model.

[0029] In conventional dry quenching coke systems, when a gravity dust collector is used as the primary dust collector, the dust removal efficiency is approximately 30%. After filtration, the proportion of coke powder particles with a diameter >1.5mm is approximately 3.4%, of which the proportion of particles with a diameter of 1.5–1.0mm is approximately 14.6%, the proportion of particles with a diameter of 1.0–0.5mm is approximately 15.2%, the proportion of particles with a diameter of 0.5–0.25mm is approximately 19.8%, the proportion of particles with a diameter of 0.25–0.125mm is approximately 19.2%, the proportion of particles with a diameter of 0.125–0.063mm is approximately 10.6%, and the proportion of particles with a diameter ≤0.063mm is approximately 17.2%. The heating surface of the evaporator in the matching dry quenching coke boiler usually adopts a structure of "a combination of bare tubes and finned tubes", and the classification of this structure is mainly based on the flue gas temperature.

[0030] First, the heating surface of the evaporator in the high-temperature section is usually in the form of a bare tube, mainly based on the following two factors:

[0031] 1. Heat exchange requirements: The high-temperature flue gas itself has a high heat transfer coefficient, that is, the high-temperature flue gas has a strong heat transfer capacity. It does not need to rely on expanding the heat transfer surface to achieve the heat exchange target. The simple structure of the bare tube can meet the heat transfer requirements of this temperature range.

[0032] 2. Operational Reliability and Economy: High-temperature flue gas is characterized by high dust concentration (approximately 14 g / Nm³), large dust particle size (0.063~1.5 mm), and high flue gas velocity (7~10 m / s), resulting in severe erosion and wear on the heated surfaces. Commonly used fin materials, such as low-carbon steel like 08Al, exhibit a significant decrease in tensile strength at 650℃, falling below 80 MPa, only 1 / 4 to 1 / 5 of its tensile strength at room temperature. This makes it highly susceptible to bending and breakage under the combined effects of high temperature, its own weight, flue gas impact, and dust erosion. While using heat-resistant steel (such as 15CrMoG) to improve the fins' temperature resistance enhances their performance, it significantly increases manufacturing costs, by 2 to 3 times compared to bare tube solutions. Furthermore, it still fails to completely resolve the thermal stress problem caused by the difference in thermal expansion between the fins and the base tube.

[0033] Secondly, finned tubes are suitable for use on the heating surface of evaporators in the medium and low temperature range. This is because the heat transfer coefficient of flue gas in the medium and low temperature range is low. As the flue gas temperature decreases, its heat transfer capacity weakens. Using a finned structure can effectively expand the heat transfer area, thereby significantly improving the heat transfer efficiency in this section. Its heat transfer coefficient can usually reach 2 to 4 times that of bare tubes, which can effectively improve the recovery effect of waste heat in the medium and low temperature range.

[0034] The inventors discovered that when a cyclone dust collector is used in the primary dust collector, the high dust removal efficiency of the cyclone primary dust collector results in coke powder with small particle size and smooth edges after dust removal. The use of bare tubes for the heating surface of the high-temperature evaporator presents at least one of the following problems: ① Severe dust accumulation: Although the dust content of the flue gas treated by the cyclone primary dust collector is reduced (removal rate ≥90%), the residual coke powder particles are small and have smooth edges, making them easily electrostatically adsorbed onto the bare tube wall; ② Insufficient flow rate: The low flue gas flow rate in the bare tube section leads to dust deposition; ③ To meet heat exchange requirements, a large number of bare tubes need to be arranged, resulting in high material consumption and increased equipment investment.

