CN219037695U - Winding tube heat exchange device and its continuous reforming process system, hydrogenation heat exchange process system - Google Patents

Abstract

The utility model discloses a heat exchange device around a tube, its continuous reforming process system, and a heat exchange process system for hydrogenation, and relates to the technical field of heat exchangers. The outer shell of the upper part and the heat exchange tubes arranged between the central tube and the outer shell. The heat exchange tubes are alternately wound along the outer side of the central tube and arranged regularly in the shape of a spiral disk in the outer shell, and the winding of two adjacent layers of heat exchange tubes In the opposite direction, the top of the outer casing is provided with a raw material outlet, the bottom is provided with a raw material inlet, the top of one side of the outer casing is provided with a product inlet, and the bottom of the other side is provided with a product outlet. The coiled tube heat exchange device provided by the utility model is safe and reliable in use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange efficiency of the heat exchanger in the heat exchange process system. Effect.

Description

Wound tube heat exchange device and its continuous reforming process system, hydrogenation heat exchange process system

technical field

The utility model relates to the technical field of heat exchangers, in particular to a tube-wound heat exchange device. In addition, it also relates to a continuous reforming process system and a hydrogenation heat exchange process system comprising the above-mentioned coiled tube heat exchange device.

Background technique

In the prior art, the heat exchanger in the heat exchange system generally adopts a plate-shell heat exchanger or a tube-and-tube vertical heat exchanger. Among them, the plate and shell heat exchanger is mainly composed of three parts: welded heat exchange tube bundle, pressure vessel shell and tube box. The heat exchange tube bundle is made of hundreds of 2mm stainless steel sheets stacked and welded and sealed around the periphery. The tube and tube vertical heat exchanger is mainly composed of the upper tube box, the upper fixed tube plate, the shell (with a pair of high-temperature flanges), the tube bundle, the outer head cover and the outer floating head (with expansion joints and distributors) and other components.

Due to the small thickness of the plate and shell heat exchanger, there are disadvantages such as easy damage and poor reliability, which increase the production cost and maintenance cost of the device. Moreover, the plate heat exchanger has poor sealing performance and is easy to leak. The gasket needs to be replaced frequently, which affects the operation, and because the sealing ring has great restrictions on the use conditions, if the operating temperature and operating pressure fluctuate during the production process, it is easy to cause damage to the sealing ring. , resulting in unplanned shutdown of the device and increased costs.

The tube-and-tube vertical heat exchanger has a pair of high-temperature flanges on the shell. Once the high-temperature flange leaks, it is necessary to extract a tube bundle tens of meters long, which makes it very difficult to replace the gasket. For large-scale reforming units , It often requires two or more heat exchangers to be connected in parallel, and problems such as bias current may occur during use. In the process of water flow, a local stagnation area (cold water area) will be formed, the heat exchange is insufficient, the water temperature rises slowly, and the heat exchange efficiency is low, resulting in a large temperature difference at the hot end of the heat exchanger, less heat recovered, and operating costs higher. If problems such as corrosion and liquid leakage occur, the traditional solution is to replace the cracked or perforated plates, but the cost of replacing the plates is relatively high.

To sum up, how to improve the heat exchange effect of the heat exchanger in the heat exchange system is an urgent problem to be solved by those skilled in the art.

Utility model content

In view of this, the purpose of this utility model is to provide a coiled tube heat exchange device, which is safe and reliable in use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange process system. The heat transfer effect of the heat exchanger.

Another object of the present invention is to provide a continuous reforming process system and a hydrogenation heat exchange process system comprising the above-mentioned coiled heat exchange device.

In order to achieve the above object, the utility model provides the following technical solutions:

A tube-wound heat exchange device, comprising: a central cylinder, an outer casing sheathed on the outer periphery of the central cylinder, and a heat exchange tube arranged between the central cylinder and the outer casing, and the heat exchange tube is arranged along the The outer sides of the central tube are alternately wound, and are regularly arranged in the shape of a spiral disk in the outer shell, and the winding directions of the heat exchange tubes in two adjacent layers are opposite. The top of the outer shell is provided with a raw material outlet, and the bottom is provided with a Raw material inlet, a product inlet is provided at the top of one side of the outer casing, and a product outlet is provided at the bottom of the other side.

