CN210560266U - Device for recycling and reusing heat at top of reforming pre-hydrogenation fractionating tower - Google Patents
Device for recycling and reusing heat at top of reforming pre-hydrogenation fractionating tower Download PDFInfo
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- CN210560266U CN210560266U CN201921444241.XU CN201921444241U CN210560266U CN 210560266 U CN210560266 U CN 210560266U CN 201921444241 U CN201921444241 U CN 201921444241U CN 210560266 U CN210560266 U CN 210560266U
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Abstract
The utility model provides a device is recycled to reforming hydrogenation fractionating tower top heat recovery in advance, the device includes: the bottom of the pre-hydrogenation fractionating tower is provided with a tower bottom heating furnace for circulating heating; a first heat exchange pipeline of the first heat exchanger is communicated with the top end of the pre-hydrogenation fractionating tower and an air cooler, and the air cooler flows back to the upper part of the pre-hydrogenation fractionating tower through a tower top water cooler and a reflux tank in sequence; and one end of a third heat exchange pipeline of the second heat exchanger is communicated with the second heat exchange pipeline after heat exchange of the first heat exchanger, and one end of a fourth heat exchange pipeline of the second heat exchanger is communicated with a third tee joint between the bottom end of the pre-hydrogenation fractionating tower and the tower bottom heating furnace. The utility model discloses can utilize reforming oil and reforming oil fractionating tower top of the tower oil gas heat transfer, effectively retrieve reforming oil fractionating tower top of the tower oil gas heat, reduce reforming oil fractionating tower top of the tower air cooler and water cooler heat load, reduce heat exergy and decrease, be favorable to the heat step to utilize.
Description
Technical Field
The utility model belongs to petrochemical's oil gas heat recovery utilizes the field, and specifically speaking relates to a device is recycled to reforming hydrogenation fractionating tower top heat recovery.
Background
The pretreatment of the reformed raw oil is an important component of a catalytic reforming device, the sulfur, nitrogen, chlorine, oxygen, metals and the like contained in the reformed raw oil are removed by hydrogenation through a pre-refining catalyst, olefin is subjected to hydrogenation saturation, and then appropriate raw oil fractions are cut by fractionation according to the requirements of target products so as to meet the quality requirements of the reforming device on feeding materials.
The main processes of the pre-hydrogenation treatment comprise: the process of hydrogenation pre-refining, steam stripping and fractionation of raw materials. The method comprises the following steps of cooling material flow after pre-hydrogenation reaction to 30-50 ℃, then feeding the material flow into a gas-liquid separation tank, pressurizing hydrogen-containing gas at the top of the tank by a compressor, then performing circulating hydrogen, performing heat exchange on pre-hydrogenated oil at the bottom of the tank with material flow at 160-180 ℃ at the bottom of a pre-hydrogenation fractionating tower, performing heat exchange with material flow at 200-220 ℃ at the bottom of a stripping tower, feeding the material flow into the stripping tower to remove C4 and the following components, feeding the material flow at the bottom of the tower into the pre-hydrogenation fractionating tower after heat exchange with feeding material, performing air cooling and water cooling on light naphtha at the top of the pre-; after the heavy naphtha at the bottom of the pre-hydrogenation fractionating tower exchanges heat with the feeding material of the stripping tower, one part of hot discharging material is directly supplied for reforming, and the other part is cooled and then is sent to a tank area.
There are problems: the reformed pre-hydrogenated oil exchanges heat with the tower bottom material flow of the pre-hydrogenated fractionating tower at the temperature of between 30 and 50 ℃, the temperature difference is large, and the exergy loss is large; the temperature of oil gas at the top of the pre-hydrogenation fractionating tower is 90-120 ℃, the temperature is high, the oil gas is directly cooled by air, and the heat is not utilized; the reboiler at the bottom of the stripping tower and the pre-hydrogenation fractionating tower consumes a large amount of fuel gas or 3.5MPa steam, and the energy consumption is high.
Therefore, how to efficiently utilize the heat at the top of the pre-hydrogenation fractionating tower and reduce the energy consumption of the device is a difficult point of the waste heat utilization of the refinery and an important measure for reducing the processing loss and improving the economic benefit of the refinery. At present, most domestic and foreign refineries adopt air cooling and water cooling for direct cooling by referring to relevant documents and patent technologies, for example: the method has the disadvantages that after the temperature of the pre-hydrogenated raw material is increased, the pre-hydrogenated raw material exchanges heat with pre-hydrogenated reaction products, a part of heat is transferred to the pre-hydrogenated reaction products, the temperature of the pre-hydrogenated reaction products before entering an air cooler is increased, so that the air cooling load is greatly increased, the phenomenon of unreasonable cooling while heating exists, and the heat utilization efficiency of the method is not high.
