Heat recovery system and device based on small-diameter dual-function

Abstract

The present invention relates to the field of heat recovery technology, and more specifically to a heat recovery system and device based on small-diameter dual-function; comprising a heat-insulating medium storage tank, a plurality of heat exchange blasting spaces, each heat exchange blasting space having its own tube-fin heat exchanger; the diameter of the heat exchange tube in the tube-fin heat exchanger is ≤4mm; each tube-fin heat exchanger has its own liquid inlet valve and liquid outlet valve, a liquid inlet pump is arranged at the output end of the medium storage tank, and the liquid inlet pump is connected to each liquid inlet valve by a branch pipeline; the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 The present invention connects a plurality of heat exchange tubes in parallel, abandoning the series connection of the traditional fin heat exchanger, so that when one of the heat exchange tubes is blocked, the fluid can flow along the other unblocked heat exchange tubes, so that the tube-fin heat exchanger can operate normally.

Description

Technical Field

[0001] The invention relates to the technical field of heat recovery, in particular to a heat recovery system and device based on small-diameter dual-functions. Background Art

[0002] In the chemical industry, many compounds are obtained by substitution reactions; substitution reactions are exothermic reactions that release a large amount of heat; in order to maintain the normal operation of the reactor, the reactor jacket is connected to a circulating heat dissipation system, and a heat transfer medium (such as water) is used to transfer the heat to a cooling tower. After the heat is dissipated by the cooling tower, the heat is re-input into the circulating heat dissipation system of the reactor jacket or directly discharged; the exothermic reaction causes the high temperature section of the heat transfer medium to reach 120℃-130℃, and the medium input temperature of the cooling tower is about 80℃. At present, the ratio of heat exchange area to heat exchanger volume of cooling towers in the chemical industry is about 8.4m 2 / m 3 , which makes the heat exchange efficiency low, bulky and occupies a large area.

[0003] During the production process of chlorinated polymers, since the substitution reaction of chlorine is an exothermic reaction, about 3500 kJ of heat is released for every 1 kg of chlorine reacted. The traditional process must transfer this part of heat through hot water or other media, and then evaporate and dissipate it through an open cooling tower or a closed cooling tower, and then recycle it. The outlet temperature of the circulating water is generally greater than 80°C. The drying process of the product generally adopts fluidized bed boiling drying, which requires the use of a steam heat exchanger, generally a tube-fin heat exchanger, to heat the air to a certain temperature; the intermittent bed generally adopts The air temperature is about 70℃-80℃; the continuous fluidized bed is generally divided into flash drying and fluidized bed chamber drying, of which flash drying requires hot air temperature of about 110℃-120℃, and fluidized bed chamber drying requires hot air temperature of about 65℃-85℃; in response to the national energy-saving and consumption-reducing policy, the high-temperature hot water produced by the chlorination reaction can be used in the drying heat exchanger; but the traditional heat exchanger is a DN25 or DN32 tube-fin heat exchanger, which is relatively large. If steam heat exchange is used, the heat exchange area is about 1250m 2 The drying demand can be met within 1000 square meters, but if hot water is used for heat exchange, the volume will be larger and cannot meet the relevant performance requirements of fluidized bed drying, such as large wind resistance and insufficient air volume. In addition, the floor area is relatively large, the installation space is limited, and the reliability of the equipment is low.

[0004] As the core device of the heat recovery system, the importance of the tube-fin heat exchanger is self-evident. Its principle is that the fluid carrying heat energy enters the heat exchange tube along the liquid inlet joint, and multiple heat exchange tubes are connected end to end through elbows to form a whole single liquid flow channel. The fluid inside the heat exchange tube will transfer heat to the fins on the outer wall, and the air enters the tube-fin heat exchanger along the air inlet joint and contacts the fins, thereby taking away the heat on the surface of the fins to heat the air. The heated air enters the storage tank for storage and recycling. Since multiple heat exchange tubes are connected end to end through elbows to form a single liquid flow channel, the residence time of the fluid in the heat exchange tube is extended, so that the heat energy of the fluid in the heat exchange tube can be fully exchanged, thereby improving the heat recovery efficiency. However, due to the limitations of a single liquid flow channel, when one section of the liquid flow channel is blocked, multiple heat exchange tubes will be unable to pass the fluid, causing the entire tube-fin heat exchanger to fail to work, so that heat recovery is affected. Summary of the invention

[0005] In order to make up for the shortcomings of the prior art, the present invention proposes a heat recovery system and device based on a small-diameter dual-function. The present invention has the advantages of high heat exchange efficiency, small footprint, and significant energy saving. The present invention utilizes the heat of chlorination reaction or other exothermic reactions in the drying process of subsequent products, utilizes the inherent fluidization link in the production process to achieve high-temperature medium cooling, and utilizes the heat released by the exothermic reaction as the production of fluidized drying hot air, so that the fluidized bed has both fluidized drying and cooling and heat dissipation functions, greatly reducing energy consumption. At the same time, the heat exchange area / outer volume of the tube-fin heat exchanger is ≥280m 2 / m 3 The heat exchange area is increased without increasing the volume of the heat exchanger; it is only necessary to modify the tube-fin heat exchanger in the existing blast heat exchange space of the fluidized bed, thereby reducing energy consumption without increasing the floor space and volume.

[0006] The technical solution adopted by the present invention to solve the technical problem is as follows: the heat recovery system based on small-diameter dual-function of the present invention comprises a heat-insulating medium storage tank, a plurality of heat exchange blasting spaces, each heat exchange blasting space has its own tube-fin heat exchanger; the diameter of the heat exchange tube in the tube-fin heat exchanger is ≤4mm; each tube-fin heat exchanger has its own liquid inlet valve and liquid outlet valve, a liquid inlet pump is arranged at the output end of the medium storage tank, and the liquid inlet pump is connected to each liquid inlet valve by a branch pipeline; the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 The air inlet of each heat exchange blast space is connected to its own blower, and the air temperature output from the heat exchange blast space is 65°C-85°C; the medium storage tank has at least one first medium inlet that allows heat transfer medium with a temperature higher than 95°C to be input therein.

[0007] Preferably, the medium storage tank has at least one second medium inlet that allows heat transfer medium below 80°C to be input therein, and the medium output by each liquid outlet valve is input to the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve; or, the medium output by each liquid outlet valve is input to the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve after passing through a cooling tower.