Preferably, a plurality of spacers are arranged vertically at equal intervals along the radial direction of the central tube, and the spacers are provided with at least two arc-shaped grooves at equal intervals along the height direction for accommodating the heat exchange tubes .

Preferably, the heat exchange tubes are distributed in an equilateral triangle on the tube sheet of the outer casing.

Preferably, the heat exchange tube and the tube sheet are welded with deep holes.

Preferably, the product inlet is provided with an anti-scouring plate, and the anti-scouring plate is used to prevent fluid from directly scouring the heat exchange tubes.

Preferably, the raw material outlet, the raw material inlet, the product inlet and the product outlet are all equipped with parking flushing devices, and the product inlet and the product outlet are all equipped with online flushing devices.

A continuous reforming process system, comprising: a feed buffer tank, a feed pump, a feed filter, a heat exchanger, a cycle machine, a first heating furnace, a first reactor, a second heating furnace, and a second reactor , a third heating furnace, a third reactor, a separation tank and a discharge pump, the heat exchanger is the coil heat exchange device described in any one of the above;

The feed buffer tank, the feed pump, the feed filter and the raw material inlet of the heat exchanger are connected in sequence, the raw material outlet of the heat exchanger, the first heating furnace, the second A reactor, the second heating furnace, the second reactor, the third heating furnace and the third reactor are connected in sequence, the outlet of the third reactor and the product of the heat exchanger The inlet is connected, the product outlet of the heat exchanger is connected to the inlet of the separator, a certain outlet of the separator, the cycler and the raw material inlet are connected in sequence, and the other outlet of the separator is connected to the Collection device connection for collecting product.

A hydrogenation heat exchange process system, comprising a first pipeline for transporting hydrogenation dilute material, a second pipeline for transporting the first hydrogenation feed, a third pipeline for transporting circulating hydrogen, and a The fourth pipeline for transporting the first hydrogenation output, the fifth pipeline for transporting the second hydrogenation feed, the sixth pipeline for transporting the second hydrogenation output, the fourth heating furnace and heat exchange device, the heat exchanger is the coiled tube heat exchange device described in any one of the above;

The heat medium channel inlet of the heat exchanger is used to accept the output end product of the hydrogenation reactor, the heat medium channel outlet is connected to downstream equipment, the first pipeline, the second pipeline and the first The outlets of the three pipelines are all connected to the inlet of the cold medium channel of the heat exchanger, and the outlet of the cold medium channel is connected to the input end of the heating furnace.

Preferably, the heat medium channel is the tube side of the heat exchanger, and the cold medium channel is the shell side of the heat exchanger;

Or the heat medium channel is the shell side of the heat exchanger, and the cold medium channel is the tube side of the heat exchanger.

Preferably, the heat exchanger is placed vertically, the heat medium channel is located at the side of the heat exchanger, and the cold medium channel is located at the end of the heat exchanger.

When using the coiled tube heat exchange device provided by the utility model, when the device needs to be used in a certain heat exchange process system, the raw material outlet, raw material inlet, product inlet and product outlet can be respectively connected correspondingly. Since the heat exchange tubes are alternately wound in a spiral shape in the space between the central cylinder and the outer shell, and the winding directions of the adjacent two layers of heat exchange tubes are opposite, it is equivalent to setting countless expansion joints inside the outer shell. When subjected to high temperature, it can expand and contract almost freely, and the temperature difference stress of the tube head of the heat exchange tube is small, which is suitable for working conditions with relatively large temperature difference. This device does not have high requirements for the temperature rise of the start-up, and it can also well deal with the unexpected situation of sudden stop. That is to say, the coiled tube heat exchange device provided by this application is safe and reliable to use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange effect of the heat exchanger in the heat exchange process system.

In summary, the coiled tube heat exchange device provided by the utility model is safe and reliable in use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange rate in the heat exchange process system. The heat transfer effect of the heater.

In addition, the utility model also provides a continuous reforming process system and a hydrogenation heat exchange process system comprising the above-mentioned coiled tube heat exchange device.