[0035] to this end, Figure 1 A partial structural schematic diagram of a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator is provided for an embodiment of this application, as shown below. Figure 1 As shown in the figure, an embodiment of this application proposes a cyclone dust removal dry quenching coke boiler system based on a full-finned tube evaporator, including a dry quenching furnace, a dry quenching boiler, and a cyclone primary dust collector. The dry quenching boiler has a flue gas heat exchange pipe 1, in which a first evaporator 2 and a second evaporator 3 are arranged sequentially along the flue gas flow direction. Both the first evaporator 2 and the second evaporator 3 are finned tube evaporators, and the operating heat exchange temperature of the first evaporator 2 is t1, and the operating heat exchange temperature of the second evaporator 3 is t2, where 570℃≤t1≤610℃, and t1>t2. The inlet of the cyclone primary dust collector is connected to the high-temperature flue gas outlet of the dry quenching furnace, and the outlet of the cyclone primary dust collector is connected to the inlet of the flue gas heat exchange pipe 1. The dust removal efficiency of the cyclone primary dust collector is ≥90%, and the particle size d of the filtered coke powder is ≤0.25mm.

[0036] In this technical solution, a cyclone primary dust collector works in conjunction with all-finned tube evaporators (first evaporator 2 and second evaporator 3). The cyclone dust collector efficiently removes large coke particles, removing over 90% of particulate matter, with residual fine dust particles having a diameter of less than or equal to 0.25 mm. During operation of the cyclone dust collector-based dry quenching coke boiler system based on the all-finned tube evaporator, the scouring effect of residual fine dust on the first evaporator 2 is significantly reduced compared to a gravity primary dust collector. Therefore, the first evaporator 2 can operate well as a finned tube evaporator, without easily experiencing bending or breakage issues. Compared to existing technologies, because the finned tube evaporator has a larger heat exchange area than a bare tube evaporator, this system can reduce the amount of piping required while maintaining the same heat exchange capacity.

[0037] Cyclone primary dust collectors can be water-cooled cyclone dust collectors. These water-cooled cyclone dust collectors reduce the flue gas temperature at the inlet of the dry quenching coke boiler while removing dust by installing a water-cooling device on the outside of the dust collector cylinder. This technical solution cools the high-temperature flue gas in the flue gas heat exchange pipe 1 to between 570℃ and 610℃. The temperature reduction brings the following technical effects: First, the volume contraction of the flue gas leads to a decrease in flow velocity, reducing the impact of residual fine dust on the first evaporator 2; second, the metal material of the first evaporator 2 easily maintains sufficient tensile strength under operating conditions of 570℃ to 610℃.

[0038] Specifically, the first evaporator 2 operates at a temperature t1 between 570°C and 610°C, and the second evaporator 3 operates at a temperature t2 between 480°C and 520°C.

[0039] Finned tube evaporators can employ a spiral fin structure, where the spiral fins are fixed to the outer wall of the tube body using a high-frequency welding process. The tube body material can be low-carbon steel or low-alloy steel. For example, the tube body can be made of carbon steel, and the spiral fins can be made of 08Al carbon steel sheet.

[0040] Figure 2 for Figure 1 The diagram shown is a partial structural schematic of the finned tube evaporator in a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator. Figure 2 As shown, specifically, a finned tube evaporator may include a tube body and spiral fins, with the spiral fins disposed on the outer wall of the tube body. The tube body can be made of seamless or welded steel pipe, and its material can be low-carbon steel. For example, the diameter D of the tube body is 38 mm, the pitch m of the spiral fins is designed to be 12 mm, the fin height h is 18 mm, and the fin thickness d is 1.2 mm, but it is not limited to these. The spiral fins are fixedly connected to the tube body by high-frequency welding. In addition, the surface of the spiral fins can be sandblasted to enhance the surface roughness, thereby further improving the heat exchange efficiency.

[0041] To address this, this technical solution utilizes a combination of tubes and spiral fins. The spiral fins increase the heat exchange surface area and guide the flue gas into a swirling flow. The centrifugal force generated by the spiral structure causes particulate matter in the flue gas to move outwards, reducing deposition on the heat exchange surface; simultaneously, the spiral channels create a turbulent effect. Compared to the traditional "bare tube and finned tube combination" structure, this design exhibits better adaptability in cyclone dust collector environments: firstly, the continuous flow channels formed by the spiral fins prevent particulate matter from accumulating between the fins; secondly, the uniformly distributed spiral structure can adapt to the non-uniform flow field generated by cyclone dust collectors. Therefore, this technical solution effectively reduces the risk of dust accumulation while improving heat exchange efficiency.