Therefore, the utility model provides a device is recycled to reforming hydrogenation fractionating tower top heat recovery in advance.
Disclosure of Invention
To the problem among the prior art, the utility model aims to provide a device is recycled to reforming hydrogenation fractionating tower top heat recovery in advance can utilize reforming refined oil and the heat transfer of reforming oil fractionating tower top oil gas, has effectively retrieved reforming oil fractionating tower top oil gas heat, has reduced reforming oil fractionating tower top air cooler and water cooler heat load, has reduced heat exergy loss, is favorable to the heat cascade utilization.
The embodiment of the utility model provides a device is recycled to reforming hydrogenation fractionating tower top heat recovery in advance, include:
the tower bottom heating furnace is arranged at the bottom of the pre-hydrogenation fractionating tower and used for circularly heating;
the first heat exchanger comprises a first heat exchange pipeline and a second heat exchange pipeline, the first heat exchange pipeline of the first heat exchanger is communicated with the top end of the pre-hydrogenation fractionating tower and an air cooler, and the air cooler reflows to the upper part of the pre-hydrogenation fractionating tower through a tower top water cooler and a reflux tank in sequence; and
and the second heat exchanger comprises a third heat exchange pipeline and a fourth heat exchange pipeline, one end of the third heat exchange pipeline of the second heat exchanger is communicated with the second heat exchange pipeline after heat exchange of the first heat exchanger, and one end of the fourth heat exchange pipeline of the second heat exchanger is communicated with a third tee joint between the bottom end of the pre-hydrogenation fractionating tower and the tower bottom heating furnace.
Preferably, the method further comprises the following steps: a first port and a second port of the three-way valve are connected in series with a second heat exchange pipeline of the first heat exchanger which does not exchange heat, and a third port of the three-way valve is communicated with a first three-way node between the second heat exchange pipeline of the first heat exchanger after heat exchange and a third heat exchange pipeline of the second heat exchanger; and
and the temperature control unit is arranged between the first three-way joint and a third heat exchange pipeline of the second heat exchanger and is electrically connected with the three-way valve.
Preferably, a first heat exchange pipeline of the first heat exchanger, which is provided with the top oil gas of the pre-hydrogenation fractionating tower, exchanges heat with a second heat exchange pipeline provided with reformed pre-hydrogenated oil.
Preferably, the third heat exchange pipeline of the second heat exchanger with the heated reformed pre-hydrogenated oil exchanges heat with the fourth heat exchange pipeline with the heated discharge at the bottom of the pre-hydrogenated fractionating tower.
Preferably, the other end of the third heat exchange pipeline of the second heat exchanger is communicated with a stripping tower, and the bottom of the stripping tower is communicated with the middle part of the pre-hydrogenation fractionating tower through a first guide pipe.
Preferably, the other end of the fourth heat exchange pipeline of the second heat exchanger is respectively communicated with the reforming unit hot feed pipe and the bottom of the heavy naphtha tank.
Preferably, a tower bottom water cooler is arranged between the fourth heat exchange pipeline of the second heat exchanger and the bottom of the heavy naphtha tank.
Preferably, the method further comprises the following steps: and one end of the second guide pipe is communicated with a second tee joint between the reflux pump and the upper part of the pre-hydrogenation fractionating tower, and the other end of the second guide pipe is communicated with the light naphtha oil tank.
Preferably, the method further comprises the following steps: and the reflux pump is connected to the pipeline between the reflux tank and the second three-way node.
Preferably, the method further comprises the following steps: and the tower bottom pump is connected with a pipeline between the bottom end of the pre-hydrogenation fractionating tower and the third tee joint.
An object of the utility model is to provide a device is recycled to reforming hydrogenation fractionating tower top heat recovery, can pass through technology and device utilize reforming pre-hydrogenation oil and pre-hydrogenation fractionating tower top oil gas heat transfer, simultaneously through the heat transfer volume of tee bend governing valve control reforming pre-hydrogenation oil, fully retrieve the heat of pre-hydrogenation fractionating tower top oil gas, reforming pre-hydrogenation oil temperature will be improved to 60 ~ 80 ℃ by 30 ~ 50 ℃, then respectively with pre-hydrogenation fractionating tower bottom commodity circulation and the heat transfer of the tower bottom commodity circulation at the bottom of the tower, the heat transfer difference has been reduced, the tower has been improved and pre-hydrogenation fractionating tower inlet temperature is added, thereby reduce the thermal load at the bottom of the tower, still can improve reforming thermal feed temperature simultaneously, reduce reforming reaction feeding heating furnace thermal load, obvious energy-conserving effect has.
