Device for producing high-octane gasoline from topped oil through non-hydroisomerization

Abstract

The utility model belongs to the field of high-octane gasoline production, and particularly relates to a device for producing high-octane gasoline from topped oil through non-hydroisomerization. The raw material conveying pump is connected with the C4 feeding device through a valve and is used for conveying the raw materials; the raw material / reaction product heat exchanger is connected with the raw material conveying pump and is used for carrying out heat exchange on the raw materials; according to the utility model, the topped oil of the reforming device is used as a raw material, a second-section feeding process and a third-section feeding process are added in the reactor, and a circulating gas process from the outlet of the compressor to the reaction system is added, so that the raw material / reaction product is obtained. Under the non-hydrogen condition, the reaction depths of alkane cracking, selective hydrogenation, isomerization and the like of the low-octane-number topped oil are improved on the basis of the catalyst, the low-octane-number topped oil is converted into the high-octane-number gasoline blending component, the octane number of the produced gasoline can reach 89-90, the saturated vapor pressure is 65-80 kPa, the improvement cost is low, and the production operation is simple.

Description

Technical Field

[0001] The utility model relates to the technical field of high-octane gasoline production, in particular to a device for producing high-octane gasoline by non-hydrogen isomerization of topped oil. Background Art

[0002] Existing equipment for producing high-octane gasoline from topped oil without hydroisomerization primarily uses C4 as the raw material and consists of a feed pipeline, heat exchanger, cooler, heating furnace, reactor, separator, compressor, stabilizer, stabilizer reflux tank, tower bottom reboiler, transfer pump, and valves. C4 is delivered from the MTBE plant to this unit, where it enters the second and third stages of the reactor under pressure from a feed pump. Another portion, heated through heat exchange, enters the heating furnace. The furnace outlet is controlled at 350°C and enters the first stage of the reactor. Within the reactor, it undergoes alkane cracking, dehydrogenation, and oligomerization. The reaction products are cooled to 40°C and enter a gas-liquid separator. The liquid component is pressurized by a pump and enters the stabilizer, while the gas component is pressurized by a compressor and enters the stabilizer. The stabilizer separates liquefied gas and gasoline through distillation, producing civilian liquefied gas and a small amount of gasoline components.

[0003] In the prior art, when C4 is used as a raw material to enter the reactor, the reaction is violent and easily causes temperature runaway, which is not conducive to safe operation. The octane number of the tops oil in the reforming unit is generally around 65-70, and the saturated vapor pressure is 130-150 kPa. Due to the low octane number and high saturated vapor pressure of the tops oil, only a small amount can be used in gasoline pool blending. If it is sold separately, the economic benefits are not obvious due to its low price. Therefore, we propose a device for producing high-octane gasoline by non-hydrogen isomerization of tops oil to solve the above problems. Utility Model Content

[0004] The purpose of the utility model is to solve the shortcomings of the prior art and to propose a device for producing high-octane gasoline by isomerizing topped oil without hydrogen.

[0005] In order to achieve the above purpose, the present invention adopts the following technical solutions:

[0006] A device for producing high-octane gasoline by non-hydrogen isomerization of topped oil, comprising:

[0007] C4 inlet valve;

[0008] The raw material delivery pump is connected to the valve of the C4 inlet device and is used to deliver the raw materials;

[0009] A raw material / reaction product heat exchanger, connected to the raw material delivery pump, is used to exchange heat for the raw materials;

[0010] a raw material heating furnace connected to the raw material / reaction product heat exchanger;

[0011] A reactor connected to the raw material heating furnace;

[0012] a reaction product cooler connected to the raw material / reaction product heat exchanger;

[0013] A gas-liquid separation tank connected to a reaction product cooler;

[0014] Inlet device valve, connected to the raw material delivery pump;

[0015] A control valve connected to the raw material delivery pump;

[0016] The second-stage feed valve and the third-stage feed valve are both connected to the reactor.

[0017] Preferably, the gas-liquid separation tank is connected to a withdrawal valve, and the withdrawal valve is connected to a stabilization tower feed pump.

[0018] Preferably, the stabilizing tower feed pump is connected to the stabilizing tower, and the stabilizing tower and the gas-liquid separation tank are connected to the same rich gas compressor.

[0019] Preferably, the stabilization tower is connected to a reboiler inlet valve, a stabilization tower bottom extraction valve, a liquefied gas cooler and a liquefied gas reflux valve.

[0020] Preferably, the liquefied gas cooler is connected to a stabilizing tower top reflux tank, and the stabilizing tower top reflux tank is connected to a liquefied gas delivery pump.

[0021] Preferably, the liquefied gas delivery pump and the liquefied gas reflux valve are connected to the same liquefied gas delivery valve.