[0042] Specifically, the tubes of the finned tube evaporator are arranged in a staggered pattern. Figure 3 for Figure 1 The diagram shown is a partial layout of the finned tube evaporator in a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator. Figure 3 As shown, the finned tube evaporator includes multiple tube bodies 21, each tube body 21 being provided with spiral fins 22. The first tube body 211 and the second tube body 212 are arranged in a staggered vertical arrangement. The spiral fins 22 include first spiral fins 221 and second spiral fins 222. Both the first tube body 211 and the second tube body 212 have folded sections at their ends. The first spiral fins 221 are disposed on the tube sections connecting the upper and lower ends of the folded sections of the first tube body 211, and the second spiral fins 222 are disposed on the tube sections connecting the upper and lower ends of the folded sections of the second tube body 212.

[0043] Furthermore, to further reduce the dust electrostatically adsorbed on the outer surface of the first evaporator 2, the aperture area of ​​the flue gas heat exchange pipe and the cross-sectional area of ​​the first evaporator can be set so that, under the operating conditions of the cyclone dust removal dry quenching boiler system based on the all-finned tube evaporator, the flue gas velocity at the location of the first evaporator is V, where 9 m / s ≤ V ≤ 12 m / s, for example, V = 9 m / s, 10 m / s, 11 m / s, 12 m / s, or any intermediate value between the above two values. By adjusting the flue gas velocity at the location of the first evaporator, this embodiment of the solution increases the flue gas velocity at the location of the first evaporator, reducing the problem of dust accumulation caused by electrostatic adsorption on the outer surface of the first evaporator 2. At the same time, increasing the flue gas velocity also helps to form turbulence between the spiral fins, enhancing the dust removal effect.

[0044] To further reduce dust electrostatic adsorption on the outer surface of the second evaporator 3, the aperture area of ​​the flue gas heat exchange pipe and the cross-sectional area of ​​the first evaporator can be set so that, under the operating conditions of the cyclone dust removal dry quenching boiler system based on the all-finned tube evaporator, the flue gas velocity V at the location of the first evaporator is 9 m / s ≤ V ≤ 12 m / s, for example, V = 9 m / s, 10 m / s, 11 m / s, 12 m / s, or any intermediate value between the above two values. This reduces the problem of dust accumulation caused by electrostatic adsorption on the outer surface of the second evaporator 3.

[0045] Compared with the conventional combination structure of bare tube and finned tube, this all-finned tube structure achieves simultaneous improvement in anti-dust accumulation performance and heat exchange efficiency under the same dust removal conditions through synergistic optimization of flow rate and structure.

[0046] The dust concentration in the flue gas filtered by the cyclone primary dust collector is less than or equal to 2g / Nm³. Reducing the dust concentration from the conventional 20g / Nm³ to below 2g / Nm³ effectively reduces the impact of the filtered coke powder on the first evaporator 2 and the second evaporator 3, thereby allowing the finned tube evaporator to operate smoothly.

[0047] In specific implementations, embodiments of this application also include a soot blower 4, which is respectively disposed above the first evaporator 2 and the second evaporator 3.

[0048] The number of soot blowers 4 installed above the first evaporator 2 is not limited to one; it can be two or more. Similarly, the number of soot blowers 4 installed above the second evaporator 3 is not limited to one; it can be two or more. For example, the installation position of the soot blowers 4 can cover the entire surface of the first evaporator 2 and the entire surface of the second evaporator 3.

[0049] This technical solution actively removes dust accumulated on the surface of the finned tube evaporator by installing a soot blower 4 at the top. Regular cleaning maintains the heat exchange efficiency of the first evaporator 2 and the second evaporator 3. Compared with passive cleaning methods, this active cleaning method effectively solves the dust accumulation problem unique to finned tubes and avoids the decrease in heat exchange efficiency caused by dust accumulation.

[0050] The sidewall of the flue gas heat exchange duct 1 is a membrane water-cooled wall 11. The membrane water-cooled wall 11 can be composed of continuously arranged water-cooled tubes and fins welded between adjacent water-cooled tubes, forming a sealed wall structure. As the sidewall structure of the flue gas heat exchange duct 1, the membrane water-cooled wall 11, through its continuous water-cooled tubes and the sealed structure formed by welding the fins, can effectively increase the heat exchange area and improve the overall strength of the duct. In a high-temperature flue gas environment, the working fluid inside the water-cooled tubes continuously carries away heat.

