CN214634104U - Isomerization reaction system - Google Patents
Isomerization reaction system Download PDFInfo
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- CN214634104U CN214634104U CN202023200587.0U CN202023200587U CN214634104U CN 214634104 U CN214634104 U CN 214634104U CN 202023200587 U CN202023200587 U CN 202023200587U CN 214634104 U CN214634104 U CN 214634104U
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Abstract
The utility model relates to a petrochemical technical field specifically is an isomerization reaction system, isomerization feeding buffer tank is connected to through taking off heptane rectifying column charging line and takes off the heptane rectifying column, takes off the heptane rectifying column and is connected to isomerization carclazyte tower through taking off heptane rectifying column discharging line, and isomerization carclazyte tower is connected to the absorption feed tank through isomerization carclazyte tower discharging line, takes off heptane rectifying column charging line and is connected to isomerization carclazyte tower discharging line through the overline. The device can eliminate the liquid impact hidden trouble of the pipeline, and reduce the shutdown and accident potential safety hazard of the device, thereby achieving the purpose of maintaining long-period safe operation.
Description
Technical Field
The utility model relates to a petrochemical technical field specifically is an isomerization reaction system.
Background
Aromatic hydrocarbons generally refer to hydrocarbons having a benzene ring or aromatic ring structure in the molecule, and are one of closed-chain hydrocarbons having a benzene ring basic structure. The aromatic hydrocarbon comprises a benzene derivative "para-xylene", which is one of the xylene isomers, the remaining isomers including ortho-xylene and meta-xylene.
The method is characterized in that the aromatic hydrocarbon production process generally needs to be carried out through the steps of fractionation, isomerization, adsorption, extraction, disproportionation and the like, each unit is independently circulated during the start-up period of an aromatic hydrocarbon production device, common circulation (long circulation) among the units needs to be established after each unit of the aromatic hydrocarbon production device is heated, and materials in a feed line from an adsorption unit to an isomerization unit are not heated during the independent circulation period, so that a large amount of cold materials in a circulating material line between the two units can cause pipeline liquid impact and weld joint cracking and leakage. Particularly, the whole pipeline of the feeding line of the deheptanide rectifying tower has the possibility of liquid impact, for example, the welded pipe of a pressure gauge on the pipeline is broken by vibration, and other welded junctions of the whole pipeline have risks.
Disclosure of Invention
In view of prior art's defect, the utility model provides an isomerization reaction system, it can be got rid of the liquid attack hidden danger of absorption unit to isomerization unit pipeline, reduces device shut down and accident potential safety hazard to the mesh of maintaining long period safe operation has been reached.
In order to reach above-mentioned purpose, the utility model provides a technical scheme is an isomerization reaction system, isomerization feeding buffer tank is connected to through taking off heptane rectifying column charge-in line and takes off heptane rectifying column, takes off heptane rectifying column and is connected to isomerization carclazyte tower through taking off heptane rectifying column discharge pipeline, and isomerization carclazyte tower is connected to the absorption feed tank through isomerization carclazyte tower discharge pipeline, takes off heptane rectifying column charge-in line to be connected to isomerization carclazyte tower discharge pipeline through the overline.
Furthermore, a first valve, a first guiding and leaching valve and a second valve are sequentially arranged on the cross-line from one end of a feeding pipeline of the heptane-removing rectifying tower to one end of a discharging pipeline of the isomerization clay tower.
Further, an isomerization feed pump is arranged on the feed pipeline of the deheptanide rectification tower close to the outlet pipe section of the isomerization feed buffer tank.
Furthermore, a fourth flow regulating valve group is arranged on a feeding pipeline of the deheptanization rectifying tower close to the outlet of the isomerization feed pump.
Further, the isomerization feed pump outlet is connected to the isomerization feed buffer tank feed line through a recycle line.
Further, the discharge pipeline of the isomerization clay tower is connected to the circulation pipeline through a return pipeline, and a first flow regulating valve group is arranged on the section of the circulation pipeline from the outlet of the isomerization feed pump to the joint of the return pipeline.
Furthermore, a second flow regulating valve group is arranged on the return pipeline.
Furthermore, a third flow regulating valve group is arranged on a discharge pipe line of the isomerization clay tower in front of the adsorption feeding tank.
Furthermore, a fifth flow regulating valve group is arranged on an isomerization clay tower discharge pipe line between the reflux pipeline joint and the third flow regulating valve group.
Furthermore, an outlet of the isomerization feed pump is connected to an outlet pipeline of the isomerization clay tower through an isolation pipeline, the isolation pipeline is connected to a pipe section of the outlet pipeline of the isomerization clay tower between the fifth flow regulating valve group and the third flow regulating valve group through a feeding pipeline of a deheptanization rectification tower at the outlet of the isomerization feed pump, and a sixth flow regulating valve group is arranged on the isolation pipeline.