Drawings
Other features, objects and advantages of the invention will become more apparent from a reading of the following detailed description of non-limiting embodiments thereof, with reference to the accompanying drawings.
Fig. 1 is a schematic diagram of a device for recovering and recycling heat at the top of a reforming pre-hydrogenation fractionating tower.
Reference numerals
1 first heat exchanger
11 first heat exchange line
12 second heat exchange line
2 second heat exchanger
21 third heat exchange line
22 fourth heat exchange circuit
3 prehydrogenation fractionating tower
4 air cooler
5 tower top water cooler
6 backflow tank
7 reflux pump
8 tower bottom pump
9 tower bottom heating furnace
10 tower bottom water cooler
13 temperature control unit
14 three-way valve
15 first three-way node
16 first draft tube
17 second flow guide pipe
18 second three-way node
19 third three-way node
Detailed Description
Example embodiments will now be described more fully with reference to the accompanying drawings. Example embodiments may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of example embodiments to those skilled in the art. The same reference numerals in the drawings denote the same or similar structures, and thus their repetitive description will be omitted.
Fig. 1 is a schematic block diagram of a device for recovering and recycling heat from the top of a reforming pre-hydrogenation fractionating tower. As shown in fig. 1, an embodiment of the present invention provides a device for recycling heat from a top of a reforming pre-hydrogenation fractionating tower, including: the system comprises a first heat exchanger 1, a second heat exchanger 2, a pre-hydrogenation fractionating tower 3, an air cooler 4, a tower top water cooler 5, a reflux tank 6, a reflux pump 7, a tower bottom pump 8, a tower bottom heating furnace 9 and a tower bottom water cooler 10. The bottom of the pre-hydrogenation fractionating tower 3 is provided with a tower bottom heating furnace 9 for circulating heating. The first heat exchanger 1 comprises a first heat exchange pipeline 11 and a second heat exchange pipeline 12, the first heat exchange pipeline 11 of the first heat exchanger 1 is communicated with the top end of the pre-hydrogenation fractionating tower 3 and the air cooler 4, and the air cooler 4 sequentially flows back to the upper part of the pre-hydrogenation fractionating tower 3 through the tower top water cooler 5 and the reflux tank 6. The first heat exchange pipeline 11 of the first heat exchanger 1, which is provided with the top oil gas at 90-120 ℃ of the pre-hydrogenation fractionating tower 3, and the second heat exchange pipeline 12, which is provided with the reforming pre-hydrogenation oil at 30-50 ℃, exchange heat to obtain the reforming pre-hydrogenation oil at 60-80 ℃. The return pump 7 is connected to the line between the return tank 6 and the second three-way junction 18. The bottom pump 8 is connected to the line between the bottom of the pre-hydrogenation fractionation column 3 and the third three-way junction 19. The second heat exchanger 2 comprises a third heat exchange pipeline 21 and a fourth heat exchange pipeline 22, one end of the third heat exchange pipeline 21 of the second heat exchanger 2 is communicated with the second heat exchange pipeline 12 after heat exchange of the first heat exchanger 1, and one end of the fourth heat exchange pipeline 22 of the second heat exchanger 2 is communicated with a third tee joint 19 between the bottom end of the pre-hydrogenation fractionating tower 3 and the tower bottom heating furnace 9. The third heat exchange pipeline 21 of the second heat exchanger 2 with the reformed pre-hydrogenated oil at 60-80 ℃ after being heated exchanges heat with the fourth heat exchange pipeline 22 with the discharged material at 160-180 ℃ after being heated at the bottom of the pre-hydrogenated fractionating tower 3. The other end of the third heat exchange pipeline 21 of the second heat exchanger 2 is communicated with a stripping tower (not shown in the figure), and the bottom of the stripping tower is communicated with the middle part of the pre-hydrogenation fractionating tower 3 through a first guide pipe 16. The other end of the fourth heat exchange line 22 of the second heat exchanger 2 is communicated with a reforming unit hot feed pipe (not shown in the figure) and a heavy naphtha tank bottom (not shown in the figure), respectively. A tower bottom water cooler 10 is arranged between the fourth heat exchange pipeline 22 of the second heat exchanger 2 and the bottom of the heavy naphtha tank. One end of the second diversion pipe 17 is communicated with a second three-way joint 18 between the reflux pump 7 and the upper part of the pre-hydrogenation fractionating tower 3, and the other end is communicated with a light naphtha tank (not shown in the figure). The utility model discloses utilize reforming to add hydrogenated oil and add hydrogenated fractionating tower top oil gas heat transfer in advance, effectively retrieved and added hydrogenated tower top oil gas heat, reduced and added hydrogenated fractionating tower top air cooler and water cooler heat load. The utility model discloses the reforming prehydrogenation oil temperature risees, has reduced and has prehydrogenation fractionating tower bottom and the heat transfer difference in temperature of the tower bottom commodity circulation of strip, has reduced exergy and has decreased, is favorable to the heat step to utilize. The utility model discloses well strip tower, pre-hydrogenation fractionating tower and reforming feed temperature improve, can reduce strip tower, pre-hydrogenation fractionating tower bottom reboiler heat load and reduce reforming feed heating furnace heat load to reduce the device energy consumption.