[0051] The embodiments of this application provide a cyclone dust removal dry quenching boiler system based on a full-finned tube evaporator. The primary dust collector is a cyclone type primary dust collector, and the heating surface of the matching dry quenching boiler evaporator can adopt a "full-finned tube" structure. The specific reasons and advantages are as follows:

[0052] Cyclone-cooled primary dust collectors effectively reduce the temperature of flue gas entering the boiler, lowering the inlet flue gas temperature of the high-temperature evaporator to approximately 590℃. Under this temperature condition, the tensile strength of the low-carbon steel fin material can still be maintained within the range of 80~120MPa, meeting the strength requirements for use. Simultaneously, after treatment by the cyclone-cooled dust collector, the dust concentration in the flue gas is significantly reduced (approximately 2g / Nm³), the dust particle size is reduced (≤0.25mm), and the erosion and wear of the heated surfaces by dust is greatly reduced.

[0053] Based on the aforementioned improvements in flue gas parameters, the adoption of a full finned tube structure has multiple advantages: First, it can save on equipment investment, eliminating the need for expensive heat-resistant steel; second, it allows for a compact structural layout, reducing the space occupied by the equipment; and third, the extended heating surface formed by the fins can enhance flue gas turbulence, which helps to peel off and remove fine dust adsorbed by electrostatics on the heating surface, thus having a certain self-cleaning effect.

[0054] The above description is merely a preferred embodiment of this utility model and is not intended to limit the scope of protection of this utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this utility model are included within the scope of protection of this utility model.

Claims

1. A cyclone dust removal and dry quenching boiler system based on a fully finned tube evaporator, characterized in that, include: Dry quenching furnace; A dry quenching coke boiler includes: a flue gas heat exchange pipe (1), a first evaporator (2) and a second evaporator (3). Along the flue gas flow direction of the flue gas heat exchange pipe (1), the first evaporator (2) and the second evaporator (3) are sequentially arranged in the flue gas heat exchange pipe (1). The working heat exchange temperature of the first evaporator (2) is t1, and the working heat exchange temperature of the second evaporator (3) is t2. 570℃≤t1≤610℃, t1>t2. Both the first evaporator (2) and the second evaporator (3) are finned tube evaporators. A cyclone primary dust collector is provided, wherein the inlet of the cyclone primary dust collector is connected to the high-temperature flue gas outlet of the dry quenching furnace, the outlet of the cyclone primary dust collector is connected to the flue gas inlet of the flue gas heat exchange pipe (1), the dust removal efficiency of the cyclone primary dust collector is ≥90%, and the particle size of the coke powder after filtration by the cyclone primary dust collector is d, where d≤0.25mm.

2. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, The cyclone primary dust collector is a cyclone water-cooled dust collector.

3. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 2, characterized in that, 480℃≤t2≤520℃。 4. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, The finned tube evaporator includes a tube body and spiral fins, wherein the spiral fins are disposed on the outer wall of the tube body.

5. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 4, characterized in that, The pipe body is a carbon steel pipe.

6. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 4, characterized in that, The spiral fins are made of 08Al carbon steel plate.

7. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, The aperture area of ​​the flue gas heat exchange pipe (1) and the cross-sectional area of ​​the first evaporator (2) satisfy the following: under the working state of the cyclone dust removal dry quenching boiler system based on the full finned tube evaporator, the flue gas velocity at the position of the first evaporator (2) is V, 9m / s≤V≤12m / s.

8. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, The dust concentration in the flue gas filtered by the cyclone primary dust collector is less than or equal to 2 g / Nm³.

9. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, Also includes: Soot blowers (4) are respectively positioned above the first evaporator (2) and the second evaporator (3).

10. The cyclone dust removal and dry quenching boiler system based on a full-finned tube evaporator according to claim 1, characterized in that, The sidewall of the flue gas heat exchange pipe (1) is a membrane water-cooled wall (11).

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