CN217179351U - Anti-clogging tubular heat exchanger - Google Patents

Abstract

The utility model relates to an anti-blocking tubular heat exchanger, which comprises a tank body, a heat exchange tube mechanism and an organic solvent spraying device; the heat exchange tube mechanism is arranged in the tank body and comprises an upper tube plate and a lower tube plate which are arranged at intervals, and a plurality of heat exchange tubes arranged between the upper tube plate and the lower tube plate, the upper tube plate and the lower tube plate divide the tank body into a heat exchange cavity in the middle, an upper end enclosure cavity in the upper part and a lower end enclosure cavity in the lower part, and the plurality of heat exchange tubes are communicated with the upper end enclosure cavity and the lower end enclosure cavity; the organic solvent spraying device is arranged in the upper seal head cavity and used for spraying organic solvent into the heat exchange tubes. The utility model provides a prevent blockking up tubulation heat exchanger when high temperature raw coal gas carries out heat recovery and crude oil separation, sprays organic solvent through organic solvent spray set in to the heat exchange tube, can dissolve the heavy oil component of condensation wall built-up coalescence on the heat exchange tube pipe wall to can reduce heat exchanger dirt coefficient, promote heat exchanger heat transfer efficiency.

Description

Anti-clogging tubular heat exchanger

Technical Field

The utility model relates to a heat exchanger technical field, more specifically relates to a prevent blockking up shell and tube heat exchanger.

Background

In the existing coal chemical industry technology, a tubular heat exchanger is usually adopted for heat recovery, which can preheat the high temperature in the high temperature crude gas for recycling and can condense and separate out the oil product in the crude gas for separation.

In the existing coal hydro-gasification process technology, crude coal gas mostly contains heavy-mass component aromatic hydrocarbons such as benzene, pyrene, naphthalene, fluorene, anthracene green and the like, and is subjected to multistage heat exchange in a heat recovery and crude oil separation section according to dew point condensation temperatures of different components so as to be separated from the crude coal gas. In the multistage heat exchanger adopted in the prior art, when the crude gas contains oil and is cooled on the wall of a heat exchange pipe, part of heavy oil components in the crude gas are condensed and wall-hung to coalesce, so that the fouling coefficient of the heat exchanger is increased, the heat exchange effect is reduced, the heavy oil components are accumulated and increased in long-period operation, and the heat exchange tubes can be blocked seriously, so that the failure of the heat exchange tubes is caused, the outlet of the heat exchanger is over-temperature, and the safe and stable operation of the whole system is influenced.

SUMMERY OF THE UTILITY MODEL

In view of this, the utility model aims at providing a prevent blockking up tubular heat exchanger to in solving current coal chemical industry technical heat recovery and crude oil separation process, tubular heat exchanger's tubular pipe wall produces the dirt easily and blocks up even, influences the heat transfer effect and causes the technical problem that the heat exchanger became invalid even.

According to the utility model, the anti-blocking tubular heat exchanger comprises a tank body, a heat exchange tube mechanism and an organic solvent spraying device; wherein the content of the first and second substances,

the heat exchange tube mechanism is arranged in the tank body and comprises an upper tube plate and a lower tube plate which are arranged at intervals, and a plurality of heat exchange tubes arranged between the upper tube plate and the lower tube plate, the upper tube plate and the lower tube plate divide the tank body into a heat exchange cavity at the middle part, an upper end enclosure cavity at the upper part and a lower end enclosure cavity at the lower part, and the plurality of heat exchange tubes are communicated with the upper end enclosure cavity and the lower end enclosure cavity;

the upper end socket cavity is provided with a tube pass inlet, the lower end socket cavity is provided with a tube pass outlet, and the upper end and the lower end of the heat exchange cavity are respectively provided with a shell pass outlet and a shell pass inlet;

the organic solvent spraying device is arranged in the upper seal head cavity and used for spraying organic solvent into the heat exchange tubes.

Preferably, the organic solvent spraying device comprises a spraying pipe and a plurality of atomizing nozzles arranged on the spraying pipe, the plurality of atomizing nozzles are distributed on the same horizontal plane, and the plurality of atomizing nozzles are vertically arranged downwards.

