Novel naphthenic base distillate oil hydrogenation device and method

Abstract

The invention discloses a novel naphthenic base distillate oil hydrogenation device and method. The device comprises a reaction feeding furnace, a hydrotreating reactor, a hydrodewaxing reactor, an interstage stripping tower and a finishing reactor, the reaction feeding furnace is sequentially connected with the hydrotreating reactor, the hydrodewaxing reactor, the interstage stripping tower and the finishing reactor. According to the invention, the yellowing resistance requirement of a naphthenic base oil product can be greatly improved, excessive cracking of the raw materials can be avoided, the product can maintain a high CN value and high viscosity, carbon type maintenance is met, indexes such as stability of the existing alkyl base oil product can meet the industrial quality requirement, and the product has a wide application prospect. And power is increased for sustainable development of enterprises.

Description

Technical Field

[0001] The present invention relates to the technical field of naphthenic oil processing, and more particularly to a novel naphthenic distillate oil hydrogenation device and method. Background Art

[0002] Naphthenic crude oil has the characteristics of low wax content, high acid value, high density, high viscosity, colloid, residual carbon content and high metal content. Its cracking performance is very poor and it cannot be used as a catalytic raw material. However, it is a high-quality raw material for producing asphalt, and can be used to prepare oil products with low pour point requirements and low viscosity-temperature requirements, such as electrical oil and refrigeration oil. Therefore, the process setting of naphthenic crude oil is arranged according to the fuel-asphalt-lubricant type route. The common processing process is: hydrotreatment, atmospheric distillation, vacuum distillation, clay refining, and then blending to produce lubricant products.

[0003] At present, cycloalkane distillate oil hydrogenation units all adopt the technical route of hydrotreating, hydrodewaxing, supplementary refining and high-pressure full hydrogenation. Some of them have a two-stage reaction stage and use interstage stripping towers, hot high-fractionation and pre-furnace hydrogen mixing processes. The side-line products produced are mainly industrial white oil related series products.

[0004] With the increasing demand for high-quality products and increasingly stringent national and industry quality requirements, producing high-quality cycloalkane base oil products with good lightness and thermal stability is of great significance for enterprises to improve their market competitiveness and create more economic benefits.

[0005] In view of this, the present invention provides a novel cycloalkane distillate oil hydrogenation device and method, which improves the yellowing resistance requirements of cycloalkane base oil products without changing the existing catalysts and equipment facilities, and can keep the product at a high CN value and high viscosity, meet the carbon type maintenance, and increase the driving force for the sustainable development of the enterprise. Summary of the invention

[0006] In view of this, the present invention provides a novel cycloalkane fraction oil hydrogenation device and method, which can prevent excessive cracking of raw materials while ensuring the yellowing resistance requirements of existing base oil products, so that the products maintain a high CN value and a high viscosity to meet the carbon type maintenance requirements.

[0007] In order to achieve the above object, the present invention adopts the following technical solution:

[0008] A novel naphthenic distillate oil hydrogenation unit comprises: a reaction feed furnace, a hydrotreating reactor, a hydrodewaxing reactor, an interstage stripping tower, and a supplementary refining reactor;

[0009] The reaction feed furnace is connected with the hydroprocessing reactor, the hydrodewaxing reactor, the interstage stripping tower and the supplementary refining reactor in sequence.

[0010] Preferably, the above device further comprises: a cold high-fraction oil tank, a cold low-fraction oil tank, a hot high-fraction oil tank, a hot low-fraction oil tank and a circulating hydrogen desulfurization device;

[0011] The bottom of the interstage stripping tower is connected to the hot high-fraction oil tank and the hot low-fraction oil tank in sequence;

[0012] The top of the interstage stripping tower is connected to the cold high-fraction oil tank and the hot low-fraction oil tank in sequence;

[0013] The bottom of the supplementary refining reactor is connected to the hot high-fraction oil tank;

[0014] The cold high-fraction oil tank is also connected to the circulating hydrogen desulfurization device and the hot low-fraction oil tank respectively;

[0015] The circulating hydrogen desulfurization device is also connected to the hydroprocessing reactor.