Description of drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the accompanying drawings that need to be used in the description of the embodiments or the prior art. Obviously, the accompanying drawings in the following description It is only an embodiment of the utility model, and those skilled in the art can also obtain other drawings according to the provided drawings without creative work.

Fig. 1 is a structural schematic diagram of a coiled tube heat exchange device provided by the utility model;

Fig. 2 is a cross-sectional view of a coiled tube heat exchange device;

Figure 3 is a schematic diagram of the pipe layout of the heat exchanger;

Figure 4 is a schematic diagram of the connection between the tube sheet and the heat exchange tubes;

Fig. 5 is a partial enlarged view of I place of Fig. 4;

Fig. 6 is the structural representation of spacer;

Fig. 7 is the continuous reforming process system provided by the utility model;

Fig. 8 is the hydrogenation heat exchange process system provided by the utility model.

In Figure 1-Figure 8:

1 is the heat exchanger, 101 is the central cylinder, 102 is the outer casing, 103 is the heat exchange tube, 104 is the raw material outlet, 105 is the raw material inlet, 106 is the product inlet, 107 is the product outlet, 108 is the distance piece, 109 is the Tube plate, 1010 is the anti-shock plate, 1011 is the parking flushing device, 1012 is the online flushing device, 2 is the feed buffer tank, 3 is the feed pump, 4 is the circulation machine, 5 is the first heating furnace, 6 is the first Reactor, 7 is the second heating furnace, 8 is the second reactor, 9 is the third heating furnace, 10 is the third reactor, 11 is the separator, 12 is the discharge pump, 13 is the first pipeline, 14 15 is the third pipeline, 16 is the fourth pipeline, 17 is the fifth pipeline, 18 is the sixth pipeline, and 19 is the fourth heating furnace.

Detailed ways

The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of them. example. Based on the embodiments of the present utility model, all other embodiments obtained by persons of ordinary skill in the art without making creative efforts belong to the scope of protection of the present utility model.

The core of the utility model is to provide a coiled tube heat exchange device, which is safe and reliable in use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the performance of heat exchangers in heat exchange process systems. heat transfer effect. Another core of the utility model is to provide a continuous reforming process system and a hydrogenation heat exchange process system including the above-mentioned coiled heat exchange device.

Please refer to Figure 1 to Figure 8.

This specific embodiment provides a tube-wound heat exchange device, including: a central cylinder 101, an outer casing 102 sleeved on the outer periphery of the central cylinder 101, and a heat exchange tube 103 arranged between the central cylinder 101 and the outer casing 102, The heat exchange tubes 103 are alternately wound along the outer side of the central cylinder 101, and are regularly arranged in the shape of a spiral disk in the outer shell 102, and the winding directions of two adjacent layers of heat exchange tubes 103 are opposite. The top of the outer shell 102 is provided with a raw material outlet 104, A raw material inlet 105 is provided at the bottom, a product inlet 106 is provided at the top of one side of the shell 102 , and a product outlet 107 is provided at the bottom of the other side.

It should be noted that by transforming the original heat exchanger 1 into a coiled tube heat exchanger 1, according to the experimental data, the temperature difference at the hot end of the heat exchanger 1 is reduced from 54°C to 43°C, which saves a lot of fuel costs, and , the temperature of the final product passing through heat exchanger 1 rises from 41°C to 52°C, which reduces the load on the furnace in the next system, saves 0.09t of fuel gas per hour, and reduces the consumption of circulating water and demineralized water in the device.

The shape, structure, size, material, etc. of the central cylinder 101, the outer shell 102, and the heat exchange tube 103 can be determined according to the actual situation and actual needs during actual operation.