[0008] Preferably, each tube-fin heat exchanger has a group of water heat exchangers; or each tube-fin heat exchanger has a group of water heat exchangers and a group of steam heat exchangers, and the water heat exchangers and the steam heat exchangers are connected in parallel.

[0009] Preferably, the heat exchange area of ​​each group of tube-fin heat exchangers is ≥ 1250m 2 ; Single heat exchange tube diameter / single heat exchange area ≥1mm / 50m 2 (3mm / 150m 2 ).

[0010] Preferably, the heat recovery system applied to the closed cooling tower comprises at least one set of tube-fin heat exchangers, and the heat exchange area / outer volume of each tube-fin heat exchanger is ≥ 280m 2 / m 3 The heat recovery system of the present invention is applied to a closed cooling tower, which can reduce the temperature of the heat transfer medium from about 80°C to 30°C or below. Compared with the traditional closed cooling tower (usually with a heat exchange area / volume of 8.4m 2 / m 3 ), with higher heat exchange efficiency under the same volume.

[0011] Preferably, the heat recovery system for chemical exothermic reaction comprises at least one set of tube-fin heat exchangers, and the heat exchange area / outer volume of each tube-fin heat exchanger is ≥ 280m 2 / m 3 .

[0012] Preferably, the heat recovery system is used in the production of chlorinated polymers, and the heat recovery device in the heat recovery system includes at least one set of tube-fin heat exchangers, and the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 The heat energy recovery system of the present invention is applied to the production of chlorinated polymers, and can reduce the temperature of the heat transfer medium in the high temperature section of the reactor of the chlorination reaction from 120°C-130°C to 65°C-85°C.

[0013] Preferably, the tube-fin heat exchanger is arranged at the air inlet of the fluidized bed, and the air enters the fluidized bed chamber after passing through the tube-fin heat exchanger. The ambient air is heated to 65°C-85°C hot air after heat exchange in the tube-fin heat exchanger and is input into the fluidized bed chamber / bed layer.

[0014] Preferably, the heat transfer medium of the tube-fin heat exchanger is the heat transfer medium after the reactor jacket absorbs the reaction heat, the heat transfer medium channel outlet of the reactor and the medium inlet of the tube-fin heat exchanger are connected by a first pipeline, and a first pump is arranged on the first pipeline, and the first pump makes the heat transfer medium flow from the reactor jacket to the tube-fin heat exchanger.

[0015] Preferably, a respective tube-fin heat exchanger is provided at the inlet of each chamber of the fluidized bed.

[0016] Preferably, the heat transfer medium output by the tube-fin heat exchanger is input into the jacket of the reactor through the second pipeline; or, the heat transfer medium output by the tube-fin heat exchanger is input into the closed cooling tower through the third pipeline.

[0017] Preferably, the above-mentioned heat energy recovery system is applied in the production of chlorinated polymers, the high-temperature medium inlet of the medium storage tank is connected to the medium outlet of the chlorination reactor jacket, the heat transfer medium with a temperature higher than 95° C. in the reactor jacket is input into the medium storage tank; the air output from the heat exchange blast space is input into the fluidizing chamber of the fluidized bed; the heat energy recovery system serves as a hot air input system for the fluidized bed.

[0018] Preferably, the substitution reaction of chlorine is an exothermic reaction, and about 3500 kJ of heat is released for every 1 kg of chlorine reacted. This part of heat is transferred out through the heat transfer medium of the reactor jacket to maintain the temperature of the reactor and ensure the normal occurrence of the substitution reaction; the high temperature section of this part of the medium can reach 120°C-130°C. The outlet water temperature of the reactor jacket is about 80°C.

[0019] Preferably, the drying process of chlorinated polymers generally adopts fluidized bed boiling drying, which requires the use of a steam heat exchanger to heat the air to a certain temperature. Intermittent fluidized beds generally use air temperatures of about 70°C-80°C; continuous fluidized beds are generally divided into flash drying and fluidized bed chamber drying, of which flash drying requires hot air temperatures of about 110°C-120°C, and fluidized bed chamber drying requires hot air temperatures of about 65°C-85°C. In traditional processes, all heat transfer media in the reactor are first sent to a cooling tower to cool to about 32°C, and then sent to the reactor as a heat transfer medium to cool the reactor.

[0020] Preferably, the present invention takes out the high temperature section medium of the reactor jacket, and uses the heat energy of the high temperature section medium to generate hot air for the fluidized bed through the heat energy recovery system, which not only meets the hot air drying requirements of the fluidized bed, but also reduces the temperature of the high temperature section medium to 65°C-80°C. At this time, the fluidized bed is equivalent to the first stage of cooling, and the medium coming out of the fluidized bed can be directly sent to the reactor for high temperature section cooling, or sent to the cooling tower to cool to below 32°C and then sent to the reactor for low temperature section cooling.

[0021] Preferably, the heat exchanger can be installed after the fan or before the fan.

[0022] A heat recovery device based on small-diameter dual-function, which is suitable for the heat recovery system based on small-diameter dual-function described above, comprises a tube-fin heat exchanger; the tube-fin heat exchanger comprises a shell and a fin body inside the shell; the fin bodies are multiple and arranged adjacently; the fin bodies are evenly distributed in the left and right directions inside the shell; the multiple fin bodies form a movable gap with the front and rear inner walls of the shell; multiple baffles are fixed in the movable gap; the baffles are in sealing contact with the fin body, and the baffles are in sealing contact with the inner wall of the shell; the two movable gaps are The baffles are staggered in the left and right directions; the front side of the shell is connected to the air inlet joint; the rear side of the shell is connected to the air outlet joint; the air inlet joint and the air outlet joint are arranged away from each other in the left and right directions of the shell; a plurality of heat exchange tubes are penetrated on the left and right sides of the shell; a plurality of heat exchange tubes are arranged in contact with the fin body; the left side of the shell is fixedly connected to the liquid inlet tank; the lower inner wall of the liquid inlet tank is fixedly connected to the liquid inlet valve; the right side of the shell is fixedly connected to the liquid outlet tank; the lower inner wall of the liquid outlet tank is fixedly connected to the liquid outlet valve; one end of the heat exchange tube is connected to the liquid inlet tank, and the other end is connected to the liquid outlet tank.