Preferably, the spray pipe comprises a vertically arranged main pipe and a horizontally arranged distribution pipe, the main pipe is connected with the organic solvent inlet on the upper seal head cavity, the distribution pipe is connected with the main pipe, and the plurality of atomizing nozzles are arranged on the distribution pipe.

Preferably, the tube-side inlet is transversely disposed on the tank, and the atomizing nozzle is disposed between the tube-side inlet and the upper tube plate.

Preferably, the ratio of the vertical distance between the plane of the atomizing nozzle and the tube-side inlet to the vertical distance between the tube-side inlet and the upper tube plate is 0.2-0.6.

Preferably, the cross section of the tank body is circular, and the main pipe is arranged in the center of the cross section of the tank body.

Preferably, the plurality of atomizing nozzles are uniformly distributed on a circle centered on the main pipe.

Preferably, the ratio of the radius of the circle where the atomizing nozzle is located to the radius of the tank body is 0.4-0.8.

Preferably, the number of the atomizing nozzles is 4, wherein 1 atomizing nozzle is located right below the main pipe, and the rest 3 atomizing nozzles are uniformly distributed on a circle with the main pipe as a center.

Preferably, one atomising nozzle adjacent the tube side inlet is angled at 60 ° to the tube side inlet relative to the centre of the main tube.

The utility model provides a prevent blockking up shell and tube heat exchanger sets up organic solvent spray set in the last head chamber through in the heat exchange tube top, when high temperature coarse coal gas carries out heat recovery and crude oil separation, sprays organic solvent in to the heat exchange tube through organic solvent spray set, dissolves the heavy oil component of condensation wall built-up coalescence on the heat exchange tube pipe wall to can reduce heat exchanger dirt coefficient, promote heat exchanger heat transfer efficiency.

Drawings

The above and other objects, features and advantages of the present invention will become more apparent from the following description of the embodiments of the present invention with reference to the accompanying drawings.

Fig. 1 shows a schematic structural diagram of an anti-clogging tubular heat exchanger according to an embodiment of the present invention.

Fig. 2 shows one arrangement of the atomizing nozzles on the distribution pipe in the anti-clogging tubular heat exchanger according to the embodiment of the present invention.

Fig. 3 shows a schematic view of an airflow streamline after high-temperature raw gas in the anti-blocking tubular heat exchanger enters the heat exchanger according to an embodiment of the utility model.

Fig. 4 shows a layout diagram of the atomizing nozzles in the anti-clogging tubular heat exchanger according to the embodiment of the present invention.

Fig. 5 shows a horizontal arrangement of atomizing nozzles in the anti-clogging tubular heat exchanger according to an embodiment of the present invention.

In the figure: the device comprises a tank body 1, a heat exchange tube mechanism 2, an upper tube plate 21, a lower tube plate 22, a heat exchange tube 23, an organic solvent spraying device 3, a main tube 31, a distribution tube 32, an atomizing nozzle 33, a tube side inlet A1, a tube side outlet A2, a shell side inlet B1, a shell side outlet B2 and an organic solvent inlet C.

Detailed Description

Various embodiments of the present invention will be described in more detail below with reference to the accompanying drawings. Like elements in the various figures are denoted by the same or similar reference numerals. For purposes of clarity, the various features in the drawings are not necessarily drawn to scale.

Referring to fig. 1, the utility model provides an anti-clogging tubular heat exchanger, which comprises a tank body 1, a heat exchange tube mechanism 2 and an organic solvent spraying device 3; the heat exchange tube mechanism 2 is arranged in the tank body 1 and comprises an upper tube plate 21 and a lower tube plate 22 which are arranged at intervals, and a plurality of heat exchange tubes 23 arranged between the upper tube plate 21 and the lower tube plate 22, the upper tube plate 21 and the lower tube plate 22 divide the tank body 1 into a heat exchange cavity in the middle, an upper end enclosure cavity in the upper part and a lower end enclosure cavity in the lower part, and the plurality of heat exchange tubes 23 are communicated with the upper end enclosure cavity and the lower end enclosure cavity; the upper end enclosure cavity is provided with a tube pass inlet A1, the lower end enclosure cavity is provided with a tube pass outlet A2, and the upper end and the lower end of the heat exchange cavity are respectively provided with a shell pass outlet B2 and a shell pass inlet B1; the organic solvent spraying device 3 is arranged in the upper head cavity and is used for spraying organic solvent into the plurality of heat exchange tubes 23.

