CN217979918U - Hydrogenation heat exchange assembly and hydrogenation heat exchange system with same - Google Patents
Hydrogenation heat exchange assembly and hydrogenation heat exchange system with same Download PDFInfo
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- CN217979918U CN217979918U CN202222116301.3U CN202222116301U CN217979918U CN 217979918 U CN217979918 U CN 217979918U CN 202222116301 U CN202222116301 U CN 202222116301U CN 217979918 U CN217979918 U CN 217979918U
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Abstract
A hydrogenation heat exchange assembly comprises a heat exchange device, a raw oil main pipeline and a hydrogen main pipeline, wherein the output end of the raw oil main pipeline is connected with a first raw oil pipeline and a second raw oil pipeline; the output end of the hydrogen main pipeline is connected with a first hydrogen pipeline and a second hydrogen pipeline; first valves are arranged on the first raw material oil pipeline, the second raw material oil pipeline, the first hydrogen pipeline and the second hydrogen pipeline; the heat exchange device is a wound tube type heat exchanger with a shell pass and two tube passes, the two tube passes are a first tube pass and a second tube pass, the inlet end of the first tube pass is communicated with the outlet end of the first raw material oil pipeline and the outlet end of the first hydrogen pipeline, and the inlet end of the second tube pass is communicated with the outlet ends of the second raw material oil pipeline and the second hydrogen pipeline. The application also discloses a hydrogenation heat exchange system with the hydrogenation heat exchange assembly. Compared with the prior art, the heat exchanger in the application can adapt to load fluctuation and realize the conversion of different processing technologies of the front hydrogen mixing and the rear hydrogen mixing.
Description
Technical Field
The utility model belongs to the technical field of the heat transfer, concretely relates to hydrogenation heat transfer subassembly and have hydrogenation heat transfer system of this subassembly.
Background
Hydrotreating is one of the more important treatment methods in petroleum products, and means that under certain temperature, hydrogen partial pressure and catalyst conditions, heteroatoms such as sulfur, nitrogen, oxygen and the like and metal impurities in the oil product are removed, so that olefin is saturated, and aromatic hydrocarbons are partially subjected to hydrogenation saturation, thereby improving the service performance of the oil product.
The hydrotreating process comprises the following steps: mixing the oil product with hydrogen, feeding the mixture into a heating furnace, heating the mixture to a specified temperature, and then feeding the mixture into a reactor filled with a catalyst; after the reaction is finished, hydrogen is separated in a separator and recycled by a compressor; the product is separated into hydrogen sulfide, ammonia, water and gaseous hydrogen generated by small amount decomposition in the reaction process in a stabilizing tower.
The prior hydrogenation heat exchange system is disclosed in patent application CN202110477804.0, namely, the invention heat exchange system and process using multi-strand wound tubular heat exchanger (application publication No. CN 113063309A) and patent application CN202110477790.2, namely, the invention heat exchange system and process for hydrogenation process (application publication No. CN 113267075A).
The work load of the heat exchanger in the existing hydrogenation heat exchange system generally needs to be maintained between 60% and 110% of the design load, and when the work period is in operation or the raw material supply is insufficient, the work load of the heat exchanger is difficult to be maintained above 60%. The low-load operation often causes the occurrence of scaling and coking in the heat exchanger, so that the whole system is difficult to operate for a long time.
SUMMERY OF THE UTILITY MODEL
The utility model discloses the first technical problem that will solve is the current situation to prior art, provides a hydrogenation heat transfer subassembly to it is undulant to make the heat exchanger can adapt to the load.
The utility model aims to solve the second technical problem that a hydrogenation heat transfer system with above-mentioned hydrogenation heat transfer subassembly is provided.
The utility model provides a technical scheme that above-mentioned first technical problem adopted is: the utility model provides a hydrogenation heat transfer subassembly, is including heat transfer device, the raw oil main line that is used for carrying raw oil, the hydrogen main line that is used for carrying hydrogen, its characterized in that:
the output end of the raw oil main pipeline is connected with a first raw oil pipeline and a second raw oil pipeline;
the output end of the hydrogen main pipeline is connected with a first hydrogen pipeline and a second hydrogen pipeline;
the first raw material oil pipeline, the second raw material oil pipeline, the first hydrogen pipeline and the second hydrogen pipeline are respectively provided with a first valve for controlling the flow;
the heat exchange device is a wound tube type heat exchanger with a shell pass and two tube passes, the two tube passes are a first tube pass and a second tube pass, the inlet end of the first tube pass is communicated with the outlet end of the first raw material oil pipeline and the outlet end of the first hydrogen pipeline, and the inlet end of the second tube pass is communicated with the outlet end of the second raw material oil pipeline and the outlet end of the second hydrogen pipeline.