[0023] Preferably, the upper and lower movable seals of the inner wall of the liquid inlet box are connected to the liquid inlet plate; the upper surface of the liquid inlet plate is fixedly connected to the left rod; a left hole is penetrated at the upper position of the inner wall of the liquid inlet box; the upper end of the left rod passes through the left hole and is fixedly connected to the movable plate; a gap is left between the left hole and the outer wall of the left rod; the lower surface of the movable plate and the upper surface of the shell are connected by a tension spring.

[0024] Preferably, the upper and lower inner walls of the liquid outlet box are movably sealed and connected to the liquid outlet plate; the upper surface of the liquid outlet plate is fixedly connected to the right rod; a right hole is provided through the upper position of the inner wall of the liquid outlet box; the upper end of the right rod passes through the right hole and is fixedly connected to the lower surface of the movable plate; a gap is left between the right hole and the outer wall of the right rod; and one-way valves are provided at the ends of the heat exchange tubes, with inflow at one end and outflow at the other end.

[0025] Preferably, the top wall of the shell is penetrated by a front hole and a rear hole; the front hole is located directly above the front movable gap; the rear hole is located directly above the rear movable gap; the front movable gap is divided into multiple front gaps by a baffle; the movable seal in the front gap is connected to the front movable block; the upper surface of the front movable block is fixedly connected to the front rod; the upper end of the front rod passes through the front hole and is fixedly connected to the lower surface of the movable plate; the rear movable gap is divided into multiple rear gaps by a baffle; the movable seal in the rear gap is connected to the rear movable block; the upper surface of the rear movable block is fixedly connected to the rear rod; the upper end of the rear rod passes through the rear hole and is fixedly connected to the lower surface of the movable plate.

[0026] Preferably, a plurality of spacers are evenly distributed on the upper and lower inner walls of the shell; the material of the spacers is the same as that of the fin body; the spacers extend to the front gap in the front and to the rear gap in the rear; the spacers separate two adjacent heat exchange tubes in the upper and lower parts; the vertical thickness of the front movable block and the rear movable block is greater than the distance between adjacent spacers; the lengths of the front rod, the rear rod, the left rod and the right rod are equal.

[0027] Preferably, the upper surfaces of the shell, the liquid inlet box and the liquid outlet box are flush; the upper surfaces of the shell, the liquid inlet box and the liquid outlet box are fixedly connected to the protective shell; the inner wall of the protective shell is movably and sealedly connected to the outer wall of the movable plate; the movable plate passes through the upper and lower parts and is movably and sealedly connected to the compensation block; the compensation block is fixedly connected to the shell; the space between the lower surface of the movable plate and the upper surface of the shell is called a storage chamber; the gas in the liquid inlet box, the liquid outlet box and the movable gap can enter the storage chamber for avoidance and storage.

[0028] The beneficial effects of the present invention are as follows:

[0029] 1. The present invention has the advantages of high heat exchange efficiency, small footprint and significant energy saving. The present invention utilizes the heat of chlorination reaction or other exothermic reaction in the drying process of subsequent products, utilizes the inherent fluidization link in the production process to realize the cooling of the high-temperature medium, and utilizes the heat released by the exothermic reaction as the production of fluidized drying hot air, so that the fluidized bed has both fluidized drying and cooling and heat dissipation functions, which greatly reduces energy consumption. At the same time, the heat exchange area / outer volume of the tube-fin heat exchanger is ≥280m 2 / m 3 The heat exchange area is increased without increasing the volume of the heat exchanger; it is only necessary to modify the tube-fin heat exchanger in the existing blast heat exchange space of the fluidized bed, thereby reducing energy consumption without increasing the floor space and volume.

[0030] 2. The present invention can completely replace the original steam heat exchanger with a hot water heat exchanger; of course, a part of the original steam heat exchanger can also be retained; hot water is pumped into the tube-fin heat exchange tube by a hot water pump. The heat exchange tube diameter of the heat exchanger of the present invention is ≤4mm, and each small heat exchange tube is provided with a hydrophobic aluminum fin to increase the heat exchange area. In this way, compared with the heat exchanger with a heat exchange tube diameter of 25mm or 32mm in the same size space, the heat exchange area is more than doubled, and the wind resistance is ≤300pa, which ensures the stable operation of fluidized bed drying.

[0031] 3. The present invention connects a plurality of heat exchange tubes in parallel, abandoning the series connection of traditional fin heat exchangers, so that when one of the heat exchange tubes is blocked, the fluid can flow along other unblocked heat exchange tubes, so that the tube-fin heat exchanger can operate normally; the liquid inlet plate is movably connected up and down in the liquid inlet box, and the liquid outlet plate is movably connected in the liquid outlet box, so that the number of activated heat exchangers in the tube-fin heat exchanger can adapt to the change of the amount of incoming fluid, so that on the one hand, too few activated heat exchange tubes affect the heat energy recovery efficiency, and on the other hand, insufficient fluid in the heat exchange tubes can be avoided to affect the heat energy recovery effect.

[0032] 4. In the present invention, the rear movable block is at the same height as the front movable block and moves upward synchronously, and the distance between adjacent spacers is smaller than the thickness of the front movable block and the rear movable block. Therefore, through the cooperation of the front movable block and the rear movable block, the surrounding space of the enabled heat exchange tube in the shell is separated from the surrounding space of the unenabled heat exchange tube, so that the gas entering the shell can concentrate on the fin body around the enabled heat exchange tube to exchange heat, further ensuring the heat energy recovery effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The present invention is further described below in conjunction with the accompanying drawings and implementation modes.

[0034] Figure 1 It is the original process principle diagram of the recycling system;

[0035] Figure 2 It is the current process principle diagram of the recycling system;

[0036] Figure 3 This is the first arrangement of the heat exchange tubes in the present invention;

[0037] Figure 4 This is the second arrangement mode of the heat exchange tubes in the present invention;

[0038] Figure 5 is a three-dimensional diagram of a tube-fin heat exchanger in the present invention;

[0039] Figure 6 yes Figure 5 A three-dimensional image from another angle;

[0040] Figure 7 is a three-dimensional diagram of the tube-fin heat exchanger of the present invention without the protective shell;

[0041] Figure 8 It is a three-dimensional diagram of the liquid inlet box and the liquid outlet box in the present invention;

[0042] Fig. 9 is a three-dimensional diagram of the housing in the present invention;

[0043] Fig.10 It is a three-dimensional diagram of the fin body and the heat exchange tube in the present invention;

[0044] Fig.11 yes Figure 5 A top sectional view of .

