TWM569414U - Winding tube type heat exchanger at top of chemical plant - Google Patents

Abstract

The present invention relates to a wound tubular heat exchanger at the top of a chemical plant, which comprises a casing, a support bucket and at least two heat exchange layers. The housing defines an axial direction, and the upper end of the housing is respectively provided with an upper tube cover and a lower tube cover, and the housing is further provided with two openings communicating with the outside. The support barrel is disposed in the casing and is respectively connected to one of the upper tube sheet of the upper tube cover and one of the lower tube sheets of the lower tube cover. The at least two heat exchange layers are disposed in the housing, and each of the heat exchange layers has at least one heat exchange tube, and the two ends of the at least one heat exchange tube of each of the heat exchange layers are respectively connected to the upper tube sheet and the lower tube The plate, each of the at least one heat exchange tube is spirally wound along the support barrel, wherein the spiral winding directions of any adjacent two heat exchange layers are opposite.

Description

Winding tube heat exchanger at the top of chemical plant

This creation is about a coiled tube heat exchanger at the top of a chemical plant.

According to the development of modern industry, in order to meet the demand, many petrochemical plants are discharged from high towers. Traditional shell-and-tube heat exchangers and plate heat exchangers are used to recover heat energy, but the temperature at the top of the tower is too low. The pressure drop limit and the limited installation space of the towers cause the temperature to be unrecoverable and thus wasted, and there are drawbacks that need to be improved.

Therefore, it is necessary to provide a novel and progressive coiled-tube heat exchanger at the top of a chemical plant to solve the above problems.

The main purpose of this creation is to provide a wound tubular heat exchanger used in the top of a chemical plant to solve the above shortcomings, and combine the advantages of many heat exchangers, under the conditions of low heat source temperature and low pressure drop of the process. With high heat transfer performance, the vertical structure can save space in places where installation is limited, and the operation is resistant to temperature and pressure changes, safe and reliable against leakage.

To achieve the above object, the present invention provides a coiled tube heat exchanger at the top of a chemical plant, which comprises a casing, a support bucket and at least two heat exchange layers. The housing defines an axial direction, and the upper end of the housing is respectively provided with an upper tube cover and a lower tube cover, and the housing is further provided with two openings communicating with the outside. The support barrel is disposed in the casing and is respectively connected to one of the upper tube sheet of the upper tube cover and one of the lower tube sheets of the lower tube cover. The at least two heat exchange layers are disposed in the housing, and each of the heat exchange layers has at least one heat exchange tube, and the two ends of the at least one heat exchange tube of each of the heat exchange layers are respectively connected to the upper tube sheet and the lower tube The plate, each of the at least one heat exchange tube is spirally wound along the support barrel, wherein the spiral winding directions of any adjacent two heat exchange layers are opposite.

The structural features of the present invention and the intended effects thereof will be described below by way of a preferred embodiment, but are not intended to limit the scope of the present invention.

Referring to FIG. 1 to FIG. 4, a preferred embodiment of the present invention is shown. The coiled-tube heat exchanger of the top of the chemical plant of the present invention comprises a casing 1, a support barrel 4 and at least two heat exchange layers 5. .

The housing 1 defines an axial direction 11. The upper end of the housing 1 along the axial direction 11 is respectively provided with an upper tube cover 2 and a lower tube cover 3. The housing 1 is further provided with two openings 12 communicating with the outside. A first fluid (such as a fluid such as hydrogen or oil and gas) enters the housing 1 from the opening 12 and exits the housing 1 via the other opening 12.

The support barrel 4 is disposed in the casing 1 and is respectively connected to one of the upper tube sheet 21 of the upper tube cover 2 and the lower tube sheet 31 of the lower tube cover 3.

The at least two heat exchange layers 5 are disposed in the casing 1. Each of the heat exchange layers 5 has at least one heat exchange tube 51. The two ends of the at least one heat exchange tube 51 of each of the heat exchange layers 5 are respectively connected to the heat exchange tube 51. The upper tube sheet 21 and the lower tube sheet 31, each of the at least one heat exchange tubes 51 are spirally wound along the support barrel 4 (as shown in FIG. 2), wherein the spiral winding directions of the adjacent two heat exchange layers 5 are opposite. In the present embodiment, the heat exchange layer 5 is two.

Each of the heat exchange layers 5 includes two heat exchange tubes 51, and the two heat exchange tubes 51 of each of the heat exchange layers 5 are spirally wound at intervals. In the embodiment, the upper tube cover 2 and the lower tube cover 3 respectively have a passage 22 and a lower passage 32 connected to one of the heat exchange tubes 51, so that a second fluid can pass through the upper passage 22 and the lower portion. One of the passages 32 flows into the heat exchange tubes 51, and then flows out through the other, and the higher temperature between the first fluid and the second fluid can transfer the heat energy to the lower temperature. Since the spiral winding directions of the adjacent two heat exchange layers 5 are opposite, when the first fluid flows in the casing 1, the two heat exchange layers 5 can form an irregular flow of the first fluid to effectively Mixing the first fluid to increase the heat exchange efficiency, and each of the heat exchange layers 5 is spirally wound, and has strong mechanical structural strength, which can effectively prevent the heat exchange tubes from being broken, and the spiral wound structure only It has a curved arc section, so unlike conventional shell-and-shell heat exchangers, it has a dead angle and is prone to accumulation.