The "hydrogen" in the present application may be recycle hydrogen (which may contain impurities) output from a hydrogenation apparatus, or hydrogen directly externally input.
In order to ensure the heat exchange effect, preferably, the heat exchange tubes of the wound tube heat exchanger are spirally wound into a plurality of layers of spiral tubes from inside to outside layer by layer, the heat exchange tubes of the first tube pass and the second tube pass are arranged in each layer of spiral tube, and the heat exchange tubes of the first tube pass and the second tube pass are uniformly distributed in each layer of spiral tube. Therefore, the shell side medium and the medium of each layer of spiral tube can exchange heat uniformly, and particularly, when raw oil and hydrogen are introduced into the first tube side and only a small amount of hydrogen is introduced into the second tube side, the heat exchange effect can be effectively ensured.
Preferably, the raw oil main pipeline and the hydrogen main pipeline are both provided with second valves for controlling flow.
Furthermore, the outlet end of the first tube pass and the outlet end of the second tube pass are independently separated to form two paths;
or the outlet end of the first tube pass and the outlet end of the second tube pass are combined into one path.
Preferably, the outlet end of the first tube side and the outlet end of the second tube side are independently separated to form two paths, and the hydrogenation heat exchange assembly further comprises:
the input end of the first raw oil bypass pipeline is communicated with the first raw oil pipeline and is positioned between the inlet end of the first raw oil pipeline and a first valve on the first raw oil pipeline; the output end of the first tube pass is communicated with the outlet end of the first tube pass;
the input end of the second raw oil bypass pipeline is communicated with the second raw oil pipeline and is positioned between the inlet end of the second raw oil pipeline and the first valve on the second raw oil pipeline; the output end of the second tube pass is communicated with the outlet end of the second tube pass;
and third valves for controlling the flow are arranged on the first raw oil bypass pipeline and the second raw oil bypass pipeline. Therefore, the third valve can be controlled according to the tube side outlet temperature of the heat exchanger, and if the tube side outlet temperature of the heat exchanger is higher, the corresponding third valve can be opened, so that the low-temperature raw oil which does not exchange heat is mixed with the medium at the tube side outlet, and the temperature of the medium at the tube side outlet is reduced.
Also preferably, the outlet end of the first tube pass and the outlet end of the second tube pass are merged into a single tube; the hydrogenation heat exchange assembly also comprises:
the input end of the third raw oil bypass pipeline is communicated with the raw oil main pipeline, and the output end of the third raw oil bypass pipeline is communicated with one combined path of the outlet end of the first tube pass and the outlet end of the second tube pass;
and a third valve is arranged on the third raw oil bypass pipeline.
The utility model provides a technical scheme that above-mentioned second technical problem adopted does: a hydrogenation heat exchange system comprises a heating furnace and a hydrogenation reactor communicated with the output end of the heating furnace, and is characterized by further comprising a hydrogenation heat exchange assembly as described above, wherein the outlet end of a first tube pass and the outlet end of a second tube pass are communicated with the input end of the heating furnace, the inlet end of the shell pass of a heat exchange device is communicated with the output end of the hydrogenation reactor, and the outlet end of the shell pass of the heat exchange device is connected to downstream equipment.
Preferably, the system also comprises a heating furnace bypass pipeline, the input end of the heating furnace bypass pipeline is connected to a pipeline between the input end of the heating furnace and the tube pass outlet end of the heat exchange device, and the output end of the heating furnace bypass pipeline is connected to a pipeline between the output end of the heating furnace and the input end of the hydrogenation reactor; and fourth valves for controlling the flow are arranged on the bypass pipeline of the heating furnace and on pipelines between the input end of the heating furnace and the tube pass outlet end of the heat exchange device. Therefore, when the temperature of the medium at the outlet of the tube side is higher, the bypass pipeline of the heating furnace can be directly taken away.