[0045] In the figure: shell 1, fin body 11, movable gap 12, front gap 121, rear gap 122, baffle 13, air inlet connector 14, air outlet connector 15, front hole 16, rear hole 17, spacer 18, heat exchange tube 2, liquid inlet box 3, liquid inlet valve 31, liquid inlet plate 32, left rod 33, left hole 34, liquid outlet box 4, liquid outlet valve 41, liquid outlet plate 42, right rod 43, right hole 44, movable plate 5, tension spring 51, front movable block 52, front rod 53, rear movable block 54, rear rod 55, compensation block 56, storage chamber 57, protective shell 6. DETAILED DESCRIPTION

[0046] In order to make the technical means, creative features, objectives and effects achieved by the present invention easy to understand, the present invention is further explained below in conjunction with specific implementation methods.

[0047] like Figures 1 to 11 As shown, the present invention includes the following embodiments:

[0048] Embodiment 1:

[0049] The heat recovery system based on small-diameter dual-function includes a heat-insulating medium storage tank, multiple heat exchange blasting spaces, each heat exchange blasting space has its own tube-fin heat exchanger; the diameter of the heat exchange tube 2 in the tube-fin heat exchanger is ≤4mm; each tube-fin heat exchanger has its own inlet valve 31 and outlet valve 41, and an inlet pump is arranged at the output end of the medium storage tank, and the inlet pump is connected to each inlet valve 31 by a branch pipeline; the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 The air inlet of each heat exchange blast space is connected to its own blower, and the air temperature output from the heat exchange blast space is 65°C-85°C; the medium storage tank has at least one first medium inlet that allows heat transfer medium with a temperature higher than 95°C to be input therein.

[0050] The medium storage tank has at least one second medium inlet that allows heat transfer medium below 80°C to be input therein, and the medium output by each liquid outlet valve 41 is input into the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve; or, the medium output by each liquid outlet valve 41 is input into the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve after passing through a cooling tower.

[0051] Each tube-fin heat exchanger has a group of water heat exchangers; or each tube-fin heat exchanger has a group of water heat exchangers and a group of steam heat exchangers, and the water heat exchangers and the steam heat exchangers are connected in parallel.

[0052] The heat exchange area of ​​each group of tube-fin heat exchanger is ≥1250m 2; Single heat exchange tube 2 diameter / single heat exchange area ≥1mm / 50m2 (3mm / 150m 2 ).

[0053] Heat recovery system for closed cooling tower, including at least one set of tube-fin heat exchanger, the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 The heat recovery system of the present invention is applied to a closed cooling tower, which can reduce the temperature of the heat transfer medium from about 80°C to 30°C or below. Compared with the traditional closed cooling tower (usually with a heat exchange area / volume of 8.4m 2 / m 3 ), with higher heat exchange efficiency under the same volume.

[0054] Heat recovery system for chemical exothermic reaction, including at least one set of tube-fin heat exchanger, the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m 2 / m 3 .

[0055] Application of heat recovery system in chlorinated polymer production. The heat recovery system includes at least one set of tube-fin heat exchangers. The heat exchange area / outer volume of each tube-fin heat exchanger is ≥ 280m 2 / m 3 The heat energy recovery system of the present invention is applied to the production of chlorinated polymers, and can reduce the temperature of the heat transfer medium in the high temperature section of the reactor of the chlorination reaction from 120°C-130°C to 65°C-85°C.

[0056] The tube-fin heat exchanger is installed at the air inlet of the fluidized bed, and the air enters the fluidized bed chamber after passing through the tube-fin heat exchanger. The ambient air is heated to 65℃-85℃ hot air after heat exchange in the tube-fin heat exchanger and is input into the fluidized bed chamber / bed layer.

[0057] The heat transfer medium of the tube-fin heat exchanger is the heat transfer medium after the reactor jacket absorbs the reaction heat. The heat transfer medium channel outlet of the reactor and the medium inlet of the tube-fin heat exchanger are connected by a first pipeline. A first pump is arranged on the first pipeline. The first pump makes the heat transfer medium flow from the reactor jacket to the tube-fin heat exchanger.

[0058] The inlet of each chamber of the fluidized bed is provided with a respective tube-fin heat exchanger.

[0059] The heat transfer medium output by the tube-fin heat exchanger is input into the jacket of the reactor through the second pipeline; or, the heat transfer medium output by the tube-fin heat exchanger is input into the closed cooling tower through the third pipeline.

[0060] The above-mentioned heat recovery system is applied in the production of chlorinated polymers. The high-temperature medium inlet of the medium storage tank is connected to the medium outlet of the chlorination reactor jacket, and the heat transfer medium with a temperature higher than 95°C in the reactor jacket is input into the medium storage tank; the air output from the heat exchange blast space is input into the fluidizing chamber of the fluidized bed; the heat recovery system serves as a hot air input system for the fluidized bed.

[0061] The substitution reaction of chlorine is an exothermic reaction, and about 3500 kJ of heat is released for every 1 kg of chlorine reacted. This part of heat is transferred out through the heat transfer medium of the reactor jacket to maintain the reactor temperature and ensure the normal occurrence of the substitution reaction; the high temperature section of this part of the medium can reach 120℃-130℃. The outlet water temperature of the reactor jacket is about 80℃.

[0062] The drying process of chlorinated polymers generally uses fluidized bed boiling drying, which requires the use of a steam heat exchanger to heat the air to a certain temperature. Intermittent fluidized beds generally use air temperatures of about 70°C-80°C; continuous fluidized beds are generally divided into flash drying and fluidized bed chamber drying, of which flash drying requires hot air temperatures of about 110°C-120°C, and fluidized bed chamber drying requires hot air temperatures of about 65°C-85°C. In traditional processes, all heat transfer media in the reactor are first sent to a cooling tower to cool to about 32°C, and then sent to the reactor as a heat transfer medium to cool the reactor.

[0063] The present invention takes out the high temperature section medium of the reactor jacket, and uses the heat energy of the high temperature section medium to generate hot air for the fluidized bed through the heat energy recovery system, which not only meets the hot air drying requirements of the fluidized bed, but also reduces the temperature of the high temperature section medium to 65°C-80°C. At this time, the fluidized bed is equivalent to the first stage of cooling, and the medium coming out of the fluidized bed can be directly sent to the reactor for high temperature section cooling, or sent to the cooling tower to cool to below 32°C and then sent to the reactor for low temperature section cooling.

