CN215427377U

CN215427377U - Pressure-reducing rectifying tower with satellite type tower kettle

Info

Publication number: CN215427377U
Application number: CN202120602169.XU
Authority: CN
Inventors: 张其凯; 徐鹏辉; 高群; 李清瑞; 王晨燕
Original assignee: Jiechuang Dongying Energy Technology Co ltd
Current assignee: Jiechuang Dongying Energy Technology Co ltd
Priority date: 2021-03-24
Filing date: 2021-03-24
Publication date: 2022-01-07
Anticipated expiration: 2031-03-24

Abstract

The utility model provides a decompression rectifying tower with a satellite tower kettle. The decompression rectifying tower comprises a satellite surrounding type decompression tower kettle and a rectifying section; the satellite surrounding type pressure reducing tower kettle comprises a main tower kettle and a plurality of sub-reactors which are arranged outside the main tower kettle in a satellite surrounding manner; the main tower kettle is provided with a first outlet and a plurality of injection inlets, and the top of the main tower kettle is provided with an opening; the sub-reactors are provided with second outlets and first inlets, the injection inlets are connected with the second outlets of the sub-reactors in a one-to-one correspondence manner, and the first outlets are connected with the first inlets; wherein the injection direction of each injection inlet can be adjusted or the injection directions of at least two injection inlets are crossed, and the volume of the sub-reactor is smaller than that of the main tower kettle; the rectifying section is communicated with the top opening of the main tower kettle, and the top of the rectifying section is provided with a light component outlet. The atmospheric residue oil is treated by the vacuum distillation tower, and the light oil extraction rate can be effectively improved under relatively mild temperature and pressure environments.

Description

Pressure-reducing rectifying tower with satellite type tower kettle

Technical Field

The utility model relates to the technical field of petrochemical industry, in particular to a pressure reduction rectifying tower with a satellite type tower kettle.

Background

It is well known that the atmospheric and vacuum systems of refineries are the leading processes of oil refineries and even the refining industry. The process connection in an atmospheric and vacuum system of an oil refinery, which is often called 'three towers and two furnaces', is as follows: the process of the initial distillation tower → the atmospheric pressure furnace → the atmospheric pressure tower → the vacuum furnace → the vacuum tower can distill off 70-80% of the raw materials required by the refining industry, so the atmospheric and vacuum system is one of the most important processes of the refinery plant.

However, since the beginning of this century, as the degree of oil extraction increases, the components of the extracted crude oil become heavier and heavier, and the crude oil becomes heavier and poorer, and the heavy and inferior crude oil, such as shale oil, oil sand oil, heavy (heavy) oil, extra heavy oil, deep petroleum, and unconventional heavy and inferior oil, such as asphalt and coal tar, starts to be produced in large quantities, so that the working condition of the refinery is continuously reduced, and the efficiency of the distillation system of the refinery is greatly reduced. In the middle of the last century, 50-70% of straight-run gasoline and diesel oil can be distilled from crude oil by a refinery atmospheric tower, but in many refineries, only inferior crude oil can be obtained, and the atmospheric tower can only distill 10-30% or even lower proportion of straight-run fuel oil from the crude oil. The reduction of the straight-run fuel oil inevitably brings about the sharp increase of the atmospheric residue and the vacuum residue of the refinery, and the final result is that the pressure for processing heavy oil by the refinery is increased, and the benefit is reduced.

Currently, the reserves of heavy oil account for more than 50% of the world's crude oil recoverable reserves. Heavy oil causes severe problems of exploitation, transportation and processing in the petroleum industry from upstream to downstream, and oil refining enterprises are faced with triple pressure of raw material heaviness and deterioration, product lightening and environmental protection, and production process cleaning and low carbonization.

For the reasons mentioned above, the atmospheric and vacuum processes of refineries are also forced to make corresponding changes: for refineries that can obtain light crude oil (API > 34) and medium crude oil (API 34-20), 'three-tower two-furnace' is a typical atmospheric and vacuum normal process. However, if only heavy crude oil (API 10-20) or even extra heavy crude oil (API < 10) is available to the refinery, the atmospheric and vacuum systems of the refinery are degraded to 'one tower and one furnace', that is: vacuum furnace → vacuum tower, atmospheric tower cannot distill any product because the crude oil is completely free of light components.

In summary, the vacuum tower and the vacuum furnace for heating the raw material of the vacuum tower are essential key equipments for all refineries, regardless of whether high-quality crude oil can be obtained or not. If the light oil extraction rate of the vacuum tower can be increased and the tail oil output called vacuum residue can be reduced, the process can greatly improve the economic benefit of the refinery.