Specifically, jar body 1 comprises triplex, including the barrel in the middle to and locate barrel upper end and the upper cover and the low head of lower extreme, all link together through the welding mode between barrel, upper cover and the low head. The heat exchange tube 23 is a circular metal tube, the upper sealing plate and the lower sealing plate are metal plates, round holes matched with the diameter of the heat exchange tube 23 are uniformly formed in the upper sealing plate and the lower sealing plate respectively, two ends of the heat exchange tube 23 penetrate through the round holes of the upper tube plate 21 and the lower tube plate 22 respectively and are fixedly connected in a welding mode, and the upper tube plate 21 and the lower tube plate 22 are fixedly connected at the upper end and the lower end of the barrel respectively in a welding mode. When the tube bundle heat exchanger is used, high-temperature gas to be cooled flows into the upper end enclosure cavity through the tube pass inlet A1, is cooled by the plurality of heat exchange tubes 23, then enters the lower end enclosure cavity, and then flows out from the tube pass outlet A2; the low-temperature liquid fluid flows into the heat exchange cavity through the shell pass inlet B1, the gas to be cooled in the heat exchange tube 23 is cooled, heat recovery is carried out, and the liquid fluid after absorbing heat flows out of the shell pass outlet B2 and enters the next working section; in the heat exchange process, heavy components can be condensed and separated out on the tube wall of the heat exchange tube 23, the organic solvent is sprayed into the heat exchange tube 23 through the organic solvent spraying device 3 to dissolve the heavy components condensed and separated out on the tube wall of the heat exchange tube 23, the heavy components enter the lower end enclosure cavity, and flow out from the tube side outlet A2 together with cooled gas to enter the next device for continuous treatment.

In this embodiment, the working principle of the anti-clogging tubular heat exchanger of this embodiment is explained by taking the coal hydrogenation gasification heat recovery and crude oil separation process as an example: after cyclone coarse dust removal and fine dust removal by a filter, the coarse coal gas at about 400 ℃ enters an upper end enclosure cavity in the tank body 1 through a tube pass inlet A1, then flows into a lower end enclosure cavity through a plurality of heat exchange tubes 23, when flowing through the heat exchange tubes 23, boiler water flowing from a battery compartment from a shell pass inlet B1 in the heat exchange cavity in the middle of the tank body 1 exchanges heat with high-temperature coarse coal gas in the heat exchange tubes 23, the boiler water enters the heat exchange cavity from a shell pass inlet B1, is heated to about 190 ℃ after cross flow heat exchange, and finally flows out from a shell pass outlet B2 to enter the next working section; the crude gas is cooled to about 200 ℃ through the heat exchange tube 23 to reach the dew point of heavy components such as crude pyrene, naphthalene, fluorene, anthracene green and the like, and the heavy components are condensed and separated out and enter a lower end enclosure cavity together with the crude gas, and then enter next equipment through a tube pass outlet A2 for gas-liquid separation. The crude gas is condensed from about 400 ℃ to about 200 ℃ in the heat exchange tube 23, part of heavy oil composition (composition with high dew point) can be separated out in the condensation process and is hung on the wall on the inner wall of the heat exchange tube 23 and is coalesced, and when the crude gas is operated for a long time, the heavy oil composition is continuously accumulated, so that the fouling coefficient of the heat exchanger is increased, the heat exchange efficiency is reduced, and the temperature of the outlet of the heat exchanger is over-temperature. According to the principle of solubility of heavy components such as crude pyrene, naphthalene, fluorene and anthracene green in crude gas in an organic solvent, the organic solvent is sprayed by an organic solvent spraying device arranged in an upper seal head cavity, and heavy blockages attached to the tube wall of a heat exchanger can be dissolved by utilizing the solubility of the liquid organic solvent, so that the purposes of dredging the heat exchange tube, reducing the fouling coefficient of the heat exchanger and improving the heat transfer efficiency of the heat exchanger are achieved. In this example, the organic solvent is benzene.