[0064] Taking chlorinated polymer as an example, it can also save the energy consumption of original evaporative cooling;

[0065] Minimum:

[0066] Q min =Cm△t=4.2×10 3 J / (kg*℃)×500m 3 / h×(90℃-60℃)=4.2×10 3 J / (kg*℃)×

[0067] 500×10 3 kg / h×30℃=63000MJ.

[0068] On the one hand, the heat is extracted for drying, and at the same time, the amount of circulating water used for cooling is saved. The total energy is shown in the above formula; for a 50,000 ton / year device, the amount of circulating water for heat recovery is 500m 3 / h.

[0069] The present invention has the advantages of high heat exchange efficiency, small footprint, and significant energy saving. The present invention utilizes the heat of chlorination reaction or other exothermic reaction in the drying process of subsequent products, utilizes the inherent fluidization link in the production process to achieve high-temperature medium cooling, and utilizes the heat released by the exothermic reaction as the production of fluidized drying hot air, so that the fluidized bed has both fluidized drying and cooling and heat dissipation functions, greatly reducing energy consumption. At the same time, the heat exchange area / outer volume of the tube-fin heat exchanger is ≥280m 2 / m 3 The heat exchange area is increased without increasing the volume of the heat exchanger. It is only necessary to transform the tube-fin heat exchanger in the existing blast heat exchange space of the fluidized bed, which does not increase the floor space and volume while reducing energy consumption.

[0070] Traditional heat exchangers use DN25 or DN32 tube-fin heat exchangers, which are relatively large. If steam heat exchange is used, the heat exchange area is about 1250m 2 The drying requirements can be met within DN25. When using a fin-tube heat exchanger, the heat exchange area / heat exchanger volume is 8.4m 2 / m 3 However, if hot water is used for heat exchange, the volume will be even larger and cannot meet the relevant performance requirements of fluidized bed drying, such as large wind resistance and insufficient air volume. In addition, the floor space is relatively large, the installation space is limited, and the reliability of the equipment is low.

[0071] Since the air inlet temperature of a conventional fluidized bed is relatively low, hot water heat exchangers can be used to replace all the original steam heat exchangers; of course, a portion of the original steam heat exchangers can also be retained. Hot water is pumped into the tube-fin heat exchange tube 2 through a hot water pump. The diameter of the heat exchange tube 2 of the heat exchanger of the present invention is ≤4mm, and each small heat exchange tube 2 is provided with a hydrophobic aluminum fin to increase the heat exchange area. In this way, compared with a heat exchanger with a heat exchange tube 2 diameter of 25mm or 32mm, the heat exchange area is more than doubled in the same size space, and the wind resistance is ≤300pa, which ensures the stable operation of the fluidized bed drying.

[0072] In this way, the excess reaction heat can be used in the drying process, saving the total steam consumption. According to estimates, for chlorinated polymer products, about 1 ton of steam per hour can be saved, which is equivalent to about 0.4 tons of steam per ton of product. In addition, the power consumption of the cooling tower used for cooling and the consumption of water replenishment can be saved. Together, about 0.5 tons of steam per ton of product can be saved.

[0073] The heat exchanger can be installed after the fan or before the fan.

[0074] The present invention utilizes the heat of chlorination reaction or other exothermic reaction in the drying process of subsequent products. Since the air inlet temperature of a conventional fluidized bed is relatively low, hot water heat exchangers can be used to replace all original steam heat exchangers; of course, a portion of the original steam heat exchanger can also be retained. Hot water is pumped into the heat exchange tube 2 with a diameter of ≤4mm through a hot water pump. Each small heat exchange tube 2 is provided with a hydrophobic aluminum fin to increase the heat exchange area. The specific detailed design changes can be made according to the existing temperature requirements. In this way, the heat exchange area is more than doubled in the same size space, and the wind resistance is ≤300pa, which ensures the stable operation of fluidized bed drying.

[0075] The following is the calculation of the ratio of heat exchange area to equipment volume:

[0076]

[0077] This evaluation parameter is called the heat exchanger surface density (m 2 / m 3 ), is a main parameter to characterize the compactness of the heat exchanger

[0078] According to the conventional product layout, the surface density of our heat exchanger tubes can reach 1500 (m 2 / m 3 ).

[0079] D in ----------Inner diameter

[0080] D out ----------Outer diameter

[0081] N B -----------Number of rows

[0082] N t -----------Number of single row tubes

[0083] L------------Tube length

[0084] S f -------------Fin spacing

[0085] N f ----------Number of fins

[0086] T f -------------Fin thickness

[0087] formula:

[0088] A1=π*Dout (LN f *T f )*N t *N B

[0089] A2=2[N B *S h *N t *S v -N B *N t *π(D out ) 2 / 4]*N f +2N B *S h *Tf*N f +2N t *S v *Tf*N f

[0090] A 总 =A1+A2

[0091] V=L*N B *S h *N t *S v

[0092] β=A 总 / V------------heat transfer surface density (m 2 / m 3 ) This value indicates the heat transfer compactness

[0093]

[0094]

[0095] Embodiment 2:

[0096] In the present invention, a heat recovery device based on a small-diameter dual-function heat recovery system is applicable, and includes a tube-fin heat exchanger; the tube-fin heat exchanger includes a shell 1 and a fin body 11 inside the shell 1; the fin bodies 11 are multiple and arranged adjacently; the fin bodies 11 are evenly distributed in the left and right directions inside the shell 1; the multiple fin bodies 11 and the front and rear inner walls of the shell 1 form a movable gap 12; multiple baffles 13 are fixedly connected in the movable gap 12; the baffles 13 are in sealing contact with the fin body 11, and the baffles 13 are in sealing contact with the inner wall of the shell 1; the baffles 13 in the two movable gaps 12 The shell 1 is staggered in the left and right directions; the front side of the shell 1 is connected to the air inlet joint 14; the rear side of the shell 1 is connected to the air outlet joint 15; the air inlet joint 14 and the air outlet joint 15 are arranged away from each other in the left and right directions of the shell 1; a plurality of heat exchange tubes 2 are penetrated on the left and right sides of the shell 1; a plurality of the heat exchange tubes 2 are arranged in contact with the fin body 11; the left side of the shell 1 is fixedly connected to the liquid inlet tank 3; the lower inner wall of the liquid inlet tank 3 is fixedly connected to the liquid inlet valve 31; the right side of the shell 1 is fixedly connected to the liquid outlet tank 4; the lower inner wall of the liquid outlet tank 4 is fixedly connected to the liquid outlet valve 41; one end of the heat exchange tube 2 is connected to the liquid inlet tank 3, and the other end is connected to the liquid outlet tank 4.