Preferably, the outlet end of the first tube pass and the outlet end of the second tube pass are independently separated to form two paths, the two paths are communicated with the input end of the heating furnace through respective pipelines, the fourth valves are arranged on the two paths of pipelines, the number of the heating furnace bypass pipelines is two, the fourth valves are arranged on the two paths of pipelines, the input ends of the two heating furnace bypass pipelines are respectively communicated with the two paths of pipelines, and the output ends of the two heating furnace bypass pipelines are connected to the pipelines between the output end of the heating furnace and the input end of the hydrogenation reactor. Therefore, the conversion of different processing technologies of the hydrogen mixing before the furnace and the hydrogen mixing after the furnace can be realized according to different working conditions and processed oil products, and the advantages of two hydrogenation technologies can be considered, so that the production is more flexible and the adaptability is wider.
Compared with the prior art, the utility model has the advantages of: by additionally arranging a first raw material oil pipeline, a second raw material oil pipeline, a first hydrogen pipeline, a second hydrogen pipeline and first valves arranged on all pipe boxes, the output ends of the first raw material oil pipeline and the first hydrogen pipeline are connected to a first pipe pass of a heat exchange device, and the output ends of the second raw material oil pipeline and the second hydrogen pipeline are connected to a second pipe pass of the heat exchange device, so that when the heat exchange device is operated under a normal working condition or a high-load working condition, the first valves are opened, and raw material oil and hydrogen are mixed and then flow out of the two pipe passes of the heat exchange device; when the heat exchange device operates under a low-load working condition, the required minimum flow rate requirement can be met by adjusting the flow of gas-liquid phases in different tube passes, if raw oil only passes through the first tube pass, hydrogen passes through the first tube pass and the second tube pass, all raw oil passes through the first tube pass, the flow rate of oil-gas mixture feeding entering the heat exchanger can be ensured to be between 60% and 110% of the normal design, the problem of low-load long-period operation is solved, the flow rate is ensured, and the heat exchange efficiency of the heat exchanger is maintained; because hydrogen passes through the second tube pass, the damage to the heat exchanger caused by long-term bearing of high external pressure and high temperature working conditions when no medium exists in a certain tube pass of the multi-flow heat exchanger is effectively avoided. And the application can realize the conversion of different processing technologies of the hydrogen mixing in front of the furnace and the hydrogen mixing in back of the furnace.
Drawings
Fig. 1 is a schematic structural diagram of a first embodiment of the present invention;
fig. 2 is a schematic structural diagram of a second embodiment of the present invention;
fig. 3 is a schematic structural diagram of a third embodiment of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments.
The first embodiment is as follows:
as shown in fig. 1, for the first preferred embodiment of the hydrogenation heat exchange assembly and the hydrogenation heat exchange system with the same of the present invention, the hydrogenation heat exchange assembly comprises a heat exchange device 1, a raw oil main pipeline 2 for transporting raw oil, a hydrogen main pipeline 3 for transporting hydrogen, a first raw oil bypass pipeline 51, and a second raw oil bypass pipeline 52.
The raw oil main pipeline 2 and the hydrogen main pipeline 3 are both provided with a second valve 42 for controlling the flow. The output end of the raw oil main pipeline 2 is connected with a first raw oil pipeline 21 and a second raw oil pipeline 22. The output end of the hydrogen manifold 3 is connected to a first hydrogen line 31 and a second hydrogen line 32. The first raw material oil line 21, the second raw material oil line 22, the first hydrogen line 31, and the second hydrogen line 32 are provided with first valves 41 for controlling flow rates.
The heat exchange device 1 is a wound tube heat exchanger having a shell side and two tube sides, the two tube sides are a first tube side 11 and a second tube side 12, an inlet end of the first tube side 11 is communicated with an outlet end of a first raw material oil line 21 and an outlet end of a first hydrogen line 31, and an inlet end of the second tube side 12 is communicated with an outlet end of a second raw material oil line 22 and an outlet end of a second hydrogen line 32. The outlet end of the first tube pass 11 and the outlet end of the second tube pass 12 are independently separated to form two paths. In this embodiment, the heat exchange tubes of the wound tube heat exchanger are spirally wound layer by layer from inside to outside to form a plurality of layers of spiral tubes, each layer of spiral tube is provided with the heat exchange tubes of the first tube pass 11 and the second tube pass 12, and the heat exchange tubes of the first tube pass and the second tube pass are the same in number and are alternately and uniformly distributed in each layer of spiral tube.