[0016] Preferably, the above device further comprises: a new hydrogen production device;

[0017] The new hydrogen production device is connected to the hydroprocessing reactor and the supplementary refining reactor respectively;

[0018] The circulating hydrogen desulfurization device is also connected to the pipeline between the new hydrogen production device and the supplementary refining reactor.

[0019] Preferably, the hydrotreating reactor and the hydrodewaxing reactor are both provided with three catalyst beds, and rapid cooling hydrogen injection facilities are provided between the beds.

[0020] Preferably, the interstage stripping tower is provided with a section of filler; the supplementary refining reactor is provided with two catalyst beds, and a quenching hydrogen injection facility is provided between the beds.

[0021] Another object of the present invention is to provide a novel cycloalkane distillate oil hydrogenation method, using the novel cycloalkane distillate oil hydrogenation device, comprising the following steps:

[0022] (1) After heat exchange, the crude oil is sent to a reaction feed furnace to be heated to the required temperature, and then sent to a hydroprocessing reactor to undergo hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions under high pressure, high temperature and catalyst to obtain product cold hydrogen;

[0023] (2) cold hydrogen is fed into a hydrodewaxing reactor, and hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions are carried out under high pressure, high temperature and catalyst action, and then a dewaxing catalyst is used to selectively remove high-condensation point macromolecular normal alkanes to obtain a dewaxing reaction product;

[0024] (3) The dewaxing reaction product is sent to the top of the interstage stripping tower after heat exchange, and the oil and gas at the top of the interstage stripping tower is sent to the cold high-precision tank after heat exchange and cooling;

[0025] (4) The bottom oil of the interstage stripping tower is sent to the supplementary refining reactor after being pressurized, where olefin and aromatic saturation reactions occur under high pressure, high temperature and catalyst;

[0026] (5) The reaction product of the supplementary refining reactor is sent to a hot high fraction tank for gas-liquid separation, the generated hot high fraction gas is returned to the bottom of the interstage stripping tower, the oil phase at the bottom of the hot high fraction tank is depressurized and sent to a hot low fraction tank for gas-liquid separation, and the hot low fraction gas is condensed and enters a cold low fraction oil tank together with the hot high fraction oil;

[0027] (6) The gas at the top of the cold high separation tank is desulfurized by a circulating hydrogen desulfurization device to generate circulating hydrogen. One path of the circulating hydrogen is mixed with new hydrogen generated by a new hydrogen production device and heated feedstock oil to enter a hydroprocessing reactor, and the other path is mixed with new hydrogen generated by a new hydrogen production device and the bottom oil of an interstage stripping tower to enter a supplementary refining reactor;

[0028] (7) The cold low fraction oil in the cold low fraction tank and the hot low fraction oil in the hot low fraction tank enter the atmospheric pressure tower and the vacuum tower in turn for fractionation. In the vacuum tower, first-line oil, second-line oil, third-line oil, fourth-line oil and vacuum tower bottom oil are extracted from top to bottom in turn.

[0029] Preferably, the high pressure in step (1) is 15.97-16.05 MPa, and the high temperature is 348-392°C.

[0030] Preferably, the high pressure in step (2) is 15.85-15.97 MPa, and the high temperature is 360-392°C.

[0031] Preferably, the high pressure in step (4) is 15.74-15.97 MPa, and the high temperature is 250°C.

[0032] Preferably, the absolute pressure in the vacuum tower is 4±1 KPa; superheated stripping steam is provided at the bottom of the vacuum tower, the steam blowing volume is 170±10 kg / h, and the temperatures at the top and bottom of the vacuum tower are 60±5°C and 240±5°C respectively.

