CN214407084U - Heat exchanger for methanol hydrogen production heat exchange system - Google Patents
Heat exchanger for methanol hydrogen production heat exchange system Download PDFInfo
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- CN214407084U CN214407084U CN202022892041.XU CN202022892041U CN214407084U CN 214407084 U CN214407084 U CN 214407084U CN 202022892041 U CN202022892041 U CN 202022892041U CN 214407084 U CN214407084 U CN 214407084U
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Abstract
The utility model discloses a heat exchanger for a methanol hydrogen production heat exchange system, which relates to the field of heat exchangers and is used for heat exchange of raw material liquid in a methanol hydrogen production process, the heat exchanger comprises a heat exchanger and a vaporization superheater, the heat exchanger is fixedly connected with the vaporization superheater through a second tube plate, and a tube pass of the heat exchanger is communicated with a shell pass of the vaporization superheater through the second tube plate; the utility model discloses a structure has that occupation of land space is little, equipment space is compact, low equipment cost, high sled dress ization and the characteristics of complete set ization, has reduced the heat loss, has improved high thermal efficiency, has certain economic value and engineering meaning.
Description
Technical Field
The utility model relates to a heat exchanger field for to the heat transfer of raw materials liquid in the methyl alcohol hydrogen manufacturing technology, in particular to a heat exchanger for methyl alcohol hydrogen manufacturing heat transfer system.
Background
The traditional vaporizing superheater and the heat exchanger in the hydrogen production from methanol are two separate devices which are respectively arranged in a process system, and then the two devices are connected by connecting pieces such as pipelines and the like to form the processes of heat exchange and vaporizing superheating. For the process of preparing hydrogen from methanol, the separated arrangement has the advantages of large occupied space, low heat utilization rate and high equipment cost, and is not beneficial to skid-mounting and complete set.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a: the heat exchanger for the methanol-to-hydrogen heat exchange system has the characteristics of small occupied space, compact equipment space, low equipment cost, high skid-mounted performance and complete set performance, reduces heat loss, improves high thermal efficiency, and has certain economic value and engineering significance.
For solving the technical problem, the utility model discloses a technical scheme as follows:
a heat exchanger for a methanol-to-hydrogen heat exchange system comprises a heat exchanger and a vaporization superheater, wherein the heat exchanger and the vaporization superheater are fixedly connected through a second tube plate, and a tube pass of the heat exchanger is communicated with a shell pass of the vaporization superheater through the second tube plate.
Further note the working state of the application:
1. process for heating and vaporizing raw material liquid
The normal-temperature raw material liquid after being mixed enters a tube pass of a heat exchanger for heat exchange, and after the heat exchange, the raw material liquid is preheated to about 140 ℃; after being preheated, the raw material liquid enters the shell pass of the vaporization superheater from a second tube plate on the heat exchanger to continuously exchange heat, and the temperature of the raw material liquid after being vaporized and superheated through heat exchange is about 250 degrees.
2. Heat exchange process of heat conducting oil
The temperature of the heat transfer oil conveyed from the oil furnace is about 270 degrees, the heat transfer oil enters a tube side of the vaporization superheater for heat exchange, and the heat transfer oil enters the next heat exchange unit after the heat exchange of the vaporization superheater.
3. Heat exchange process of reformed gas
The temperature of the converted gas from the reactor is about 250 degrees, the converted gas enters the shell side of the heat exchanger for heat exchange, and the temperature is about 120 degrees after the heat exchange.
Further, the heat exchanger includes the casing down, and casing opening both ends are equipped with first tube sheet and second tube sheet respectively down, are equipped with the heat exchange tube between first tube sheet and the second tube sheet, and one side that the second tube sheet was kept away from to first tube sheet is equipped with raw materials liquid pipe case, is equipped with the raw materials liquid import on the raw materials liquid pipe case.
Furthermore, the upper side of the lower shell is provided with a reformed gas inlet, and the lower side is provided with a reformed gas outlet.
Furthermore, a baffling baffle connected with the heat exchange tube is arranged on the inner side of the lower shell.