When using the coiled tube heat exchange device provided by the utility model, when the device needs to be used in a certain heat exchange process system, the raw material outlet 104, the raw material inlet 105, the product inlet 106 and the product outlet 107 can be connected correspondingly . Since the heat exchange tubes 103 are alternately wound in a spiral shape in the space between the central cylinder 101 and the outer shell 102, and the winding directions of the adjacent two layers of heat exchange tubes 103 are opposite, it is equivalent to setting countless expansion tubes inside the outer shell 102. The heat exchange tube 103 can expand and contract almost freely when subjected to high temperature, and the heat exchange tube 103 has a small temperature difference stress at the tube head, which is suitable for working conditions with a relatively large temperature difference. This device does not have high requirements for the temperature rise of the start-up, and it can also well deal with the unexpected situation of sudden stop. That is to say, the coiled tube heat exchange device provided by this application is safe and reliable to use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange effect of heat exchanger 1 in the heat exchange process system .

In summary, the coiled tube heat exchange device provided by the utility model is safe and reliable in use, has excellent heat transfer performance, and has the characteristics of high temperature resistance, high pressure resistance, and fluctuation resistance, which can improve the heat exchange rate in the heat exchange process system. The heat transfer effect of Heater 1.

On the basis of the above-mentioned embodiments, preferably, a plurality of spacers 108 are vertically arranged at equal intervals along the radial direction of the central cylinder 101, and at least two spacers 108 are arranged at equal intervals along the height direction for accommodating heat exchange. The arc-shaped grooves of the tubes 103 are used to maintain a preset distance between two adjacent layers of heat exchange tubes 103 and between upper and lower heat exchange tubes 103 of the same layer. For example, the preset distance can be set to 22mm, so as to arrange more heat exchange tubes 103 and reduce the structural size.

Preferably, the heat exchange tubes 103 are distributed in an equilateral triangle on the tube sheet 109 of the outer casing 102 .

It should be noted that the tube sheet 109 is arranged in an equilateral triangle, and the largest number of heat exchange tubes 103 can be arranged on the same area of the tube sheet 109, so that the arrangement of the heat exchange tubes 103 is compact, and the fluid passing through the outer shell 102 can be directly flushed and exchanged. The heat pipe 103 makes the shell-side fluid distribution more uniform.

Preferably, the heat exchange tube 103 and the tube sheet 109 are welded with deep holes. The parts of the device are connected by full welding to ensure zero leakage when the device performs heat exchange operation, which is safe and reliable. Moreover, the high temperature end of the tube sheet 109 is likely to generate carbon ions to gather and burst the heat exchange tubes 103 , but the above problems can be effectively avoided by adopting deep hole welding.

On the basis of the above embodiments, preferably, the product inlet 106 is provided with an anti-scouring plate 1010, and the anti-scouring plate 1010 is used to prevent the fluid from directly scouring the heat exchange tube 103, that is, the anti-scour plate 1010 can effectively prevent the fluid from directly scouring the heat exchange The vibration instability and corrosion of the heat exchange tube 103 caused by the tube 103.

Preferably, the raw material outlet 104 , the raw material inlet 105 , the product inlet 106 and the product outlet 107 are all equipped with a parking flushing device 1011 , and the product inlet 106 and the product outlet 107 are all equipped with an online flushing device 1012 . During the use of the device, the product inlet 106 and the product outlet 107 can be flushed through the online flushing device 1012. After the device is used, the raw material outlet 104, the raw material inlet 105, and the product inlet can be flushed through the parking flushing device 1011. 106 and product outlet 107 for flushing operation.

In addition to the above-mentioned coiled heat exchange device, the utility model also provides a continuous reforming process system comprising the coiled tube heat exchange device disclosed in the above embodiment, which includes: a feed buffer tank 2, a feed pump 3, a feed Filter, heat exchanger 1, cycler 4, first heating furnace 5, first reactor 6, second heating furnace 7, second reactor 8, third heating furnace 9, third reactor 10, separation tank And the discharge pump 12, the heat exchanger 1 is any one of the above coil heat exchange devices;

The feed buffer tank 2, the feed pump 3, the feed filter and the raw material inlet 105 of the heat exchanger 1 are connected in sequence, the raw material outlet 104 of the heat exchanger 1, the first heating furnace 5, the first reactor 6, the second The heating furnace 7, the second reactor 8, the third heating furnace 9 and the third reactor 10 are connected in sequence, the outlet of the third reactor 10 is connected with the product inlet 106 of the heat exchanger 1, and the product outlet 107 of the heat exchanger 1 It is connected with the inlet of the separator 11, an outlet of the separator 11, the circulator 4 and the raw material inlet 105 are connected in sequence, and the other outlet of the separator 11 is connected with a collection device for collecting products. For the structure of other parts of the continuous reforming process system, please refer to the prior art, which will not be repeated here.