[0097] During operation, after the worker allows steam or hot water to enter the liquid inlet box 3 through the liquid inlet valve 31, since the liquid inlet box 3 is connected to one end of the plurality of heat exchange tubes 2, the steam or hot water enters the inner side of the plurality of heat exchange tubes 2. When the liquid inlet valve 31 starts to pass the fluid containing heat, the normal temperature air is introduced into the shell 1 by the air inlet joint 14, and the normal temperature air will enter the movable gap 12 on the front side of the fin body 11. Since the movable gap 12 is separated by a plurality of baffles 13, and the baffles 13 in the two movable gaps 12 are staggered in the left and right directions, the normal temperature air passes through the plurality of fin bodies 11 in the movable gap 12 on the front side and enters the movable gap 12 on the rear side, and the gas in the movable gap 12 on the rear side enters the movable gap 12 on the front side along the plurality of fin bodies 11 again. , the gas will pass through the fin body 11 back and forth in the shell 1 along the front and rear direction while moving toward the left. The gas will move back and forth in a winding manner, thereby extending the residence time of the gas in the shell 1, and the gas will take away the heat on the fin body 11. The heat of the fluid in the heat exchange tube 2 will transfer energy to the gas in the shell 1 through the fin body 11, so that the gas is heated up and heat exchange is achieved. The heated gas will finally be discharged along the air outlet joint 15 for utilization. As the fluid in the heat exchange tube 2 exchanges heat with the air, if one of the heat exchange tubes 2 is blocked, since multiple heat exchange tubes 2 are connected in parallel, the series connection of the traditional fin heat exchanger is abandoned, so that the fluid can flow along other unblocked heat exchange tubes 2, so that the tube-fin heat exchanger can operate normally.

[0098] It should be noted that the style or structure of the air inlet connector 14 and the air outlet connector 15 in the present invention includes but is not limited to the style or structure shown in the drawings of the present invention. It can also be a non-standard style such as a round tube type and a square tube type. In actual application, it can be customized according to the actual heat exchange capacity. Of course, the diameters of the air inlet connector 14 and the air outlet connector 15 can also be customized according to the actual air intake and outlet volumes. It is not limited to the diameter sizes of the air inlet connector 14 and the air outlet connector 15 shown in the drawings of the present invention. Furthermore, the diameter sizes of the air inlet connector 14 and the air outlet connector 15 can also be reasonably set according to the actual volume of the heat recovery device, and the present invention does not make too many restrictions here.

[0099] Embodiment 3:

[0100] The upper and lower inner walls of the liquid inlet box 3 are movably sealed and connected to the liquid inlet plate 32; the upper surface of the liquid inlet plate 32 is fixedly connected to the left rod 33; a left hole 34 is penetrated through the upper position of the inner wall of the liquid inlet box 3; the upper end of the left rod 33 passes through the left hole 34 and is fixedly connected to the movable plate 5; a gap is left between the left hole 34 and the outer wall of the left rod 33; the lower surface of the movable plate 5 is connected to the upper surface of the shell 1 by a tension spring 51.

[0101] In this embodiment, the upper and lower inner walls of the liquid outlet box 4 are movably sealed and connected to the liquid outlet plate 42; the upper surface of the liquid outlet plate 42 is fixedly connected to the right rod 43; a right hole 44 is penetrated through the upper position of the inner wall of the liquid outlet box 4; the upper end of the right rod 43 passes through the right hole 44 and is fixedly connected to the lower surface of the movable plate 5; a gap is left between the right hole 44 and the outer wall of the right rod 43; both ends of the heat exchange tubes 2 are provided with one-way valves, one end for inflow and the other end for outflow.

[0102] During operation, steam and hot water are generated by reaction, so the flow rates of steam and hot water fluctuate. When the flow rate of the fluid entering the inlet valve 31 is large, more heat exchange tubes 2 are required to ensure the heat exchange efficiency. When the flow rate of the liquid entering the inlet valve 31 is small, too many heat exchange tubes 2 will cause the fluid to fail to completely fill the heat exchange tubes 2, affecting the heat exchange effect. Therefore, the inlet plate 32 is movably sealed in the inlet box 3. After the fluid enters the inlet box 3 along the inlet valve 31 under the action of the pump, the fluid will squeeze the inlet plate 32. The greater the flow rate of the fluid entering the inlet box 3, the greater the squeezing pressure of the fluid in the inlet box 3 on the inlet plate 32, and vice versa. In this way, when the flow rate entering the inlet box 3 increases, the inlet plate 32 is pressed and moved up. After the inlet plate 32 moves up, the space of the inlet box 3 below the inlet plate 32 is connected to more heat exchange tubes 2, so that more heat exchange tubes 2 can work, so that the number of working heat exchange tubes 2 increases with the increase of the fluid flow rate, and the inlet plate During the upward movement of the liquid inlet plate 32, the gas above the liquid inlet plate 32 will be squeezed out along the left hole 34, and the fluid inside the heat exchange tube 2 above the liquid inlet plate 32 cannot flow out due to the one-way valve at the end. During the upward movement of the liquid inlet plate 32, the left rod 33 will be driven upward, and during the upward movement of the left rod 33, the movable plate 5 will be driven upward, and during the upward movement of the movable plate 5, the tension spring 51 will be pulled, so that the upward movement of the liquid inlet plate 32 and the movable plate 5 needs to overcome the tension of the tension spring 51, and during the upward movement of the movable plate 5, the right rod 43 will be driven upward, and the right rod 44 will be driven upward. 3 will drive the liquid outlet plate 42 to move upward, so that the liquid outlet plate 42 moves upward synchronously in the liquid outlet box 4 as the liquid inlet plate 32 moves upward. During the upward movement of the liquid outlet plate 42, more heat exchange tubes 2 will be activated. It is important that during the upward movement of the liquid outlet plate 42, the gas in the liquid outlet box 4 space above the liquid outlet plate 42 is discharged along the right hole 44. Under the pressure balance at both ends of the unactivated heat exchange tube 2, the fluid inside the unactivated heat exchange tube 2 is difficult to flow out, and the one-way valves at both ends of the activated heat exchange tube 2 are opened under the flow of fluid;

[0103] When the flow rate entering the liquid inlet box 3 becomes smaller, the liquid inlet plate 32 will move downward under the tension of the tension spring 51. During the downward movement of the liquid inlet plate 32, the movable plate 5 and the liquid outlet plate 42 will be driven to move downward synchronously, so that more heat exchange tubes 2 are disconnected from the flow of the liquid inlet valve 31; in summary, this embodiment connects the liquid inlet plate 32 movably up and down in the liquid inlet box 3, and connects the liquid outlet plate 42 movably in the liquid outlet box 4, so that the number of activated heat exchangers in the tube-fin heat exchanger adapts to the change of the incoming fluid volume, and then on the one hand, too few activated heat exchange tubes 2 affect the heat energy recovery efficiency, and on the other hand, it avoids the lack of fluid in the heat exchange tubes 2 affecting the heat energy recovery effect.