The organic solvent spraying device 3 comprises a spraying pipe and a plurality of atomizing nozzles 33 arranged on the spraying pipe, the atomizing nozzles 33 are distributed on the same horizontal plane, and the atomizing nozzles 33 are all vertically arranged downwards. As shown in fig. 1, the shower pipe includes a main pipe 31 vertically disposed and a distribution pipe 32 horizontally disposed, the main pipe 31 is connected to an organic solvent inlet C on the upper head chamber, the distribution pipe 32 is connected to the main pipe 31, and a plurality of atomizing nozzles 33 are provided on the distribution pipe 32. The distribution pipe 32 may be configured as a circular pipe or as radially arranged branch pipes connected to the main pipe 31. By horizontally arranging the distribution pipes 32, it is possible to increase the area of the arrangement of the atomizing nozzles 33, to increase the spraying range, and to make the organic solvent spray uniformly.

As shown in fig. 1, in this embodiment, the tube-side inlet a1 is transversely disposed on the tank 1, that is, the gas to be cooled flows transversely into the upper head chamber, the gas flow entering the upper head chamber from the tube-side inlet a1 is due to the jet flow turning back effect, and the distribution of the gas amount (corresponding to the amount of heavy blockage) entering each heat exchange tube 23 is uneven, and the schematic flow line diagram of the gas flow is shown in fig. 3. Due to the disturbance effect of the air flow, the uneven distribution of the spraying amount of the organic solvent in each heat exchange tube 23 is also influenced, and the optimal dissolving effect of the blockage on the tube wall of the heat exchange tube 23 cannot be realized. Therefore, the atomizing nozzles 33 of the organic solvent spraying device 3 should be reasonably arranged in space position in combination with the flowing characteristics of the gas flow. The combination of the air flow characteristics and the arrangement of the atomizing nozzle 33 between the tube side inlet a1 and the upper tube plate 21 can effectively reduce the influence of air flow disturbance. Referring to fig. 4, a vertical distance between a plane where the atomizing nozzle 33 is located and the tube-side inlet a1 is H1, a vertical distance between the tube-side inlet a1 and the upper tube plate 21 is H, a ratio of H1 to H is in a range of 0.2 to 0.6, and in this embodiment, H1 is 0.4H, so that the atomizing nozzle 33 is located within the returning air flow.

Further, the cross section of the tank body 1 is circular, the main pipe 31 is arranged at the center of the cross section of the tank body 1, and the plurality of atomizing nozzles 33 are uniformly distributed on a circle with the main pipe 31 as the center. As shown in fig. 2, four atomizing nozzles 33 are uniformly distributed in a ring shape. So set up and to make organic solvent spray more evenly, reach better spraying effect.

In this embodiment, the number of the atomizing nozzles 33 is four, one atomizing nozzle 33 is disposed right below the main pipe 31 (i.e., the center of the cross section of the can body 1), and the remaining three atomizing nozzles 33 are uniformly distributed on a circle with the main pipe 31 as a center. As shown in fig. 5, in this embodiment, the angle α between one atomizing nozzle 33 adjacent to the tube-side inlet a1 and the tube-side inlet a1 with respect to the center of the main tube 31 is 60 °, that is, the two atomizing nozzles 33 adjacent to the tube-side inlet a1 are symmetrically disposed on both sides of the airflow inflow path, so that the influence of the airflow disturbance can be reduced as much as possible. Wherein, the distance of the atomizing nozzle 33 of three atomizing nozzle 33 apart from central point to put is L (the radius of 3 atomizing nozzle 33 place circles that the hoop evenly arranged), jar 1 radius is R, the radius of the circle of atomizing nozzle 33 place circle and the ratio of jar 1 radius of body are 0.4 ~ 0.8, in this embodiment, L is 0.6R, the heat exchange tube jam degree that this embodiment synthesized the consideration air current flow field characteristics correspond, use as far as possible few atomizing nozzle, and arrange atomizing nozzle's spatial arrangement in a reasonable way, with satisfying organic solvent and spraying the wide coverage, reduce and spray the blind area, and then better satisfy dissolving to the heavy component on the heat exchange tube.