The input end of the first raw oil bypass line 51 is communicated with the first raw oil line 21 and is located between the input end of the first raw oil line 21 and the first valve 41 on the first raw oil line 21, and the output end of the first raw oil bypass line 51 is communicated with the output end of the first tube side 11. The input end of the second raw oil bypass line 52 is communicated with the second raw oil line 22 and is positioned between the inlet end of the second raw oil line 22 and the first valve 41 on the second raw oil line 22, and the output end of the second raw oil bypass line 52 is communicated with the outlet end of the second tube side 12. Meanwhile, the first stock oil bypass line 51 and the second stock oil bypass line 52 are both provided with a third valve 43 for controlling the flow rate.
The hydrogenation heat exchange system of the embodiment comprises the hydrogenation heat exchange assembly, the heating furnace 6, the hydrogenation reactor 7 and the heating furnace bypass pipeline 8.
Two pipelines coming out of two tube passes of the heat exchanger are combined into one pipeline and then communicated with the input end of the heating furnace 6, the output end of the heating furnace 6 is communicated with the input end of the hydrogenation reactor 7, the output end of the hydrogenation reactor 7 is communicated with the inlet end of the shell pass of the heat exchange device 1, and the outlet end of the shell pass of the heat exchange device 1 is connected to downstream equipment. The downstream equipment is in the prior art and comprises a hot high-pressure separating tank, a hot low-pressure separating tank, an air cooler, a cold low-pressure separating tank and the like, and the details are not repeated herein.
The input end of the heating furnace bypass pipeline 8 is connected to a pipeline between the input end of the heating furnace 6 and the tube pass outlet end of the heat exchange device 1, and the output end of the heating furnace bypass pipeline is connected to a pipeline between the output end of the heating furnace 6 and the input end of the hydrogenation reactor 7; and fourth valves 44 for controlling flow are arranged on the heating furnace bypass pipeline 8 and the pipelines between the input end of the heating furnace 6 and the tube side outlet end of the heat exchange device 1. And a fourth valve 44 on the line between the input of furnace 6 and the tube-side outlet of heat exchange unit 1 is located on the line between the input of furnace 6 and the input of bypass line 8.
The heat exchange process of the embodiment is as follows:
when a first working condition that N is more than or equal to 60% and M is more than or equal to 110% is met between a working load M and a design load N in the wound tube type heat exchanger, each first valve 41 is opened, raw oil and hydrogen are mixed and then flow through two tube passes of the wound tube type heat exchanger, and the hydrogen-oil ratio in each tube pass is 500-1100 Nm 3 /m 3 (the hydrogen-oil ratio may be 500Nm 3 /m 3 、1100Nm 3 /m 3 Or any value between 500 and 1100, specifically designed according to actual working conditions);
when a second working condition that N is more than or equal to 30% and M is less than or equal to 60% is met between the working load M and the design load N in the coiled tube type heat exchanger, the first valve 41 on the first raw material oil pipeline 21 is opened, the first valve 41 on the second raw material oil pipeline 22 is closed, and the first valves 41 on the first hydrogen pipeline and the second hydrogen pipeline are opened, so that the hydrogen is divided into two paths, the first path of hydrogen is mixed with the raw material oil and then flows through the first tube pass, and the hydrogen-oil ratio in the first tube pass is 475-1050 Nm 3 Per m (hydrogen to oil ratio may be 475 Nm) 3 /m 3 、1050Nm 3 /m 3 Or any value between 475 and 1050, specifically designed according to actual working conditions); the second path of hydrogen gas flows through a second tube pass, and the flow velocity of the hydrogen gas in the second tube pass is not lower than 0.1m/s; the hydrogen-oil ratio in the hydrogenation reaction is determined by the performance of the catalyst, when the performance of the catalyst is fixed, the raw oil processing is reduced, and the hydrogen can be synchronously reduced. The raw oil only passes through one tube pass under the second working condition, so that the hydrogen flow rate is not greatly changed compared with the hydrogen flow rate under the first working condition.
When the working load M and the design load N in the wound tube type heat exchanger meet a third working condition that M is more than N110%, each first valve 41 is opened, the raw oil and the hydrogen are mixed and then wound around two tube passes of the wound tube type heat exchanger, and the hydrogen-oil ratio in each tube pass is 450-1000 Nm 3 /m 3 (the hydrogen-oil ratio may be 450Nm 3 /m 3 、1000Nm 3 /m 3 Or anywhere between 450 and 1000, specifically designed according to actual operating conditions). Under the third working condition, the raw oil bypass is closed for sufficient heat exchange, and the hydrogen-oil ratio is reduced at the moment.