It should be noted that the mixed material from the previous system can first enter the feed buffer tank 2, and after being lifted by the feed pump 3, the particulate matter in the material can be removed in the feed filter. After the circulating hydrogen is mixed, the first feed material with a shell-side inlet temperature of 95°C is obtained, and after heat exchange by heat exchanger 1, the first discharge material with a shell-side outlet temperature of 64°C is obtained, and the first discharge material enters the first heating in turn After the furnace 5, the first reactor 6, the second heating furnace 7, the second reactor 8, the third heating furnace 9, and the third reactor 10 are reacted, a new product with a temperature of 29° C. is obtained, which is used as the second The feed material flows into the tube side of the heat exchanger 1, and after heat exchange by the heat exchanger 1, the second discharge material with a temperature of 52°C at the outlet of the tube side is obtained. It enters the circulator 4 from the top of the separation tank, returns to the heat exchanger 1 to continue the reaction after being compressed, and the remaining gas is discharged into the collection device as a product.

In addition to the above coiled tube heat exchange device, the utility model also provides a hydrogenation heat exchange process system comprising the coiled tube heat exchange device disclosed in the above embodiment, which includes a first pipeline 13 for transporting hydrogenation dilute material, The second pipeline 14 for transporting the first hydrogenation feed, the third pipeline 15 for transporting recycled hydrogen, the fourth pipeline 16 for transporting the first hydrogenation output, and the fourth pipeline 16 for transporting the second hydrogenation The fifth pipeline 17 for hydrogen feed, the sixth pipeline 18 for transporting the second hydrogenation output, the fourth heating furnace 19 and the heat exchanger 1, the heat exchanger 1 is a coiled tube exchange of any one of the above-mentioned heating device;

The heat medium channel inlet of the heat exchanger 1 is used to accept the output end product of the hydrogenation reactor, and the heat medium channel outlet is connected to downstream equipment, and the outlets of the first pipeline 13, the second pipeline 14 and the third pipeline 15 are all It is connected with the inlet of the cold medium channel of the heat exchanger 1, and the outlet of the cold medium channel is connected with the input end of the heating furnace. For the structure of other parts of the hydrogenation heat exchange process system, please refer to the prior art, which will not be repeated here.

It should be noted that the technologies for reducing the sulfur content of diesel oil mainly include hydrodesulfurization, oxidative extraction, biological desulfurization, and adsorption desulfurization, etc. Among them, diesel hydrogenation is the main and effective technology for producing ultra-low sulfur diesel in the prior art. Hydrotreating refers to the conversion of harmful impurities such as sulfur, oxygen, and nitrogen in oil into corresponding hydrogen sulfide, water, and ammonia in the presence of hydrogen partial pressure and catalysts, and hydrogenation of olefins and diolefins. Aromatics are partially hydrogenated and saturated to improve the quality of oil products.

The process of hydrogenation treatment is as follows: the oil product is mixed with hydrogen-containing gas and sent to a heating furnace to be heated to a specified temperature, and then enters a reactor equipped with a catalyst; after the reaction product is cooled, it enters a high-pressure separator 11 for gas-liquid separation. The gas phase part of the reaction product is recycled by the compressor, and the liquid phase part of the reaction product is separated under reduced pressure and then enters the product fractionation system to realize the conversion of the product. In addition, due to the harsh operating conditions of the equipment used in the hydrogenation process, most of them are high-temperature and high-pressure equipment, and the conventional heat exchanger 1 is difficult to produce on a large scale. The device can effectively improve the heat exchange effect of the hydrogenation process.

On the basis of the above embodiments, preferably, the heat medium channel is the tube side of the heat exchanger 1, and the cold medium channel is the shell side of the heat exchanger 1; or the heat medium channel is the shell side of the heat exchanger 1, and the cold medium channel is the shell side of the heat exchanger 1. The channel is the tube side of heat exchanger 1. That is, the hot medium passage and the cold medium passage can be determined according to actual conditions and actual needs.