In a preferred embodiment, the present invention further comprises a temperature control unit 13 and a three-way valve 14. A first port and a second port of the three-way valve 14 are connected in series to the second heat exchange pipeline 12 of the first heat exchanger 1 which does not exchange heat, and a third port of the three-way valve 14 is communicated with a first three-way node 15 between the second heat exchange pipeline 12 of the first heat exchanger 1 after heat exchange and a third heat exchange pipeline 21 of the second heat exchanger 2. The temperature control unit 13 is disposed between the first three-way node 15 and the third heat exchange pipeline 21 of the second heat exchanger 2, and the temperature control unit 13 is electrically connected to the three-way valve 14. The temperature control unit 13 monitors the temperature between the first three-way joint 15 and the third heat exchange pipeline 21 of the second heat exchanger 2 in real time, and when the temperature at the point is higher than 80 ℃, the reformed pre-hydrogenated oil which flows into the first heat exchange pipeline 11 of the first heat exchanger 1 and is 30 ℃ to 50 ℃ is increased through the three-way valve 14, so that the temperature of the reformed pre-hydrogenated oil after heat exchange is reduced. When the temperature at this point is lower than 60 ℃, the reformed pre-hydrogenated oil of 30 ℃ to 50 ℃ flowing into the first heat exchange line 11 of the first heat exchanger 1 is reduced by the three-way valve 14, thereby increasing the temperature of the reformed pre-hydrogenated oil after heat exchange. The utility model discloses a tee bend governing valve carries out temperature control to reforming pre-hydrogenated oil, adjusts the top of the tower oil gas heat transfer volume in a flexible way, makes the device operation more nimble.
The utility model provides a reforming prehydrogenation fractionating tower top heat recovery utilizes technology and device, through technology and device utilize reforming prehydrogenation oil and the heat transfer of prehydrogenation fractionating tower top oil gas, through the heat transfer volume of tee bend governing valve control reforming prehydrogenation oil simultaneously, fully retrieve the heat of prehydrogenation fractionating tower top oil gas, the reforming prehydrogenation oil temperature will be improved to 60 ~ 80 ℃ by 30 ~ 50 ℃, then respectively with the bottom commodity circulation of prehydrogenation fractionating tower bottom commodity circulation and the heat transfer of the tower bottom commodity circulation of stripping tower, the heat transfer difference has been reduced, the strip tower has been improved and has prehydrogenation fractionating tower feeding temperature, thereby reduce the bottom heat load of tower, still can improve the reforming heat feed temperature simultaneously, reduce reforming reaction feeding heating furnace heat load, obvious energy-conserving effect has.
The utility model provides a refinery reforming plant adds hydrogen fractionating tower top of tower oil gas heat recovery and utilizes's technique in advance, as shown in fig. 1, mainly include first heat exchanger (add hydrogen fractionating tower top of tower oil gas heat exchanger) 1, second heat exchanger (the tower bottom heat exchanger is fed in advance to the tower/in advance the fractionating tower) 2, add hydrogen fractionating tower 3 in advance, add hydrogen fractionating tower top of tower air cooler 4, top of the tower water cooler 5, reflux drum 6, reflux pump 7, bottom of the tower pump 8, tower bottom heating furnace 9, tower bottom water cooler 10.
The method comprises the following steps:
(1) the reformed pre-hydrogenated oil S1 with the temperature of 30-50 ℃ is heated to 60-80 ℃ by the pre-hydrogenated fractionating tower top oil gas heat exchanger 1.