In the application, the working load in the wound tube type heat exchanger can be judged according to the proportion of the processed raw oil to the design value. And under each working condition, the pressure and the temperature of the raw oil are generally slightly higher than those of the hydrogen.
In the heat exchanger, the inlet temperature of a tube side is 110-160 ℃, the outlet temperature of the tube side is 320-380 ℃, the inlet temperature of a shell side is 360-420 ℃, the outlet temperature of the shell side is 220-260 ℃ and the operating pressure is 5-20 MPa.
When the winding tube type heat exchanger is switched from high-load (more than or equal to N60%) operation to low-load (less than N60%) operation, firstly cleaning a first tube pass 11, specifically as follows: introducing all raw oil and most hydrogen into a first tube side 11, introducing a small part of hydrogen with the flow rate of 0.1m/s into a second tube side 12 (note that except for ensuring that the hydrogen with the low flow rate of 0.1-0.7 m/s exists in the second tube side, all other hydrogen is introduced into the first tube side, the temperature and the pressure of the raw oil and the hydrogen are unchanged), maintaining for 48-72 h, introducing all hydrogen into the first tube side 11, introducing all the raw oil into the second tube side 12, and maintaining for 12-24 h, and then finishing the cleaning of the first tube side 11;
and then cleaning a second tube pass, which comprises the following steps: introducing all raw oil and most hydrogen into a second tube side 12, introducing a small part of hydrogen with the flow rate of 0.1-0.7 m/s into a first tube side 11 (note: except for ensuring that the hydrogen with the low flow rate of 0.1-0.7 m/s exists in the first tube side, all other hydrogen is introduced into the second tube side, and the temperature and the pressure of the raw oil and the hydrogen are unchanged), and finishing the cleaning of the second tube side 12 after maintaining for 48-72 h.
The second embodiment:
as shown in fig. 2, for the utility model discloses a hydrogenation heat transfer subassembly and have hydrogenation heat transfer system's of this subassembly preferred embodiment two, this embodiment is the same basically with embodiment one, the difference lies in this embodiment, the exit end of first tube side 11, the exit end of second tube side 12 is for independently separately and form two the tunnel, two tunnel are linked together through respective pipeline and heating furnace 6's input, and all be equipped with foretell fourth valve 44 on two tunnel pipelines, heating furnace bypass pipeline 8 also has two, and all be equipped with fourth valve 44, two heating furnace bypass pipeline 8's input is linked together with two tunnel pipelines that correspond respectively, the output is connected on the pipeline between heating furnace 6's output and hydrogenation ware 7's input.
Example three:
as shown in fig. 3, it is a third preferred embodiment of the hydrogenation heat exchange assembly and the hydrogenation heat exchange system having the same of the present invention, the present embodiment is basically the same as the first embodiment, and the difference lies in that in the present embodiment, the outlet end of the first tube side 11 and the outlet end of the second tube side 12 are combined into one path, and the combined pipeline is communicated with the stock oil main pipeline 2 through a third stock oil bypass pipeline 53, and a third valve 43 is disposed on the third stock oil bypass pipeline 53.
Claims (9)
1. The utility model provides a hydrogenation heat transfer subassembly, is including heat transfer device (1), raw oil main line (2) for carrying raw oil, hydrogen main line (3) for carrying hydrogen, its characterized in that:
the output end of the raw oil main pipeline (2) is connected with a first raw oil pipeline (21) and a second raw oil pipeline (22);
the output end of the hydrogen main pipeline (3) is connected with a first hydrogen pipeline (31) and a second hydrogen pipeline (32);
the first raw material oil pipeline (21), the second raw material oil pipeline (22), the first hydrogen pipeline (31) and the second hydrogen pipeline (32) are respectively provided with a first valve (41) for controlling the flow;
the heat exchange device (1) is a wound tube type heat exchanger with a shell pass and two tube passes, the two tube passes are a first tube pass (11) and a second tube pass (12), the inlet end of the first tube pass (11) is communicated with the outlet end of a first raw material oil pipeline (21) and the outlet end of a first hydrogen pipeline (31), and the inlet end of the second tube pass (12) is communicated with the outlet end of a second raw material oil pipeline (22) and the outlet end of a second hydrogen pipeline (32).