The utility model has the advantages that: during start-up, the overlines are circularly heated during the heating of each unit, so that the problem of pipeline liquid impact caused by the intersection of cold and hot materials in the pipeline at the later stage is solved.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic view of a first flow regulating valve set;
fig. 3 is a schematic structural view of a second flow regulating valve group, a fourth flow regulating valve group and a fifth flow regulating valve group;
FIG. 4 is a schematic diagram of a third flow regulating valve set;
in the figure: 1. an isomerization feeding buffer tank, 2, a heptane-removing rectifying tower feeding pipeline, 2.1, a fourth flow regulating valve bank, 3, a heptane-removing rectifying tower, 4, a heptane-removing rectifying tower discharging pipeline, 5, an isomerization clay tower, 6, an isomerization clay tower discharging pipeline, 6.1, a third flow regulating valve bank, 6.2, a fifth flow regulating valve bank, 7, an adsorption feeding tank, 8, a crossover line, 8.1, a first valve, 8.2, a first guide shower valve, 8.3, a second valve, 9, an isomerization feeding pump, 10, a circulation pipeline, 10.1, a first flow regulating valve bank, 11, an isomerization feeding buffer tank feeding pipeline, 12, a reflux pipeline, 12.1, a second flow regulating valve bank, 13, an isolation pipeline, 13.1, a sixth residual liquid flow regulating valve bank, 14 and a tower pumping.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
An isomerization reaction system is characterized in that an isomerization feed buffer tank 1 is connected to a heptane-removing rectifying tower 3 through a heptane-removing rectifying tower feed pipeline 2, the heptane-removing rectifying tower 3 is connected to an isomerization clay tower 5 through a heptane-removing rectifying tower discharge pipeline 4, the isomerization clay tower 5 is connected to an adsorption feed tank 7 through an isomerization clay tower discharge pipeline 6, and the heptane-removing rectifying tower feed pipeline 2 is connected to the isomerization clay tower discharge pipeline 6 through a cross line 8.
Furthermore, a first valve 8.1, a first leaching valve 8.2 and a second valve 8.3 are sequentially arranged on the cross line 8 from one end of the feeding pipeline 2 of the heptane-removing rectifying tower to one end of the discharging pipeline 6 of the isomerization clay tower.
In this embodiment, after the first valve 8.1, the first pilot valve 8.2, and the second valve 8.3 are provided, a cycle from the bottom of the heptane-removing rectifying tower 3 to the feeding line of the heptane-removing rectifying tower 3 can be established by the bottom pump of the heptane-removing rectifying tower 3, so that the feeding line of the heptane-removing rectifying tower 3 is heated at the initial stage of start-up, and it is ensured that no liquid impact occurs in the feeding line of the heptane-removing rectifying tower 3 when a unit element cycle (long cycle) is established at the later stage.
Further, an isomerization feed pump 9 is arranged on the feed pipeline 2 of the deheptanizer rectification tower close to the outlet pipe section of the isomerization feed buffer tank 1.
Further, the upstream feeding device of the isomerization feeding buffer tank 1 is a raffinate tower 14, which is the material after the target product of the adsorption unit is separated.
Furthermore, a fourth flow regulating valve group 2.1 is arranged on a feed pipeline 2 of the deheptanizer rectification tower close to the outlet of the isomerization feed pump 9.
Further, the outlet of the isomerization feed pump 9 is connected to an isomerization feed buffer tank feed line 11 through a recycle line 10.
Further, the isomerization clay tower discharge pipeline 6 is connected to the circulation pipeline 10 through a return pipeline 12, and a first flow regulating valve group 10.1 is arranged on the section of the circulation pipeline 10 from the outlet of the isomerization feed pump 9 to the joint of the return pipeline 12.
Furthermore, a second flow regulating valve group 12.1 is arranged on the return line 12.
Further, a third flow regulating valve group 6.1 is arranged on an isomerization clay tower discharge pipeline 6 in front of the adsorption feed tank 7.
Furthermore, a fifth flow regulating valve group 6.2 is arranged on an isomerized clay tower discharging pipeline 6 between the joint of the return pipeline 12 and the third flow regulating valve group 6.1.
Further, an outlet of the isomerization feed pump 9 is connected to the isomerization clay tower discharge pipeline 6 through an isolation pipeline 13, the isolation pipeline 13 is connected to a pipe section of the isomerization clay tower discharge pipeline 6 between the fifth flow regulating valve bank 6.2 and the third flow regulating valve bank 6.1 through a heptane-removing rectification tower feed pipeline 2 at the outlet of the isomerization feed pump 9, and a sixth flow regulating valve bank 13.1 is arranged on the isolation pipeline 13.