(2) Then heated by a heat exchanger 2 at the bottom of the feeding/pre-hydrogenation tower of the stripping tower.
(3) From S2 to a stripping tower, the bottom material flow S3 separated by the stripping tower exchanges heat and enters a pre-hydrogenation fractionating tower 3.
(4) Oil gas at the top of the pre-hydrogenation fractionating tower is cooled by the pre-hydrogenation fractionating tower 1, then is sequentially cooled by the air cooler 4 and the water cooler 5, and then enters the reflux tank 6.
(5) Part of the water is returned by the return pump 7, and the other part is taken out at S5.
(6) The pre-hydrogenated fractionating tower 3 bottoms stream is cooled by 2 and divided into two paths, one path S4 is directly fed for the reforming unit, and the other path S5 is cooled by a tower bottom water cooler 10 and then fed to a heavy naphtha tank area.
Compared with the prior art, the utility model discloses following beneficial effect has at least:
the utility model discloses a heat transfer flow to the pre-hydrogenation fractionating unit of reformer optimizes, recycle adds the heat of hydrogenation fractionating tower top oil gas in advance, reduce the strip tower, add the heat load of hydrogenation fractionating tower and reforming feed heating furnace in advance, pre-hydrogenation fractionating tower air cooling and water cooling load have been reduced simultaneously, compared with the prior art, reduce about strip tower fuel consumption 1 ~ 3%, reduce and add hydrogen fractionating tower fuel consumption 2 ~ 4%, reduce about reforming feed heating furnace fuel consumption 10 ~ 15%, reduce and add hydrogen fractionating tower air cooling power consumption 15 ~ 25% in advance about, obvious energy-conserving effect has.
To facilitate understanding of the present invention, the present invention has the following embodiments. It should be understood by those skilled in the art that the described embodiments are merely provided to assist in understanding the present invention and should not be construed as specifically limiting the present invention.
Example 1
By taking a 230 ten thousand tons/year reforming device of a certain oil refinery as an example, the utility model discloses a reforming heat recycling method is demonstrated according to the calculation of reforming pre-hydrogenated oil heat exchange to 70 ℃ and pre-hydrogenated fractionating tower top oil gas heat exchanger (1) heat exchange 4888 kW.
The changes in the thermal load of the stripper, prefractionator and reforming feed heater before and after optimization are shown in table 1 below.
TABLE 1 optimization of thermal load changes before and after stripping, prefractionator and reforming feed heater
According to the upper table, adopt the utility model discloses a process can reduce strip tower heating load 1.7%, reduces to add hydrogenation fractionating tower heating load 3.1%, reduces reforming feed heating furnace heating load 12.5%, reduces to add hydrogenation fractionating tower headspace air cooling and water cooling load 21.7%, and strip tower headspace air cooling and water cooling load increase 6.4%, and reforming reaction product air cooler load increases 3%, has obvious energy-conserving effect.
To sum up, the utility model aims to provide a device is recycled to reforming pre-hydrogenation fractionating tower top heat recovery, can pass through technology and device utilize reforming pre-hydrogenation oil and pre-hydrogenation fractionating tower top oil gas heat transfer, through the heat transfer volume of three way control valve control reforming pre-hydrogenation oil simultaneously, fully retrieve the heat of pre-hydrogenation fractionating tower top oil gas, reforming pre-hydrogenation oil temperature will be improved to 60 ℃ -80 ℃ by 30 ℃ -50 ℃, then respectively with pre-hydrogenation fractionating tower bottom commodity circulation and the heat transfer of strip tower bottom commodity circulation, the heat transfer difference in temperature has been reduced, improved strip tower and pre-hydrogenation fractionating tower feed temperature, thereby reduce the bottom heat load of tower, still can improve reforming heat feed temperature simultaneously, reduce reforming reaction feeding heating furnace heat load, have obvious energy-conserving effect.
The foregoing is a more detailed description of the present invention, taken in conjunction with the specific preferred embodiments thereof, and it is not intended that the invention be limited to the specific embodiments shown and described. To the utility model belongs to the technical field of ordinary technical personnel, do not deviate from the utility model discloses under the prerequisite of design, can also make a plurality of simple deductions or replacement, all should regard as belonging to the utility model discloses a protection scope.