Furthermore, a temperature compensation element is arranged on the lower shell.
Further, the vaporization superheater comprises an upper shell, a vaporization superheat outlet is formed in the upper shell, the two ends of an opening of the upper shell are respectively connected with a second tube plate and a third tube plate, one side, close to the second tube plate, of the third tube plate is provided with a U-shaped tube bundle, the other side of the third tube plate is provided with a heat conduction oil tube box, the heat conduction oil tube box is divided into two cavities by a partition plate, the side edges of the two cavities are respectively provided with a heat conduction oil inlet and a heat conduction oil outlet, the top side of the two cavities is provided with an air outlet, and the two cavities are respectively arranged corresponding to the pipe orifices of the U-shaped tube bundle.
Furthermore, a pull rod is further arranged on one side, close to the second tube plate, of the third tube plate, and an inner ring baffle plate and an outer ring baffle plate are fixedly arranged on the pull rod.
Furthermore, a support frame is arranged on the upper shell.
Furthermore, the upper part of the upper shell is provided with a vaporization overheating outlet.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
the utility model discloses a through with between heat exchanger and the vaporization over heater through second tube sheet fixed connection, the tube side of heat exchanger and the shell side of vaporization over heater communicate through the second tube sheet, through such structure setting, the occupation of land space is little, has reduced unnecessary piping between heat exchanger and the vaporization over heater, and equipment becomes compacter, has reduced equipment cost, does benefit to sled dress ization and complete set ization, has certain economic value and engineering significance;
the normal-temperature raw material liquid after being mixed enters a tube pass of a heat exchanger for heat exchange, the raw material liquid is preheated to about 140 degrees after the heat exchange, the raw material liquid enters a shell pass of a vaporization superheater from a second tube plate 11 on the heat exchanger for continuous heat exchange after being preheated, and the temperature of the raw material liquid after being vaporized and superheated through the heat exchange is about 250 degrees; the temperature of the heat transfer oil conveyed from the oil furnace is about 270 degrees, the heat transfer oil enters a tube side of the vaporization superheater for heat exchange, and enters the next heat exchange unit after the heat exchange of the vaporization superheater; the temperature of converted gas from the reactor is about 250 degrees, the converted gas enters the shell side of the heat exchanger for heat exchange, and the temperature is about 120 degrees after the heat exchange, so that the continuous heat exchange of the raw material liquid is realized, the heat loss is reduced, and the heat efficiency is improved.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic structural diagram of the heat exchanger of the present invention;
FIG. 3 is a schematic cross-sectional structure of the heat exchanger of the present invention;
FIG. 4 is a schematic view of a vaporization superheater according to the present invention;
FIG. 5 is a schematic cross-sectional view of a vaporization superheater in accordance with the present invention;
reference numerals in the drawings indicate: 1-heat exchanger, 2-vaporization superheater, 3-raw material liquid inlet, 4-raw material liquid tube box, 5-first tube plate, 6-lower shell, 7-heat exchange tube, 8-baffle plate, 9-temperature compensation element, 10-reformed gas inlet, 11-second tube plate, 12-reformed gas outlet, 13-U-shaped tube bundle, 14-pull rod, 15-upper shell, 16-supporting piece, 17-third tube plate, 18-heat conducting oil inlet, 19-exhaust port, 20-heat conducting oil outlet, 21-vaporization superheat outlet, 22-inner and outer ring baffle plate and 23-partition plate.
Detailed Description
The present application is further described below with reference to the accompanying drawings.