[0033] It can be seen from the above technical solution that compared with the prior art, the present invention has the following beneficial effects:

[0034] The present invention can significantly improve the yellowing resistance requirements of cycloalkane base oil products, and can avoid excessive cracking of raw materials, so that the product maintains a high CN value and a high viscosity, meets the carbon type maintenance, and enables the stability and other indicators of existing alkyl base oil products to meet the industry quality requirements, thereby increasing the impetus for the sustainable development of enterprises. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying creative work.

[0036] Figure 1 It is a schematic diagram of the structure of the device of the present invention;

[0037] in, Figure 1 In the figure: 1-reaction feed furnace; 2-hydrogenation treatment reactor; 3-hydrogenation dewaxing reactor; 4-interstage stripping tower; 5-supplementary refining reactor; 6-new hydrogen production device; 7-cold high separation tank; 8-hot high separation tank; 9-cold low separation tank; 10-hot low separation tank; 11-circulating hydrogen desulfurization device. DETAILED DESCRIPTION

[0038] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0039] Example 1

[0040] This embodiment provides a novel naphthenic distillate oil hydrogenation device, comprising: a reaction feed furnace 1, a hydrotreating reactor 2, a hydrodewaxing reactor 3, an interstage stripping tower 4, a supplementary refining reactor 5, a cold high-fraction oil tank 7, a cold low-fraction oil tank 9, a hot high-fraction oil tank 8, a hot low-fraction oil tank 10, a circulating hydrogen desulfurization device 11 and a new hydrogen production device 6;

[0041] The reaction feed furnace 1 is connected to the hydrotreating reactor 2, the hydrodewaxing reactor 3, the interstage stripping tower 4, and the supplementary refining reactor 5 in sequence.

[0042] The bottom of the interstage stripping tower 4 is connected to the hot high-fraction oil tank 8 and the hot low-fraction oil tank 10 in sequence;

[0043] The top of the interstage stripping tower 4 is connected to the cold high-fraction oil tank 7 and the hot low-fraction oil tank 9 in sequence;

[0044] The bottom of the supplementary refining reactor 5 is connected to the hot high-fraction oil tank 8;

[0045] The cold high fraction oil tank 7 is also connected to the circulating hydrogen desulfurization device 11 and the hot low fraction oil tank 9 respectively;

[0046] The circulating hydrogen desulfurization device 11 is also connected to the hydroprocessing reactor 2 .

[0047] The new hydrogen production device 6 is connected to the hydroprocessing reactor 2 and the supplementary refining reactor 5 respectively;

[0048] The circulating hydrogen desulfurization device 11 is also connected to the pipeline between the new hydrogen production device 6 and the supplementary refining reactor 5 .

[0049] The hydrotreating reactor 2 and the hydrodewaxing reactor 3 are both provided with three catalyst beds, and rapid cooling hydrogen injection facilities are provided between the beds.

[0050] The interstage stripping tower 4 is provided with a section of filler; the supplementary refining reactor 5 is provided with two catalyst beds, and a quenching hydrogen injection facility is provided between the beds.

[0051] Example 2

[0052] This embodiment provides a novel cycloalkane distillate oil hydrogenation method, comprising:

[0053] (1) After heat exchange, the crude oil is sent to a reaction feed furnace to be heated to the required temperature, and then sent to a hydroprocessing reactor to undergo hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions under the action of a catalyst at 15.97-16.05 MPa and 348-392°C to obtain product cold hydrogen;

[0054] (2) cold hydrogen is fed into a hydrodewaxing reactor, and hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions are carried out at 15.85-15.97 MPa and 360-392° C. under the action of a catalyst, and then a dewaxing catalyst is used to selectively remove high-condensation-point macromolecular normal alkanes to obtain a dewaxing reaction product;

[0055] (3) The dewaxing reaction product is sent to the top of the interstage stripping tower after heat exchange, and the oil and gas at the top of the interstage stripping tower is sent to the cold high-precision tank after heat exchange and cooling;