Preferably, the heat exchanger 1 is placed vertically, the heat medium channel is located at the side of the heat exchanger 1 , and the cold medium channel is located at the end of the heat exchanger 1 . Placing the heat exchanger 1 vertically can greatly reduce the footprint of the equipment.

In order to further illustrate the use process of the hydrogenation heat exchange process system provided by the utility model, an example is given below.

The mixture of hydrogenation dilute feedstock, first hydrogenation feed and circulating hydrogen can be input into the cold medium channel of heat exchanger 1, the temperature of the mixture is 90-96°C, and the temperature of the mixture coming out of the cold medium channel of heat exchanger 1 is 317-353°C; the mixture coming out of the cold medium channel of heat exchanger 1 passes through the heating furnace and the hydrogenation reactor in turn, and then is output from the hydrogenation reactor. The temperature of the first hydrogenation output is 379-410°C. The product passes through the heat medium channel of the heat exchanger 1, and the temperature of the second hydrogenation output from the heat medium channel of the heat exchanger 1 is lowered to 155.7-157.1°C, and enters the downstream equipment.

The advantage of this process system is that the heat exchanger 1 is designed as a coiled tube heat exchange device with a hot medium channel and a cold medium channel. By winding the heat exchange tubes 103, the heat exchange area of a single device is increased in a limited space. Such setting can reduce the number of heat exchangers 1, thereby reducing equipment footprint, frame investment, high-pressure pipeline consumption, piping work and equipment maintenance costs, etc.; 1. The first hydrogenation discharge material is heat exchanged in the heat exchanger 1, which improves the thermal efficiency of the heat exchanger 1, also increases the temperature of the material entering the heating furnace, and reduces the temperature of the reaction product entering the downstream equipment, thereby reducing the heating rate. The load of the furnace and downstream equipment, while simplifying the process, and ensuring that the heat exchange system can run for a longer period; at the same time, the structure of the system is simple and easy to operate.

It should be noted that the first heating furnace 5, the second heating furnace 7, the third heating furnace 9, the fourth heating furnace 19, the first reactor 6, the second reactor 8 and the first heating furnace mentioned in this application document Three reactors 10, the first pipeline 13 and the second pipeline 14 and the third pipeline 15 and the fourth pipeline 16 and the fifth pipeline 17 and the sixth pipeline 18, wherein, the first and the second and the The third, the fourth, the fifth and the sixth are just to distinguish the different positions, and there is no order.

In addition, it should also be noted that the orientation or positional relationship indicated by "in and out" in this application is based on the orientation or positional relationship shown in the drawings, and is only for the purpose of simplifying description and understanding, rather than indicating or implying Means that a device or element must have a specific orientation, be constructed and operate in a specific orientation, and therefore should not be construed as limiting the invention.

Each embodiment in this specification is described in a progressive manner, each embodiment focuses on the difference from other embodiments, and the same and similar parts of each embodiment can be referred to each other. Any combination of all the embodiments provided by the utility model is within the protection scope of the utility model, and will not be repeated here.

Above, the coiled tube heat exchange device and its continuous reforming process system and hydrogenation heat exchange process system provided by the utility model have been introduced in detail. In this paper, specific examples are used to illustrate the principle and implementation of the present utility model, and the descriptions of the above embodiments are only used to help understand the method and core idea of the present utility model. It should be pointed out that for those of ordinary skill in the art, without departing from the principle of the utility model, some improvements and modifications can also be made to the utility model, and these improvements and modifications also fall into the protection of the claims of the utility model. within range.