[0104] Embodiment 4:

[0105] The top wall of the shell 1 is penetrated by a front hole 16 and a rear hole 17; the front hole 16 is located directly above the front movable gap 12; the rear hole 17 is located directly above the rear movable gap 12; the front movable gap 12 is divided into a plurality of front gaps 121 by the baffle 13; the front movable block 52 is movably sealed in the front gap 121; the upper surface of the front movable block 52 is fixedly connected to the front rod 53; the upper end of the front rod 53 passes through the front hole 16 and is fixedly connected to the lower surface of the movable plate 5; the rear movable gap 12 is divided into a plurality of rear gaps 122 by the baffle 13; the rear movable block 54 is movably sealed in the rear gap 122; the upper surface of the rear movable block 54 is fixedly connected to the rear rod 55; the upper end of the rear rod 55 passes through the rear hole 17 and is fixedly connected to the lower surface of the movable plate 5.

[0106] In this embodiment, a plurality of spacers 18 are evenly distributed on the upper and lower inner walls of the shell 1; the material of the spacers 18 is the same as that of the fin body 11; the spacers 18 extend to the front gap 121 in the front and to the rear gap 122 in the rear; the spacers 18 separate two adjacent heat exchange tubes 2 in the upper and lower parts; the vertical thickness of the front movable block 52 and the rear movable block 54 is greater than the spacing between adjacent spacers 18; the lengths of the front rod 53, the rear rod 55, the left rod 33 and the right rod 43 are equal.

[0107] During operation, the air inlet connector 14 and the air outlet connector 15 are both arranged at the lower position of the outer wall of the shell 1, and the liquid inlet plate 32 moves up and down as the flow rate of the fluid entering the liquid inlet box 3 changes. The liquid inlet plate 32, the liquid outlet plate 42, the front movable block 52 and the rear movable block 54 are of the same height. The liquid inlet plate 32 will drive the left rod 33 to move upward during the upward movement, and the movable plate 5 will drive the front rod 53, the rear rod 55 and the right rod 43 to move upward during the upward movement of the movable plate 5, and the liquid outlet plate 42 will be driven upward during the upward movement of the right rod 43. The front movable block 52 will move upward during the upward movement of the front rod 53, and the front movable block 52 will move in the front gap 121 when it moves upward. The upward movement height of the front movable block 52 directly affects the range of the fin body 11 passed by the airflow, and the rear movable block 54 will be driven upward during the upward movement of the rear rod 55, and the rear movable block 54 will move in the rear gap The rear movable block 54 is at the same height as the front movable block 52 and moves up synchronously, and the spacing between adjacent partitions 18 is smaller than the thickness of the front movable block 52 and the rear movable block 54. Therefore, through the cooperation of the front movable block 52 and the rear movable block 54, the enabled heat exchange tube 2 in the shell 1 is separated from the surrounding space of the unenabled heat exchange tube 2, so that the gas entering the shell 1 can concentrate on the heat exchange of the fin body 11 around the enabled heat exchange tube 2, further ensuring the heat energy recovery effect; similarly, the liquid inlet plate 32 will drive the left rod 33 to move downward during the downward movement, and the movable plate 5 will be driven downward during the downward movement of the left rod 33. The movable plate 5 will drive the front movable block 52 and the rear movable block 54 to move upward during the downward movement of the movable plate 5, so as to separate the surrounding space of the enabled heat exchange tube 2 from the unenabled heat exchange tube 2 again, and the front movable block 52 and the rear movable block 54 move with the movement of the liquid inlet plate 32.

[0108] Embodiment 5:

[0109] The upper surfaces of the shell 1, the liquid inlet box 3 and the liquid outlet box 4 are flush; the upper surfaces of the shell 1, the liquid inlet box 3 and the liquid outlet box 4 are fixedly connected to the protective shell 6; the inner wall of the protective shell 6 is movably and sealedly connected to the outer wall of the movable plate 5; the movable plate 5 passes through and is movably and sealedly connected to the compensation block 56; the compensation block 56 is fixedly connected to the shell 1; the space between the lower surface of the movable plate 5 and the upper surface of the shell 1 is called the storage chamber 57; the gas in the liquid inlet box 3, the liquid outlet box 4 and the movable gap 12 can enter the storage chamber 57 for avoidance and storage.

[0110] During operation, as the inlet plate 32 moves upward, the inlet plate 32 will squeeze the gas in the inlet box 3 into the storage chamber 57 along the left hole 34. As the inlet plate 32 moves upward, the outlet plate 42 will be driven upward through the movable plate 5. As the outlet plate 42 moves upward, the gas in the outlet box 4 will be squeezed into the storage chamber 57 along the right hole 44. The front movable block 52 in the front gap 121 moves upward as the movable plate 5 moves upward. The front movable block 52 will squeeze the gas in the front gap 121 into the storage chamber 57 along the front hole 16 for temporary storage. The rear movable block 54 will squeeze the gas in the rear gap 121 into the storage chamber 57 along the front hole 16 for temporary storage. The gas in 22 is squeezed into the storage chamber 57 along the rear hole 17 for temporary storage; when the liquid inlet plate 32 moves downward, the gas in the storage chamber 57 returns to the liquid inlet box 3, the movable gap 12 and the liquid outlet box 4. In this way, through the setting of the storage chamber 57, the gas squeezed out and supplemented inside the liquid inlet box 3, the movable gap 12 and the liquid outlet box 4 can be sealed, thereby preventing the liquid inlet box 3, the movable gap 12 and the liquid outlet box 4 from being contaminated by external substances, and further preventing external gas from taking away the residual heat in the liquid inlet box 3, the movable gap 12 and the liquid outlet box 4, thereby ensuring the heat recovery effect.