[0056] (4) The bottom oil of the interstage stripping tower is sent to the supplementary refining reactor after being pressurized, where olefin and aromatic saturation reactions occur at 15.74-15.97 MPa, 250°C and a catalyst;

[0057] (5) The reaction product of the supplementary refining reactor is sent to a hot high fraction tank for gas-liquid separation, the generated hot high fraction gas is returned to the bottom of the interstage stripping tower, the oil phase at the bottom of the hot high fraction tank is depressurized and sent to a hot low fraction tank for gas-liquid separation, and the hot low fraction gas is condensed and enters a cold low fraction oil tank together with the hot high fraction oil;

[0058] (6) The gas at the top of the cold high separation tank is desulfurized by a circulating hydrogen desulfurization device to generate circulating hydrogen. One path of the circulating hydrogen is mixed with new hydrogen generated by a new hydrogen production device and heated feedstock oil to enter a hydroprocessing reactor, and the other path is mixed with new hydrogen generated by a new hydrogen production device and the bottom oil of an interstage stripping tower to enter a supplementary refining reactor;

[0059] (7) The cold low fraction oil in the cold low fraction tank and the hot low fraction oil in the hot low fraction tank enter the atmospheric pressure tower and the vacuum tower in turn for fractionation. In the vacuum tower, first-line oil, second-line oil, third-line oil, fourth-line oil and vacuum tower bottom oil are extracted from top to bottom in turn.

[0060] Among them, in this embodiment, the present invention mainly lies in the improvement of the hydrogenation process. The atmospheric pressure tower and the vacuum tower in the distillation process are both conventional technical means in the field, and therefore are not shown in the drawings of the specification. The absolute pressure in the vacuum tower is 4±1Kpa; superheated stripping steam is provided at the bottom of the vacuum tower, and the steam blowing volume is 170±10kg / h. The temperatures at the top and bottom of the vacuum tower are 60±5℃ and 240±5℃, respectively.

[0061] In this specification, each embodiment is described in a progressive manner, and each embodiment focuses on the differences from other embodiments. The same or similar parts between the embodiments can be referred to each other. For the device disclosed in the embodiment, since it corresponds to the method disclosed in the embodiment, the description is relatively simple, and the relevant parts can be referred to the method part.

[0062] The above description of the disclosed embodiments enables one skilled in the art to implement or use the present invention. Various modifications to these embodiments will be apparent to one skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to the embodiments shown herein, but rather to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A novel cycloalkane distillate oil hydrogenation unit, characterized in that: include: Reaction feed furnace, hydrotreating reactor, hydrodewaxing reactor, interstage stripping tower, supplementary refining reactor; The reaction feed furnace is connected with the hydroprocessing reactor, the hydrodewaxing reactor, the interstage stripping tower and the supplementary refining reactor in sequence.

2. A novel cycloalkane distillate oil hydrogenation device according to claim 1, characterized in that: Also includes: Cold high-fraction oil tank, cold low-fraction oil tank, hot high-fraction oil tank, hot low-fraction oil tank and circulating hydrogen desulfurization device; The bottom of the interstage stripping tower is connected to the hot high-fraction oil tank and the hot low-fraction oil tank in sequence; The top of the interstage stripping tower is connected to the cold high-fraction oil tank and the hot low-fraction oil tank in sequence; The bottom of the supplementary refining reactor is connected to the hot high-fraction oil tank; The cold high-fraction oil tank is also connected to the circulating hydrogen desulfurization device and the hot low-fraction oil tank respectively; The circulating hydrogen desulfurization device is also connected to the hydroprocessing reactor.

3. A novel cycloalkane distillate oil hydrogenation device according to claim 2, characterized in that: Also includes: New hydrogen production equipment; The new hydrogen production device is connected to the hydroprocessing reactor and the supplementary refining reactor respectively; The circulating hydrogen desulfurization device is also connected to the pipeline between the new hydrogen production device and the supplementary refining reactor.