It should be noted that fig. 2 is a schematic structural diagram of a first flow rate regulating valve set; in the figure, the first flow rate control valve group includes a gate valve V1, a gate valve V2, a ball valve V3, and a diaphragm valve FV 1.
Fig. 3 is a schematic structural view of a second flow regulating valve group, a fourth flow regulating valve group and a fifth flow regulating valve group; the flow regulating valve group comprises a gate valve V4, a one-way valve V5, a ball valve V6, a splayed blind plate M1 and a pilot shower valve V5.
FIG. 4 is a schematic diagram of a third flow regulating valve set; the third flow regulating valve group comprises a gate valve V8, a gate valve V9, a diaphragm valve FV2 and a ball valve V10.
As shown in fig. 1, the material flowing out from the isomerization feed buffer tank 1 is conveyed to the deheptanization rectification tower 3 from a deheptanization rectification tower feed pipeline 2 by an isomerization feed pump 9, the deheptanization rectification tower 3 discharges materials to an isomerization clay tower 5 through a deheptanization rectification tower discharge pipeline 4, the isomerization clay tower 5 is connected to an adsorption feed tank 7 through an isomerization clay tower discharge pipeline 6, in the embodiment, the deheptanization rectification tower feed pipeline 2 is connected to the isomerization clay tower discharge pipeline 6 through a crossover 8 aiming at the liquid impact phenomenon occurring during the starting, and the materials in the deheptanization rectification tower feed pipeline 2 can be heated together through the crossover 8 during the temperature rise of the device, so that the liquid impact problem of the pipeline during the establishment of the long circulation of the device can be avoided. The crossover wire 8 in the embodiment is used when working and heating, and does not need to be fed with materials at ordinary times.
It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (9)
1. An isomerization reaction system characterized by: the isomerization feeding buffer tank is connected to the deheptanization rectifying tower through a deheptanization rectifying tower feeding pipeline, the deheptanization rectifying tower is connected to the isomerization clay tower through a deheptanization rectifying tower discharging pipeline, the isomerization clay tower is connected to the adsorption feeding tank through an isomerization clay tower discharging pipeline, and the deheptanization rectifying tower feeding pipeline is connected to the isomerization clay tower discharging pipeline through a cross line.
2. An isomerization reaction system as defined in claim 1 wherein: and an isomerization feed pump is arranged on the feed pipeline of the heptane-removing rectifying tower close to the outlet pipe section of the isomerization feed buffer tank.
3. An isomerization reaction system as defined in claim 2 wherein: and a fourth flow regulating valve group is arranged on the feeding pipeline of the deheptanization rectifying tower close to the outlet of the isomerization feeding pump.
4. An isomerization reaction system as defined in claim 2 wherein: the isomerization feed pump outlet is connected to the isomerization feed surge tank feed line by a recycle line.
5. An isomerization reaction system as defined in claim 4 wherein: the isomerization clay tower discharge pipeline is connected to the circulation pipeline through a return pipeline, and a first flow regulating valve group is arranged on a section of the circulation pipeline from the outlet of the isomerization feed pump to the joint of the return pipeline.
6. An isomerization reaction system as defined in claim 5 wherein: and a second flow regulating valve group is arranged on the return pipeline.
7. An isomerization reaction system as defined in claim 5 wherein: and a third flow regulating valve group is arranged on a discharge pipe line of the isomerization clay tower in front of the adsorption feeding tank.
8. An isomerization reaction system as defined in claim 7 wherein: and a fifth flow regulating valve bank is arranged on an isomerization clay tower discharge pipe line between the reflux pipeline joint and the third flow regulating valve bank.
9. An isomerization reaction system as defined in claim 8 wherein: the isomerization feed pump outlet is connected to an isomerization clay tower discharge pipeline through an isolation pipeline, the isolation pipeline is connected to an isomerization clay tower discharge pipeline section between the fifth flow regulating valve group and the third flow regulating valve group through a heptane-removing rectification tower feed pipeline of the isomerization feed pump outlet, and a sixth flow regulating valve group is arranged on the isolation pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202023200587.0U CN214634104U (en) | 2020-12-28 | 2020-12-28 | Isomerization reaction system |
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| CN202023200587.0U CN214634104U (en) | 2020-12-28 | 2020-12-28 | Isomerization reaction system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625741A (en) * | 2020-12-28 | 2021-04-09 | 大连福佳·大化石油化工有限公司 | Isomerization reaction system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625741A (en) * | 2020-12-28 | 2021-04-09 | 大连福佳·大化石油化工有限公司 | Isomerization reaction system |
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