[0022] Preferably, the stabilization tower bottom extraction valve is connected to a gasoline delivery pump, and the gasoline delivery pump is connected to a gasoline delivery valve.

[0023] In the utility model, the device for producing high-octane gasoline by non-hydrogen isomerization of topped oil has the following beneficial effects:

[0024] The utility model uses the tops oil of a reforming unit as a raw material, adds two-stage and three-stage feeding processes in a reactor, and adds a circulating gas process from a compressor outlet to a reaction system. Under non-hydrogen conditions, the tops oil with a low octane number is subjected to a catalyst to increase the depth of reactions such as alkane cracking, selective hydrogenation, and isomerization, so as to convert the tops oil into a high-octane gasoline blending component. The octane number of the produced gasoline can reach 89-90 and the saturated vapor pressure can reach 65-80 kPa. The transformation cost is low and the production operation is simple. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 This is a schematic structural diagram of a device for producing high-octane gasoline by non-hydrogen isomerization of topped oil proposed in the present invention;

[0026] Figure 2Schematic diagram of the prior art.

[0027] In the figure: 1. C4 inlet valve; 2. Raw material delivery pump; 3. Raw material / reaction product heat exchanger; 4. Raw material heating furnace; 5. Reactor; 6. Reaction product cooler; 7. Gas-liquid separation tank; 8. Extraction valve; 9. Stabilization tower feed pump; 10. Rich gas compressor; 11. Stabilization tower; 12. Reboiler inlet valve; 13. Stabilization tower bottom extraction valve; 14. Gasoline delivery pump; 15. Gasoline export valve; 16. Liquefied gas cooler; 17. Stabilization tower top reflux tank; 18. Liquefied gas delivery pump; 19. Liquefied gas reflux valve; 20. Liquefied gas export valve; 21. Inlet valve; 22. Control valve; 23. Second-stage feed valve; 24. Third-stage feed valve. DETAILED DESCRIPTION

[0028] 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. Example 1

[0029] Reference Figure 1 A device for producing high-octane gasoline by non-hydrogen isomerization of topped oil, comprising:

[0030] C4 inlet device valve 1;

[0031] The raw material delivery pump 2 is connected to the valve 1 of the C4 inlet device and is used to deliver the raw materials;

[0032] The raw material / reaction product heat exchanger 3 is connected to the raw material delivery pump 2 and is used to exchange heat with the raw material;

[0033] a raw material heating furnace 4 connected to the raw material / reaction product heat exchanger 3;

[0034] Reactor 5, connected to raw material heating furnace 4;

[0035] a reaction product cooler 6 connected to the raw material / reaction product heat exchanger 3;

[0036] A gas-liquid separation tank 7 is connected to a reaction product cooler 6;

[0037] The inlet valve 21 is connected to the raw material delivery pump 2;

[0038] The control valve 22 is connected to the raw material delivery pump 2;

[0039] The second-stage feed valve 23 and the third-stage feed valve 24 are both connected to the reactor 5 .

[0040] In the present invention, the gas-liquid separation tank 7 is connected to a withdrawal valve 8 , and the withdrawal valve 8 is connected to a stabilizing tower feed pump 9 .

[0041] In the present invention, the stabilizing tower feed pump 9 is connected to the stabilizing tower 11 , and the stabilizing tower 11 and the gas-liquid separation tank 7 are connected to the same rich gas compressor 10 .

[0042] In the present invention, the stabilization tower 11 is connected to a reboiler inlet valve 12 , a stabilization tower bottom extraction valve 13 , a liquefied gas cooler 16 and a liquefied gas reflux valve 19 .

[0043] In the present invention, the liquefied gas cooler 16 is connected to a stabilizing tower top reflux tank 17 , and the stabilizing tower top reflux tank 17 is connected to a liquefied gas delivery pump 18 .

[0044] In the present invention, the liquefied gas delivery pump 18 and the liquefied gas reflux valve 19 are connected to the same liquefied gas delivery valve 20 .

[0045] In the present invention, the stabilizing tower bottom extraction valve 13 is connected to a gasoline delivery pump 14, and the gasoline delivery pump 14 is connected to a gasoline delivery valve.