Claims (10)
1. A device for recycling the heat of the top of a reforming pre-hydrogenation fractionating tower is characterized by comprising:
the system comprises a pre-hydrogenation fractionating tower (3), wherein a tower bottom heating furnace (9) for circulating heating is arranged at the bottom of the pre-hydrogenation fractionating tower (3);
the first heat exchanger (1) comprises a first heat exchange pipeline (11) and a second heat exchange pipeline (12), the first heat exchange pipeline (11) of the first heat exchanger (1) is communicated with the top end of the pre-hydrogenation fractionating tower (3) and the air cooler (4), and the air cooler (4) sequentially passes through the tower top water cooler (5) and the reflux tank (6) and then reflows to the upper part of the pre-hydrogenation fractionating tower (3); and
the second heat exchanger (2) comprises a third heat exchange pipeline (21) and a fourth heat exchange pipeline (22), one end of the third heat exchange pipeline (21) of the second heat exchanger (2) is communicated with the second heat exchange pipeline (12) after heat exchange of the first heat exchanger (1), and one end of the fourth heat exchange pipeline (22) of the second heat exchanger (2) is communicated with a third tee joint (19) between the bottom end of the pre-hydrogenation fractionating tower (3) and the tower bottom heating furnace (9).
2. The apparatus for recovering and reusing the heat of the top of a reforming pre-hydrogenation fractionation tower according to claim 1, wherein:
a first port and a second port of the three-way valve (14) are connected in series with a second heat exchange pipeline (12) of the first heat exchanger (1) which does not exchange heat, and a third port of the three-way valve (14) is communicated with a first three-way node (15) between the second heat exchange pipeline (12) of the first heat exchanger (1) after heat exchange and a third heat exchange pipeline (21) of the second heat exchanger (2); and
and the temperature control unit (13) is arranged between the first three-way joint (15) and a third heat exchange pipeline (21) of the second heat exchanger (2), and the temperature control unit (13) is electrically connected with the three-way valve (14).
3. The apparatus for recovering and reusing the heat of the top of a reforming pre-hydrogenation fractionation tower according to claim 1, wherein: the first heat exchange pipeline (11) of the first heat exchanger (1) with the top oil gas of the pre-hydrogenation fractionating tower (3) exchanges heat with the second heat exchange pipeline (12) with reforming pre-hydrogenation oil.
4. The apparatus for recovering and reusing the heat of the top of a reforming pre-hydrogenation fractionation tower according to claim 1, wherein: the third heat exchange pipeline (21) of the second heat exchanger (2) with the heated reformed pre-hydrogenated oil exchanges heat with the fourth heat exchange pipeline (22) with the heated discharge at the bottom of the pre-hydrogenation fractionating tower (3).
5. The apparatus for recovering and reusing the heat of the top of a reforming pre-hydrogenation fractionation tower according to claim 1, wherein: the other end of a third heat exchange pipeline (21) of the second heat exchanger (2) is communicated with a stripping tower, and the bottom of the stripping tower is communicated with the middle part of the pre-hydrogenation fractionating tower (3) through a first guide pipe (16).
6. The apparatus for recovering and reusing the heat of the top of a reforming pre-hydrogenation fractionation tower according to claim 1, wherein: the other end of a fourth heat exchange pipeline (22) of the second heat exchanger (2) is respectively communicated with a reforming unit hot feeding pipe and the bottom of a heavy naphtha tank.
7. The apparatus for recycling the heat of the top of the reforming pre-hydrogenation fractionation tower as claimed in claim 6, wherein: and a tower bottom water cooler (10) is arranged between a fourth heat exchange pipeline (22) of the second heat exchanger (2) and the bottom of the heavy naphtha tank.
8. The apparatus for recycling the overhead heat of the reforming pre-hydrogenation fractionation tower according to claim 1, further comprising: and one end of the second guide pipe (17) is communicated with a second three-way node (18) between the reflux pump (7) and the upper part of the pre-hydrogenation fractionating tower (3), and the other end of the second guide pipe (17) is communicated with the light naphtha tank.
9. The apparatus for recycling the overhead heat of the reforming pre-hydrogenation fractionation tower according to claim 8, further comprising: and the return pump (7) is connected to a pipeline between the return tank (6) and the second three-way node (18).
10. The apparatus for recycling the overhead heat of the reforming pre-hydrogenation fractionation tower according to claim 1, further comprising: and the tower bottom pump (8) is connected to a pipeline between the bottom end of the pre-hydrogenation fractionating tower (3) and the third tee joint (19).
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| CN201921444241.XU CN210560266U (en) | 2019-09-02 | 2019-09-02 | Device for recycling and reusing heat at top of reforming pre-hydrogenation fractionating tower |
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