The two ends of the support barrel 4 have a tapered section 41 which is respectively connected between the upper tube sheet 21 and the lower tube sheet 31.

Preferably, each of the heat exchange tubes 51 has a helix angle of 15 to 35 degrees, and is 30 degrees in this embodiment, so that the second fluid does not pass through the heat exchange tubes 51 very quickly. It will stay in the heat exchange tubes 51 for too long, so that the time for optimum heat exchange efficiency through the heat exchange tubes 51 can be provided.

The casing 1 is respectively provided with a half ball segment 13 at both ends of the axial direction 11 to maintain the structural strength of both ends of the axial direction 11 of the casing 1.

Each of the heat exchange tubes 51 is a stainless steel tube body or a titanium alloy tube body (in the present embodiment, a stainless steel tube body), which is less corrosive to improve durability. In other embodiments, the heat exchange tubes may be other high temperature resistant tubes. And corrosion resistant materials.

For example, as shown in FIG. 4, when a fluid (such as oil and gas) in the fractionation column 91 is discharged from the top of the tower, the inlet 1 enters the casing 1 through the opening 12, and is discharged through the other opening 12. The casing 1 and a crude oil pipe 92 flow into the heat exchange tubes 51 through the lower passage 32 and flow out through the upper passage 22, and the crude oil can exchange heat with the oil and gas, can be heated from 35 degrees Celsius to 75 degrees, and is introduced into the fractionation. The fractionation process in the column 91 can reduce the loss of oil and gas heat, and can reduce the fuel consumption of the heater 93 disposed in the fractionation column 91, even under the condition that the heat source temperature is too low and the process low pressure drop limit High heat transfer performance, it should be noted that in other embodiments, the flow directions of the fluids in the heat exchange tubes 51 and the housing 1 may be reversed, and the positions of the first fluid and the second fluid may also be reversed. To match the structural design of different chemical plants.

In summary, the winding tubular heat exchanger of the top of the chemical plant of the present invention has the opposite spiral winding direction of the adjacent two heat exchange layers, and the second heat exchange is performed when the first fluid flows in the casing. The layer may form an irregular flow of the first fluid to effectively mix the first fluid to increase heat exchange efficiency, and each of the heat exchange layers is spirally wound, and has strong mechanical structural strength, which can effectively avoid each The heat exchange tube is broken, and the spirally wound structure only has a curved arc section, so unlike conventional shell-and-shell heat exchangers, there is a dead angle which is liable to cause accumulation.

1‧‧‧shell

2‧‧‧Upper cover

3‧‧‧ Lower cap

4‧‧‧Support bucket

5‧‧‧Heat exchange layer

11‧‧‧Axial

12‧‧‧ openings

13‧‧‧Semi-spherical segment

22‧‧‧Upper channel

31‧‧‧ Lower tube sheet

32‧‧‧lower channel

41‧‧‧Constriction

51‧‧‧ heat exchange tube

91‧‧‧ fractionation tower

92‧‧‧ crude oil pipeline

93‧‧‧heater

21‧‧‧Upper tube sheet

1 is a perspective view of a preferred embodiment of the present invention. 2 is a partially hidden perspective view of a preferred embodiment of the present invention. 3 is a cross-sectional view of a test in accordance with a preferred embodiment of the present invention. 4 is a flow chart of a preferred embodiment of the present invention.

Claims (8)

A wound tubular heat exchanger at the top of a chemical plant, comprising: a casing defining an axial direction, wherein the casing is respectively provided with an upper pipe cover and a lower pipe cover at both ends of the axial direction, and the casing is separately provided a second opening connected to the outside; a support barrel disposed in the housing and connected at both ends to the upper tube sheet of the upper tube cover and the lower tube sheet of the lower tube cover; at least two heat exchange layers are disposed at In the housing, each of the heat exchange layers has at least one heat exchange tube, and the two ends of the at least one heat exchange tube of each of the heat exchange layers are respectively connected to the upper tube sheet and the lower tube sheet, and the at least one heat exchange tube The spiral winding is performed along the support barrel, wherein the spiral winding directions of any two adjacent heat exchange layers are opposite. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein each of the heat exchange layers comprises two heat exchange tubes, and the two heat exchange tubes of each of the heat exchange layers are spirally wound at intervals. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein both ends of the support barrel have a tapered section, and the two tapered sections are respectively connected to the upper tube sheet and the lower tube sheet between. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein each of the heat exchange tubes has a helix angle of 15 to 35 degrees. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein the casing is provided with a half ball segment at both ends of the axial direction. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein each of the heat exchange tubes is a stainless steel tube body or a titanium alloy tube body. The coiled tube heat exchanger of the top of a chemical plant according to claim 1, wherein the upper tube cover and the lower tube cover respectively have a passage and a lower passage connected to one of the heat exchange tubes. The coiled tube heat exchanger of the top of a chemical plant according to claim 2, wherein both ends of the support barrel have a tapered section, and the two tapered sections are respectively connected to the upper tube sheet and the lower tube sheet The spiral angle of each of the heat exchange tubes is 15 degrees to 35 degrees; the shell is respectively provided with a half ball segment along both ends of the axial direction; each of the heat exchange tubes is a stainless steel tube body or a titanium alloy tube body; The upper tube cover and the lower tube cover respectively have a passage and a lower passage connected to one of the heat exchange tubes.