Claims (10)

1. A tube-wound heat exchange device, characterized in that it comprises: a central cylinder (101), an outer casing (102) sleeved on the outer periphery of the central cylinder (101), and an outer casing (102) disposed on the central cylinder (101) and the heat exchange tubes (103) between the outer shell (102), the heat exchange tubes (103) are alternately wound along the outer side of the central cylinder (101), and spiral in the outer shell (102) Discs are regularly arranged, and the winding directions of the heat exchange tubes (103) in two adjacent layers are opposite. The top of the outer casing (102) is provided with a raw material outlet (104), and the bottom is provided with a raw material inlet (105). A product inlet (106) is provided at the top of one side of the outer housing (102), and a product outlet (107) is provided at the bottom of the other side. 2. The tube-wound heat exchange device according to claim 1, characterized in that, a plurality of spacers (108) are arranged vertically and equidistantly along the radial direction of the central cylinder (101), and the distance pieces (108) (108) At least two arc-shaped grooves for accommodating the heat exchange tubes (103) are arranged at equal intervals along the height direction. 3. The tube-wound heat exchange device according to claim 1, characterized in that, the heat exchange tubes (103) are distributed in an equilateral triangle on the tube plate (109) of the outer casing (102). 4. The coiled tube heat exchange device according to claim 3, characterized in that, deep hole welding is used between the heat exchange tube (103) and the tube sheet (109). 5. The coiled tube heat exchange device according to any one of claims 1 to 4, characterized in that, the product inlet (106) is provided with an anti-shock plate (1010), and the anti-shock plate (1010) is used for Prevent the fluid from directly washing the heat exchange tube (103). 6. The coiled tube heat exchange device according to any one of claims 1 to 4, characterized in that, the raw material outlet (104), the raw material inlet (105), the product inlet (106) and the Both the product outlets (107) are equipped with parking flushing devices (1011), and the product inlets (106) and the product outlets (107) are both equipped with online flushing devices (1012). 7. A continuous reforming process system is characterized in that, comprising: feed buffer tank (2), feed pump (3), feed filter, heat exchanger (1), circulator (4), the first A heating furnace (5), the first reactor (6), the second heating furnace (7), the second reactor (8), the third heating furnace (9), the third reactor (10), the separation tank and A discharge pump (12), the heat exchanger (1) is the coiled tube heat exchange device described in any one of claims 1-6; The feed buffer tank (2), the feed pump (3), the feed filter and the raw material inlet (105) of the heat exchanger (1) are connected in sequence, and the heat exchanger (1 ), the first heating furnace (5), the first reactor (6), the second heating furnace (7), the second reactor (8), the The third heating furnace (9) and the third reactor (10) are connected in sequence, the outlet of the third reactor (10) is connected to the product inlet (106) of the heat exchanger (1), and the The product outlet (107) of the heat exchanger (1) is connected to the inlet of the separator (11), and a certain outlet of the separator (11), the cycler (4) and the raw material inlet (105) are sequentially Connected, another outlet of the separator (11) is connected with a collecting device for collecting the product. 8. A hydrogenation heat exchange process system, characterized in that it comprises a first pipeline (13) for transporting hydrogenation dilute material, a second pipeline (14) for transporting the first hydrogenation feed, The third pipeline (15) for conveying the recycled hydrogen, the fourth pipeline (16) for conveying the first hydrogenation output, the fifth pipeline (17) for conveying the second hydrogenation feed, and the In the sixth pipeline (18), the fourth heating furnace (19) and the heat exchanger (1) for conveying the second hydrogenation discharge, the heat exchanger (1) is any one of the above-mentioned claims 1-6 The coiled tube heat exchange device; The heat medium channel inlet of the heat exchanger (1) is used to receive the output end product of the hydrogenation reactor, the heat medium channel outlet is connected to downstream equipment, the first pipeline (13), the second Both the outlet of the pipeline (14) and the third pipeline (15) are connected to the inlet of the cold medium passage of the heat exchanger (1), and the outlet of the cold medium passage is connected to the input end of the heating furnace. 9. The hydrogenation heat exchange process system according to claim 8, characterized in that, the heat medium passage is the tube side of the heat exchanger (1), and the cold medium passage is the heat exchanger ( 1) the shell side; Or the heat medium channel is the shell side of the heat exchanger (1), and the cold medium channel is the tube side of the heat exchanger (1). 10. The hydrogenation heat exchange process system according to claim 9, characterized in that, the heat exchanger (1) is placed vertically, and the heat medium channel is located on the side of the heat exchanger (1) , the cold medium channel is located at the end of the heat exchanger (1).

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