System for improving hydrogen yield and aromatic hydrocarbon yield by utilizing first-section cold separation oil conveying for reforming

Abstract

The utility model belongs to the field of petrochemical oil refining, and particularly relates to a system for improving hydrogen yield and aromatic hydrocarbon yield by utilizing one-section cold separation oil conveying for reforming. The second valve is connected with the cold high-pressure oil separation tank; the three-way pipe is connected with the second valve; the mixer is connected with the three-way pipe and is used for mixing the first-section cold separation oil and the mixed naphtha; according to the utility model, one section of cold separation oil after gasoline hydrodesulfurization is changed into reforming for pre-hydrogenation, so that on one hand, the feeding amount of a gasoline hydrogenation second-section hydrodesulfurization reaction system is reduced, the processing load of the reaction system is reduced, and the gas consumption of a heating furnace, the air cooling power consumption and the circulating water consumption of a water cooler are gradually reduced; the reaction depth reduces the activity of the catalyst, the service life of the catalyst is prolonged in a phase-changing manner, a part of benefits are brought to cost reduction and efficiency improvement of the device, and on the other hand, after the reforming load is improved, the hydrogen yield is increased, and the aromatic hydrocarbon yield is increased.

Description

Technical Field

[0001] The utility model relates to the technical field of petrochemical oil refining, in particular to a system for improving hydrogen production and aromatic hydrocarbon yield by utilizing a first stage cold oil separation, transportation and reforming. Background Art

[0002] Due to market changes, in order to respond to the market and optimize the operation of the entire plant and reduce the processing load of some units, the upstream units will reduce the direct feed of reforming after adjusting the load, and the hydrogen production of the units at low load will be reduced. A set of dry gas hydrogen production units in the plant is still in a shutdown state, and the insufficient hydrogen consumption restricts the diesel hydrotreating unit from operating at full load. Therefore, we proposed a system that uses a one-stage cold oil separation to transport to reforming to increase hydrogen production and aromatics yield to solve the above problems. Utility Model Content

[0003] The purpose of the utility model is to solve the shortcomings of the prior art and to propose a system that utilizes a stage of cold oil separation for transportation and reforming to increase hydrogen production and aromatics yield.

[0004] In order to achieve the above purpose, the present invention adopts the following technical solutions:

[0005] A system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation and transportation for reforming, comprising:

[0006] Cold high-pressure oil tank;

[0007] The second valve is connected to the cold high-pressure oil tank;

[0008] A tee pipe connected to the second valve;

[0009] A mixer connected to the tee pipe is used to mix the first stage cold separated oil and the mixed naphtha;

[0010] The naphtha buffer tank is connected to the mixer, and a regulating valve is provided between the naphtha buffer tank and the mixer.

[0011] Preferably, the system further comprises a reformer, and the mixer is located in the reformer.

[0012] Preferably, the reformer is provided with a mixed naphtha line, and the tee pipe is connected to the mixer via the mixed naphtha line.

[0013] Preferably, a first valve is provided on the mixed naphtha line.

[0014] Preferably, the three-way pipe is connected to a collecting pipe, and a third valve is provided between the three-way pipe and the collecting pipe.

[0015] Preferably, an interface pipe is connected to the reforming device.

[0016] In the present invention, the beneficial effects of the system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation and transportation for reforming are as follows:

[0017] The utility model changes the first-stage cold oil separation after gasoline hydrodesulfurization into reforming and pre-hydrogenation. On the one hand, the feed amount of the gasoline hydrogenation second-stage hydrodesulfurization reaction system is reduced, the processing load of the reaction system is reduced, the gas consumption of the heating furnace, the power consumption of the air cooling (frequency conversion), and the circulating water consumption of the water cooler are gradually reduced, the reaction depth is reduced, the catalyst activity is not so intense, and the service life of the catalyst is extended in disguise, which brings some benefits to the cost reduction and efficiency improvement of the device. On the other hand, after the reforming load is increased, the hydrogen production is increased and the aromatics yield is increased. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 This is a block diagram of a system proposed by the utility model for increasing hydrogen production and aromatics yield by utilizing a first stage of cold oil separation for transportation and reforming.

[0019] In the figure: 1. Cold high-pressure separation oil tank; 2. First valve; 3. Second valve; 4. Tee; 5. Third valve; 6. Collecting pipe; 7. Mixer; 8. Interface pipe; 9. First section of cold oil separation delivery line; 10. Reforming unit; 11. Mixed naphtha line; 12. Naphtha buffer tank; 13. Control valve. DETAILED DESCRIPTION

[0020] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments.