[0111] In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate directions or positional relationships based on the attached Figure 4 The orientation or positional relationship shown is only for the convenience of describing the present invention and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation. Therefore, it cannot be understood as limiting the scope of protection of the present invention. In addition, the terms "first", "second", "third", etc. are only used to distinguish the description and cannot be understood as indicating or implying relative importance.

[0112] The above shows and describes the basic principles, main features and advantages of the present invention. It should be understood by those skilled in the art that the present invention is not limited to the above embodiments. The above embodiments and descriptions are only for explaining the principles of the present invention. Without departing from the spirit and scope of the present invention, the present invention may have various changes and improvements, which fall within the scope of the present invention. The scope of protection of the present invention is defined by the attached claims and their equivalents.

Claims

1. A heat recovery system based on small-diameter dual-function, characterized in that: It includes an insulated medium storage tank, multiple heat exchange blasting spaces, each heat exchange blasting space has its own tube-fin heat exchanger; the diameter of the heat exchange tube in the tube-fin heat exchanger is ≤4mm; each tube-fin heat exchanger has its own liquid inlet valve and liquid outlet valve, and a liquid inlet pump is arranged at the output end of the medium storage tank, and the liquid inlet pump is connected to each liquid inlet valve by a branch pipeline; the heat exchange area / outer volume of each tube-fin heat exchanger is ≥280m2 / m3; the air flow inlet of each heat exchange blasting space is connected to its own blower, and the air temperature output from the heat exchange blasting space is 65℃-85℃; the medium storage tank has at least one first medium inlet that allows heat transfer medium with a temperature higher than 95℃ to be input therein; Wherein, the tube-fin heat exchanger comprises a shell and a fin body inside the shell; the fin bodies are multiple and arranged adjacently; the fin bodies are evenly distributed in the left and right directions of the inner side of the shell; the multiple fin bodies form a movable gap with the front and rear inner walls of the shell; multiple baffles are fixedly connected in the movable gap; the baffles are in sealing contact with the fin bodies, and the baffles are in sealing contact with the inner wall of the shell; the baffles in the two movable gaps are staggered in the left and right directions; the front side of the shell is connected to the air inlet joint; the rear side of the shell is connected to the air outlet joint; the air inlet joint and the air outlet joint are arranged away from each other in the left and right directions of the shell; multiple heat exchange tubes are penetrated on the left and right sides of the shell; multiple heat exchange tubes are arranged in contact with the fin bodies; the left side of the shell is fixedly connected to the liquid inlet box; the lower inner wall of the liquid inlet box is fixedly connected to the liquid inlet valve; the right side of the shell is fixedly connected to the liquid outlet box; the lower inner wall of the liquid outlet box is fixedly connected to the liquid outlet valve; one end of the heat exchange tube is connected to the liquid inlet box, and the other end is connected to the liquid outlet box.

2. The heat recovery system based on small-diameter dual-function according to claim 1 is characterized in that: The medium storage tank has at least one second medium inlet that allows heat transfer medium below 80°C to be input therein, and the medium output by each liquid outlet valve is input into the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve; or, the medium output by each liquid outlet valve is input into the second medium inlet of the medium storage tank via a reflux pipe and a reflux valve after passing through a cooling tower.

3. A heat recovery device based on small diameter dual functions, which is applicable to the heat recovery system based on small diameter dual functions as claimed in claim 1, characterized in that: The device comprises a tube-fin heat exchanger, wherein the upper and lower inner walls of a liquid inlet box in the tube-fin heat exchanger are movably sealed and connected to a liquid inlet plate; the upper surface of the liquid inlet plate is fixedly connected to a left rod; a left hole is penetrated through the upper position of the inner wall of the liquid inlet box; the upper end of the left rod passes through the left hole and is fixedly connected to a movable plate; a gap is left between the left hole and the outer wall of the left rod; the lower surface of the movable plate is connected to the upper surface of the shell by a tension spring.

4. The heat recovery device based on small-diameter dual-function according to claim 3 is characterized in that: The upper and lower inner walls of the liquid outlet box are movably sealed to connect the liquid outlet plate; the upper surface of the liquid outlet plate is fixedly connected to the right rod; a right hole is provided through the upper position of the inner wall of the liquid outlet box; the upper end of the right rod passes through the right hole and is fixedly connected to the lower surface of the movable plate; a gap is left between the right hole and the outer wall of the right rod; both ends of the heat exchange tubes are provided with one-way valves, with inflow at one end and outflow at the other end.

5. The heat recovery device based on small-diameter dual-function according to claim 4 is characterized in that: The top wall of the shell is penetrated by a front hole and a rear hole; the front hole is located directly above the front movable gap; the rear hole is located directly above the rear movable gap; the front movable gap is divided into multiple front gaps by a baffle; the movable seal in the front gap is connected to the front movable block; the upper surface of the front movable block is fixedly connected to the front rod; the upper end of the front rod passes through the front hole and is fixedly connected to the lower surface of the movable plate; the rear movable gap is divided into multiple rear gaps by a baffle; the movable seal in the rear gap is connected to the rear movable block; the upper surface of the rear movable block is fixedly connected to the rear rod; the upper end of the rear rod passes through the rear hole and is fixedly connected to the lower surface of the movable plate.

6. The heat recovery device based on small-diameter dual-function according to claim 5 is characterized in that: A plurality of spacers are evenly distributed on the upper and lower inner walls of the shell; the material of the spacers is the same as that of the fin body; the spacers extend to the front gap in the front and to the rear gap in the rear; the spacers separate two adjacent heat exchange tubes in the upper and lower parts; the vertical thickness of the front movable block and the rear movable block is greater than the distance between adjacent spacers; the lengths of the front rod, the rear rod, the left rod and the right rod are equal.

7. The heat recovery device based on small-diameter dual-function according to claim 6 is characterized in that: The upper surfaces of the shell, the liquid inlet box and the liquid outlet box are flush; the upper surfaces of the shell, the liquid inlet box and the liquid outlet box are fixedly connected to the protective shell; the inner wall of the protective shell is movably and sealedly connected to the outer wall of the movable plate; the movable plate passes through the upper and lower parts and is movably and sealedly connected to the compensation block; the compensation block is fixedly connected to the shell; the space between the lower surface of the movable plate and the upper surface of the shell is called a storage chamber; The gas in the liquid inlet box, the liquid outlet box and the movable gap can enter the storage cavity for avoidance and storage.

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