Referring to fig. 1, a heat exchanger for a methanol hydrogen production heat exchange system, including heat exchanger 1 and vaporization superheater 2, pass through second tube sheet 11 fixed connection between heat exchanger 1 and the vaporization superheater 2, the tube side of heat exchanger 1 and the shell side of vaporization superheater 2 communicate through second tube sheet 11, through such structural arrangement, occupation of land space is little, unnecessary piping between heat exchanger 1 and the vaporization superheater 2 has been reduced, equipment becomes compacter, equipment cost has been reduced, do benefit to sled dress ization and complete set, certain economic value and engineering significance have. The normal-temperature raw material liquid after being mixed enters a tube pass of a heat exchanger 1 for heat exchange, the raw material liquid is preheated to about 140 degrees after the heat exchange, the raw material liquid enters a shell pass of a vaporization superheater from a second tube plate 11 on the heat exchanger 1 for continuous heat exchange after being preheated, and the temperature of the raw material liquid after being vaporized and superheated through the heat exchange is about 250 degrees; the temperature of the heat conduction oil conveyed from the oil furnace is about 270 degrees, the heat conduction oil enters the tube side of the vaporization superheater 2 for heat exchange, and enters the next heat exchange unit after the heat exchange of the vaporization superheater 2; the temperature of the converted gas from the reactor is about 250 degrees, the converted gas enters the shell side of the heat exchanger 1 for heat exchange, and the temperature is about 120 degrees after the heat exchange, so that the continuous heat exchange of the raw material liquid is realized, the heat loss is reduced, and the heat efficiency is improved.
Referring to fig. 2 and 3, in the above device, the heat exchanger 1 includes a lower shell 6, a first tube plate 5 and a second tube plate 11 are respectively disposed at two open ends of the lower shell 6, a heat exchange tube 7 is disposed between the first tube plate 5 and the second tube plate 11, a raw material liquid tube box 4 is disposed at one side of the first tube plate 5 away from the second tube plate 11, a raw material liquid inlet 3 is disposed on the raw material liquid tube box 4, and the raw material liquid flows into the raw material liquid tube box 4 from the raw material liquid inlet 3, and then flows into the heat exchange tube 7 and flows to the shell side of the vaporizing superheater 2 through the second tube plate 11 under the action of pressure.
Referring to fig. 2, in the above-described apparatus, a temperature compensation element 9 is provided on the lower case 6 in consideration of the reason for the temperature difference.
Referring to fig. 2, in the above device, the upper side of the lower shell 6 is provided with a reformed gas inlet 10, the lower side is provided with a reformed gas outlet 12, and the reformed gas enters the shell pass of the heat exchanger 1 from the reformed gas inlet 10 and is discharged from the reformed gas outlet 12, so that the heat transfer effect is enhanced, and the heat exchange is facilitated; the inner side of the lower shell 6 is provided with a baffle 8 connected with the heat exchange tube 7, and the baffle 8 increases the turbulence intensity and improves the heat transfer coefficient.
Referring to fig. 4 and 5, in the above apparatus, the vaporizing superheater 2 includes an upper shell 15, a vaporizing superheater outlet 21 is provided on the upper shell 15, a second tube plate 11 and a third tube plate 17 are respectively connected to two ends of an opening of the upper shell 15, a U-shaped tube bundle 13 is provided on one side of the third tube plate 17 close to the second tube plate 11, a shadow part in fig. 5 indicates a position where the U-shaped tube bundle 13 can be disposed, a heat transfer oil tube box is provided on the other side of the third tube plate 17 close to the second tube plate 11, the heat transfer oil tube box is divided into two cavities by a partition plate 23, a heat transfer oil inlet 18 and a heat transfer oil outlet 20 are respectively provided on sides of the two cavities, an exhaust port 19 is provided on a top side, and the two cavities are respectively disposed corresponding to pipe orifices of the U-shaped tube bundle 13, the heat transfer oil flows into the cavity on one side of the heat transfer oil tube box from the heat transfer oil inlet 18, then enters the U-shaped tube bundle 13, flows out from the outlet on the other side of the U-shaped tube bundle 13, and then enters the cavity on the other side of the heat transfer oil tube box, and heat exchange is realized.
Referring to fig. 4, in the above device, the upper part of the upper shell 15 is provided with the vaporization overheating outlet 21, the raw material liquid flowing into the shell pass of the vaporization superheater 2 is discharged from the vaporization overheating outlet 21 after being heated and evaporated, and the vaporization overheating outlet 21 is arranged at the upper part of the upper shell 15 and has good heat exchange effect.