2. The hydrogenation heat exchange assembly of claim 1, wherein: the heat exchange tubes of the wound tube heat exchanger are spirally wound into a plurality of layers of spiral tubes from inside to outside layer by layer, the heat exchange tubes of a first tube pass (11) and a second tube pass (12) are arranged in each layer of spiral tube, and the heat exchange tubes of the first tube pass and the second tube pass are uniformly distributed in each layer of spiral tube.
3. The hydrogenation heat exchange assembly of claim 1, wherein: and the raw oil main pipeline (2) and the hydrogen main pipeline (3) are respectively provided with a second valve (42) for controlling the flow.
4. The hydrogenation heat exchange assembly of claim 1, wherein: the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12) are independently separated to form two paths;
or the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12) are combined into a whole.
5. The hydrogenation heat exchange assembly of claim 4, wherein: the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12) are independently separated to form two paths, and the hydrogenation heat exchange assembly further comprises:
a first feed oil bypass line (51) having an input end in communication with the first feed oil line (21) and located between the inlet end of the first feed oil line (21) and a first valve (41) on the first feed oil line (21); the output end of the first tube pass is communicated with the outlet end of the first tube pass (11);
a second feedstock bypass line (52) having an input end in communication with the second feedstock line (22) and located between the inlet end of the second feedstock line (22) and the first valve (41) on the second feedstock line (22); the output end of the first tube pass is communicated with the outlet end of the second tube pass (12);
the first stock oil bypass line (51) and the second stock oil bypass line (52) are each provided with a third valve (43) for controlling the flow rate.
6. The hydrogenation heat exchange assembly of claim 4, wherein: the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12) are combined into a single path; the hydrogenation heat exchange component also comprises:
a third raw oil bypass pipeline (53), the input end of which is communicated with the raw oil main pipeline (2), and the output end of which is communicated with a combined path of the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12);
and a third valve (43) is arranged on the third raw oil bypass pipeline (53).
7. A hydrogenation heat exchange system comprises a heating furnace (6) and a hydrogenation reactor (7) communicated with the output end of the heating furnace (6), and is characterized by further comprising a hydrogenation heat exchange assembly according to claims 4-6, wherein the outlet end of a first tube pass (11) and the outlet end of a second tube pass (12) are communicated with the input end of the heating furnace (6), the inlet end of the shell pass of a heat exchange device (1) is communicated with the output end of the hydrogenation reactor (7), and the outlet end of the shell pass of the heat exchange device (1) is connected to downstream equipment.
8. The hydrogenation heat exchange system of claim 7, wherein: the heat exchanger also comprises a heating furnace bypass pipeline (8), the input end of the heating furnace bypass pipeline is connected to a pipeline between the input end of the heating furnace (6) and the tube pass outlet end of the heat exchanger (1), and the output end of the heating furnace bypass pipeline is connected to a pipeline between the output end of the heating furnace (6) and the input end of the hydrogenation reactor (7); and fourth valves (44) for controlling the flow are arranged on the heating furnace bypass pipeline (8) and the pipeline between the input end of the heating furnace (6) and the tube pass outlet end of the heat exchange device (1).
9. The hydroprocessing heat exchange system of claim 8, wherein: the outlet end of the first tube pass (11) and the outlet end of the second tube pass (12) are independently separated to form two paths of pipelines, the two paths of pipelines are communicated with the input end of the heating furnace (6) through respective pipelines, the four valves (44) are arranged on the two paths of pipelines, the number of the heating furnace bypass pipelines (8) is two, the four valves (44) are arranged, the input ends of the two heating furnace bypass pipelines (8) are communicated with the corresponding two paths of pipelines respectively, and the output ends of the two heating furnace bypass pipelines are connected to the pipelines between the output end of the heating furnace (6) and the input end of the hydrogenation reactor (7).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222116301.3U CN217979918U (en) | 2022-08-11 | 2022-08-11 | Hydrogenation heat exchange assembly and hydrogenation heat exchange system with same |
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| CN202222116301.3U CN217979918U (en) | 2022-08-11 | 2022-08-11 | Hydrogenation heat exchange assembly and hydrogenation heat exchange system with same |
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