4. A novel cycloalkane distillate oil hydrogenation device according to claim 3, characterized in that: The hydrotreating reactor and the hydrodewaxing reactor are both provided with three catalyst beds, and rapid cooling hydrogen injection facilities are provided between the beds.

5. A novel cycloalkane distillate oil hydrogenation device according to claim 4, characterized in that: The interstage stripping tower is provided with a section of filler; the supplementary refining reactor is provided with two catalyst beds, and a rapid cooling hydrogen injection facility is provided between the beds.

6. A novel method for hydrogenating cycloalkane distillate oil, characterized in that: The novel cycloalkane distillate oil hydrogenation device according to claim 3 comprises the following steps: (1) After heat exchange, the crude oil is sent to a reaction feed furnace to be heated to the required temperature, and then sent to a hydroprocessing reactor to undergo hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions under high pressure, high temperature and catalyst to obtain product cold hydrogen; (2) cold hydrogen is fed into a hydrodewaxing reactor, and hydrodesulfurization, denitrogenation, deoxygenation and aromatic saturation reactions are carried out under high pressure, high temperature and catalyst action, and then a dewaxing catalyst is used to selectively remove high-condensation point macromolecular normal alkanes to obtain a dewaxing reaction product; (3) The dewaxing reaction product is sent to the top of the interstage stripping tower after heat exchange, and the oil and gas at the top of the interstage stripping tower is sent to the cold high-precision tank after heat exchange and cooling; (4) The bottom oil of the interstage stripping tower is sent to the supplementary refining reactor after being pressurized, where olefin and aromatic saturation reactions occur under high pressure, high temperature and catalyst; (5) The reaction product of the supplementary refining reactor is sent to a hot high fraction tank for gas-liquid separation, the generated hot high fraction gas is returned to the bottom of the interstage stripping tower, the oil phase at the bottom of the hot high fraction tank is depressurized and sent to a hot low fraction tank for gas-liquid separation, and the hot low fraction gas is condensed and enters a cold low fraction oil tank together with the hot high fraction oil; (6) The gas at the top of the cold high separation tank is desulfurized by a circulating hydrogen desulfurization device to generate circulating hydrogen. One path of the circulating hydrogen is mixed with new hydrogen generated by a new hydrogen production device and heated feedstock oil to enter a hydroprocessing reactor, and the other path is mixed with new hydrogen generated by a new hydrogen production device and the bottom oil of an interstage stripping tower to enter a supplementary refining reactor; (7) The cold low fraction oil in the cold low fraction tank and the hot low fraction oil in the hot low fraction tank enter the atmospheric pressure tower and the vacuum tower in turn for fractionation. In the vacuum tower, first-line oil, second-line oil, third-line oil, fourth-line oil and vacuum tower bottom oil are extracted from top to bottom in turn.

7. A novel cycloalkane distillate oil hydrogenation method according to claim 6, characterized in that: The high pressure in step (1) is 15.97-16.05 MPa, and the high temperature is 348-392°C.

8. A novel cycloalkane distillate oil hydrogenation method according to claim 6, characterized in that: The high pressure in step (2) is 15.85-15.97 MPa, and the high temperature is 360-392°C.

9. A novel cycloalkane distillate oil hydrogenation method according to claim 6, characterized in that: The high pressure in step (4) is 15.74-15.97 MPa, and the high temperature is 250°C.

10. A novel cycloalkane distillate oil hydrogenation method according to claim 6, characterized in that: The absolute pressure in the vacuum tower is 4±1Kpa; superheated stripping steam is provided at the bottom of the vacuum tower, the steam blowing volume is 170±10kg / h, and the temperatures at the top and bottom of the vacuum tower are 60±5℃ and 240±5℃ respectively.

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