[0021] Reference Figure 1 , a system that uses a cold oil separation tank to transport and reform to increase hydrogen production and aromatics yield, cold high-pressure oil tank 1;

[0022] The second valve 3 is connected to the cold high-pressure separation oil tank 1;

[0023] A three-way pipe 4 connected to the second valve 3;

[0024] Mixer 7, connected to the tee pipe 4, for mixing the first stage cold oil separation and the mixed naphtha;

[0025] The naphtha buffer tank 12 is connected to the mixer 7 , and a regulating valve 13 is provided between the naphtha buffer tank 12 and the mixer 7 .

[0026] In this embodiment, a reforming device 10 is further included, and the mixer 7 is located inside the reforming device 10 .

[0027] In this embodiment, a mixed naphtha line 11 is provided in the reformer 10 , and the tee pipe 4 is connected to the mixer 7 via the mixed naphtha line 11 .

[0028] In this embodiment, a first valve 2 is provided on the mixed naphtha line 11 .

[0029] In this embodiment, the three-way pipe 4 is connected to the collecting pipe 6 , and a third valve 5 is provided between the three-way pipe 4 and the collecting pipe 6 .

[0030] In this embodiment, the reforming device 10 is connected to an interface pipe 8 .

[0031] In this embodiment, a new tee is welded at the bottom of the original hydrodesulfurization post-cooled high-pressure oil tank to the stabilization tower line manifold, and the external pipeline is connected to the boundary of the catalytic gasoline hydrogenation unit at the tee. The pipeline corridor outside the unit is re-laid to the boundary of the reforming unit, connected to the original mixed naphtha line in the reforming boundary and incorporated into the pre-hydrogenation naphtha buffer tank.

[0032] In this embodiment, a section of the cold oil separation delivery line to the second valve 3 to the collecting pipe 6 is not used and is only used during start-up and shutdown. Under normal circumstances, this line section is in an inactive state. The collecting pipe to the stabilizing tower hand valve is closed and locked on the first round on site, and is connected to the reforming process and is normally open.

[0033] The first stage cold separation oil is merged into the mixed naphtha line, and after mixing, it enters the naphtha buffer tank through regulation and control. The normal delivery rate of the first stage cold separation oil is controlled at around 11-15t / h.

[0034] The utility model can make the first stage of cold oil separation go to reforming, and can increase the production of hydrogen and aromatics through adjustment, while improving economic benefits and reducing energy consumption. The process design is simple, the operation is convenient, and the control is flexible.

[0035] The analysis data table of the first stage cold oil separation test data is as follows:

[0036]

[0037] The above is only a preferred specific implementation method of the present invention, but the protection scope of the present invention is not limited to this. Any technician familiar with the technical field within the technical scope disclosed by the present invention can make equivalent replacements or changes based on the technical solution and utility model concept of the present invention, which should be covered by the protection scope of the present invention.

Claims

1. A system for increasing hydrogen production and aromatics yield by utilizing a cold oil separation and reforming, characterized in that: include: Cold high-pressure oil tank (1); A second valve (3) is connected to the cold high-pressure oil tank (1); A three-way pipe (4) connected to the second valve (3); A mixer (7) is connected to the tee pipe (4) and is used to mix the first stage cold oil separation and the mixed naphtha; The naphtha buffer tank (12) is connected to the mixer (7), and a regulating valve (13) is provided between the naphtha buffer tank (12) and the mixer (7).

2. The system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation, transportation and reforming according to claim 1, characterized in that: It also includes a reformer (10), wherein the mixer (7) is located in the reformer (10).

3. The system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation, transportation and reforming according to claim 2, characterized in that: The reformer (10) includes a mixed naphtha line (11), and the tee pipe (4) is connected to the mixer (7) via the mixed naphtha line (11).

4. The system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation, transportation and reforming according to claim 3, characterized in that: The mixed naphtha line (11) is provided with a first valve (2).

5. The system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation, transportation and reforming according to claim 4, characterized in that: The three-way pipe (4) is connected to a collecting pipe (6), and a third valve (5) is provided between the three-way pipe (4) and the collecting pipe (6).

6. The system for increasing hydrogen production and aromatics yield by utilizing a first stage cold oil separation, transportation and reforming according to claim 5, characterized in that: The reforming device (10) is connected to an interface pipe (8).

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