[0046] In the present invention, the C4 feed valve 1 is closed and the C4 raw material is stopped, and a topped oil feeding process is added. The topped oil enters the raw material delivery pump 2 for pressurization through the feed valve 21. Before the raw material enters the raw material / reaction product heat exchanger 3, a circulating gas process of the compressor outlet return is added. The returned circulating gas is mixed with the topped oil through the control valve 22 and then enters the raw material / reaction product heat exchanger 3. The raw material after heat exchange is divided into two parts, one part enters the raw material heating furnace 4, is heated to 350°C by the heating furnace, and enters the reactor 5 from the top of the reactor. The other part is newly added with a process, which enters the second-stage feed valve 23 and the third-stage feed valve 24 of the reactor, so that the raw material is respectively subjected to the second-stage reactor and the third-stage reactor, which is beneficial to reactions such as alkane cracking, selective hydrogenation, isomerization, and polymerization. The reaction product is cooled to about 40°C through the raw material / reaction product heat exchanger 3 and the reaction product cooler 6, and enters the gas-liquid separation tank 7 for gas-liquid separation. The gaseous phase component at the top of the tank is pressurized by the rich gas compressor 10, and the H2-rich component The gas phase components enter the reaction system through the newly added circulating gas process through the circulating gas valve 22, and the remaining gas phase components enter the stabilization tower 11. The separated liquid phase components enter the stabilization tower feed pump 9 through the gas-liquid separation tank bottom extraction valve 8 and then enter the stabilization tower 11 after being pressurized. The bottom temperature of the stabilization tower is controlled at 150°C by the reboiler inlet valve 12. The gasoline component and the liquefied gas are separated under the action of distillation. The gasoline component enters the gasoline delivery pump 14 through the stabilization tower bottom extraction valve 13 and is sent to the gasoline outlet valve 15. In the oil tank area, the liquefied gas from the stabilization tower enters the liquefied gas cooler 16 and then the reflux tank 17 at the top of the stabilization tower. Part of the liquefied gas in the reflux tank passes through the liquefied gas delivery pump 18 and the liquefied gas reflux valve 19 into the top of the stabilization tower 11 for reflux, and part of it passes through the liquefied gas delivery valve 20 and is delivered to the liquefied gas tank area. After the transformation, the octane number of the produced gasoline component reaches 89-90, and the saturated vapor pressure drops to 65-80kPa, realizing gasoline blending components, and increasing efficiency by about 30 million yuan throughout the year. Example 2

[0047] The difference from Example 1 is that: 1. The C4 feed line is deactivated and a new top oil feed line is added to prevent the reactor from overheating.

[0048] The reactor feeding process was changed from one-stage feeding to three-stage simultaneous feeding to better utilize the reaction activity of each bed section of the reactor;

[0049] A return line is added at the compressor outlet as circulating gas back into the reactor. The gas phase components are rich in H2 and can undergo selective hydrogenation reaction and isomerization reaction under the action of catalyst.

[0050] 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 device for producing high-octane gasoline from topped oil without hydroisomerization, characterized in that: include: C4 inlet valve (1); A raw material delivery pump (2) is connected to the C4 inlet device valve (1) and is used to deliver the raw material; A raw material / reaction product heat exchanger (3) is connected to the raw material delivery pump (2) and is used to exchange heat with the raw material; A raw material heating furnace (4) connected to the raw material / reaction product heat exchanger (3); The reactor (5) is connected to the raw material heating furnace (4); a reaction product cooler (6), connected to the raw material / reaction product heat exchanger (3); A gas-liquid separation tank (7) is connected to a reaction product cooler (6); The inlet valve (21) is connected to the raw material delivery pump (2); A control valve (22) connected to the raw material delivery pump (2); The second-stage feed valve (23) and the third-stage feed valve (24) are both connected to the reactor (5).

2. The device for producing high-octane gasoline from a kind of tops oil non-hydroisomerization according to claim 1, wherein The gas-liquid separation tank (7) is connected to a withdrawal valve (8), and the withdrawal valve (8) is connected to a stabilization tower feed pump (9).

3. The device for producing high-octane gasoline by non-hydroisomerization of topping oil according to claim 2, wherein The stabilizing tower feed pump (9) is connected to the stabilizing tower (11), and the stabilizing tower (11) and the gas-liquid separation tank (7) are connected to the same rich gas compressor (10).

4. The device for producing high-octane gasoline from a kind of tops oil non-hydroisomerization according to claim 3, characterized in that, The stabilization tower (11) is connected to a reboiler inlet valve (12), a stabilization tower bottom extraction valve (13), a liquefied gas cooler (16) and a liquefied gas reflux valve (19).

5. The device for producing high-octane gasoline from a kind of tops oil non-hydroisomerization according to claim 4, characterized in that, The liquefied gas cooler (16) is connected to a stabilizing tower top reflux tank (17), and the stabilizing tower top reflux tank (17) is connected to a liquefied gas delivery pump (18).

6. A device for producing high-octane gasoline from tops oil without hydroisomerization according to claim 5, characterized in that: The liquefied gas delivery pump (18) and the liquefied gas reflux valve (19) are connected to the same liquefied gas delivery valve (20).

7. The device for producing high-octane gasoline from a kind of tops oil non-hydroisomerization according to claim 6, characterized in that, The stabilizing tower bottom extraction valve (13) is connected to a gasoline delivery pump (14), and the gasoline delivery pump (14) is connected to a gasoline delivery valve.

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