To sum up, the utility model provides a prevent blockking up shell and tube heat exchanger sets up organic solvent spray set in the last head chamber of heat exchange tube top, when high temperature coarse coal gas carries out heat recovery and crude oil separation, sprays organic solvent in to the heat exchange tube through organic solvent spray set, dissolves the heavy oil component of condensation wall built-up coalescence on the heat exchange tube pipe wall to can reduce heat exchanger dirt coefficient, promote heat exchanger heat transfer efficiency.

It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.

Finally, it should be noted that: it should be understood that the above examples are only for clearly illustrating the present invention and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious changes and modifications may be made without departing from the scope of the present invention.

Claims (10)

1. An anti-blocking tubular heat exchanger is characterized by comprising a tank body, a heat exchange tube mechanism and an organic solvent spraying device; wherein the content of the first and second substances,

the heat exchange tube mechanism is arranged in the tank body and comprises an upper tube plate and a lower tube plate which are arranged at intervals, and a plurality of heat exchange tubes arranged between the upper tube plate and the lower tube plate, the upper tube plate and the lower tube plate divide the tank body into a heat exchange cavity at the middle part, an upper end enclosure cavity at the upper part and a lower end enclosure cavity at the lower part, and the plurality of heat exchange tubes are communicated with the upper end enclosure cavity and the lower end enclosure cavity;

the upper end socket cavity is provided with a tube pass inlet, the lower end socket cavity is provided with a tube pass outlet, and the upper end and the lower end of the heat exchange cavity are respectively provided with a shell pass outlet and a shell pass inlet;

the organic solvent spraying device is arranged in the upper seal head cavity and used for spraying organic solvent into the heat exchange tubes.

2. The anti-clogging tubular heat exchanger according to claim 1, wherein the organic solvent spraying device comprises a spraying tube and a plurality of atomizing nozzles arranged on the spraying tube, the plurality of atomizing nozzles are distributed on the same horizontal plane, and the plurality of atomizing nozzles are all arranged vertically downwards.

3. The anti-clogging tubular heat exchanger according to claim 2, wherein the shower comprises a vertically arranged main tube and a horizontally arranged distribution tube, the main tube is connected to the organic solvent inlet on the upper head chamber, the distribution tube is connected to the main tube, and the plurality of atomizing nozzles are disposed on the distribution tube.

4. The anti-clogging tube array heat exchanger of claim 3 wherein the tube side inlet is disposed transversely to the tank and the atomizing nozzle is disposed between the tube side inlet and the upper tube sheet.

5. The anti-clogging tube and tube heat exchanger of claim 4 wherein the ratio of the vertical distance between the plane of the atomizing nozzles and the tube side inlet to the vertical distance between the tube side inlet and the upper tube sheet is 0.2 to 0.6.

6. The anti-clogging tubular heat exchanger according to claim 4, wherein the cross section of the tank is circular, and the main tube is provided at the center of the cross section of the tank.

7. The anti-clogging tube array heat exchanger of claim 6 wherein a plurality of said atomizing nozzles are evenly distributed on a circle centered on said primary tube.

8. The anti-clogging tubular heat exchanger according to claim 7, wherein the ratio of the radius of the circle on which the atomizing nozzle is located to the radius of the tank body is 0.4-0.8.

9. The anti-clogging tubular heat exchanger according to claim 7, wherein the number of the atomizing nozzles is 4, 1 of the atomizing nozzles is located right below the main tube, and the remaining 3 atomizing nozzles are uniformly distributed on a circle centered on the main tube.

10. The anti-clogging tube array heat exchanger of claim 7 wherein one atomizing nozzle adjacent to the tube side inlet is at an angle of 60 ° to the tube side inlet with respect to the center of the main tube.

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