Referring to fig. 4, in the above-mentioned apparatus, a pull rod 14 is further disposed on one side of the third tube plate 17 close to the second tube plate 11, and an inner and outer annular baffle 22 is fixedly disposed on the pull rod 14 for enhancing the heat exchange effect.
Referring to fig. 4 and 5, in the above-mentioned device, a support frame 16 is provided on the upper casing 15 for fixing the position of the present invention.
The above-mentioned embodiments only express the specific embodiments of the present application, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present application. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the concept of the present invention, which falls within the scope of protection of the person skilled in the art.
Claims (9)
1. A heat exchanger for a methanol-to-hydrogen heat exchange system comprises a heat exchanger (1) and a vaporization superheater (2), and is characterized in that the heat exchanger (1) and the vaporization superheater (2) are fixedly connected through a second tube plate (11), and a tube pass of the heat exchanger (1) is communicated with a shell pass of the vaporization superheater (2) through the second tube plate (11).
2. The heat exchanger for the hydrogen production from methanol heat exchange system according to claim 1, characterized in that the heat exchanger (1) comprises a lower shell (6), a first tube plate (5) and a second tube plate (11) are respectively arranged at two open ends of the lower shell (6), a heat exchange tube (7) is arranged between the first tube plate (5) and the second tube plate (11), a raw material liquid tube box (4) is arranged at one side of the first tube plate (5) far away from the second tube plate (11), and a raw material liquid inlet (3) is arranged on the raw material liquid tube box (4).
3. The heat exchanger for the hydrogen-methanol heat exchange system is characterized in that the lower shell (6) is provided with a reformed gas inlet (10) at the upper side and a reformed gas outlet (12) at the lower side.
4. A heat exchanger for a hydrogen-methanol heat exchange system according to claim 3, characterized in that the inner side of the lower shell (6) is provided with a baffle (8) connected with the heat exchange tube (7).
5. A heat exchanger for a hydrogen-methanol heat exchange system according to claim 2, characterized in that the lower shell (6) is provided with a temperature compensation element (9).
6. The heat exchanger for the methanol hydrogen production heat exchange system according to claim 1, wherein the vaporizing superheater (2) comprises an upper shell (15), a vaporizing superheat outlet (21) is arranged on the upper shell (15), a second tube plate (11) and a third tube plate (17) are respectively connected to two ends of an opening of the upper shell (15), a U-shaped tube bundle (13) is arranged on one side of the third tube plate (17) close to the second tube plate (11), a heat transfer oil tube box is arranged on the other side of the third tube plate, the heat transfer oil tube box is divided into two cavities by a partition plate (23), a heat transfer oil inlet (18) and a heat transfer oil outlet (20) are respectively arranged on the lateral sides of the two cavities, an exhaust port (19) is arranged on the top side of the two cavities, and the two cavities are respectively arranged corresponding to pipe orifices of the U-shaped tube bundle (13).
7. The heat exchanger for the hydrogen-methanol production heat exchange system according to claim 6, characterized in that a pull rod (14) is further arranged on one side of the third tube plate (17) close to the second tube plate (11), and an inner ring baffle plate and an outer ring baffle plate (22) are fixedly arranged on the pull rod (14).
8. The heat exchanger for the hydrogen-methanol production heat exchange system according to claim 7, wherein a support frame (16) is arranged on the upper shell (15).
9. The heat exchanger for the hydrogen-methanol heat exchange system according to claim 7, characterized in that the upper part of the upper shell (15) is provided with a vaporization superheat outlet (21).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022892041.XU CN214407084U (en) | 2020-12-04 | 2020-12-04 | Heat exchanger for methanol hydrogen production heat exchange system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022892041.XU CN214407084U (en) | 2020-12-04 | 2020-12-04 | Heat exchanger for methanol hydrogen production heat exchange system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214407084U true CN214407084U (en) | 2021-10-15 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022892041.XU Active CN214407084U (en) | 2020-12-04 | 2020-12-04 | Heat exchanger for methanol hydrogen production heat exchange system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214407084U (en) |
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2020
- 2020-12-04 CN CN202022892041.XU patent/CN214407084U/en active Active
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