As for the introduction of foreign advanced technologies in China at present, two approaches are mainly used for improving the extraction rate of the vacuum tower, wherein one approach is to increase the feeding temperature of the vacuum tower, and the temperature is generally increased from 380-390 ℃ to 410-420 ℃. Yet another way to increase the draw-off rate of the vacuum column is to increase the vacuum level of the vacuum column, which is commonly referred to as deep draw. The vacuum degree of the reduced pressure deep drawing is generally 92-97 KPa, and the distillation true boiling point is about 600 ℃. Of course, by taking such measures, the extraction rate of the vacuum column can be increased by 5 to 8%. The economic benefit is significant for megaton feed throughput.

However, increasing the feed temperature to the edge of substantial coking (426 ℃) is a risk to the plant operation and therefore increases in the vacuum column feed temperature must be done with caution. In the process of pressure reduction and deep drawing, the requirement can be met only by at least three stages of steam injection, which needs to consume a large amount of energy.

For the above reasons, it is necessary to provide a vacuum tower with high light oil extraction rate, milder operating temperature and pressure conditions, and lower energy consumption.

SUMMERY OF THE UTILITY MODEL

The utility model mainly aims to provide a vacuum distillation tower with a satellite tower kettle, which aims to solve the problems of low light oil extraction rate, harsh operating conditions and huge energy consumption in the vacuum distillation of atmospheric residue in the vacuum tower in the prior art.

In order to achieve the above object, according to one aspect of the present invention, there is provided a vacuum rectification column having a satellite tower, comprising: the satellite surrounding type pressure reducing tower kettle comprises a main tower kettle and a plurality of sub-reactors which are arranged outside the main tower kettle in a satellite surrounding manner; the main tower kettle is provided with a first outlet and a plurality of injection inlets, and the top of the main tower kettle is provided with an opening; the sub-reactors are provided with second outlets and first inlets, the injection inlets are communicated with the second outlets of the sub-reactors in a one-to-one correspondence manner, and the first outlets are communicated with the first inlets; wherein the injection direction of each injection inlet can be adjusted or the injection directions of at least two injection inlets are crossed, and the volume of the sub-reactor is smaller than that of the main tower kettle; and the rectifying section is positioned above the main tower kettle and communicated with the top opening of the main tower kettle, and the top of the rectifying section is provided with a light component outlet.

Furthermore, a non-submerged impinging stream assembly is arranged in the main tower kettle and is arranged in the jetting direction of each jetting inlet and used for carrying out non-submerged impinging, cavitation and shearing on jetted materials of the jetting inlets.

Furthermore, each first outlet is connected with the first inlet through a circulating pipeline, and the circulating pipeline is also provided with a forced circulating pump.

Further, the volume of the sub-reactor is denoted as V1, and the volume of the main column bottom is denoted as V2, V1/V2 is 1/20 to 1/10000.

Furthermore, the volume of the sub-reactor is less than or equal to 0.025m³A pressurized micro-reactor with an inner diameter less than 0.1m or a volume less than or equal to 0.1m³And a normal pressure micro-reactor with an inner diameter less than 0.1 m.

Further, still include: the vacuum pump is connected with the light component outlet; and the waste gas tank is provided with a light component inlet which is connected with an outlet of the vacuum pump.

Further, the waste gas tank is also provided with a liquid phase component outlet and a waste gas outlet, and the waste gas outlet is connected with the first inlet of at least part of the sub-reactors.

Furthermore, the lateral part of the rectifying section is also provided with a lateral line extraction outlet, the lateral line extraction outlet comprises a gasoline fraction extraction outlet, a diesel fraction extraction outlet and a residual distillate extraction outlet which are arranged from top to bottom, and the reduced pressure rectifying tower with the satellite tower kettle further comprises: the gasoline storage tank is connected with the gasoline fraction extraction port; the diesel oil storage tank is connected with the diesel oil fraction extraction outlet; and the residual distillate oil storage tank is connected with the residual distillate oil extraction outlet.

Further, the outlet of the residual distillate storage tank is connected with the first inlet of at least part of the sub-reactors.

Further, the reactor also comprises a hydrogen supply unit which is connected with the first inlet of at least part of the sub-reactors.

Further, the bottom of the main tower still is provided with a vacuum residue discharge outlet.

Further, the injection direction of any one of the injection inlets intersects with the injection direction of at least one of the remaining injection inlets.

Further, the non-submerged impinging stream assembly comprises: the casing, the inner chamber of casing is used for providing non-submerged formula striking place, and the casing includes a plurality of injection channels that set up with each injection inlet one-to-one, is provided with a plurality of first pore structures on injection channel's the outer wall, and the axial of first pore structure and injection channel's axial direction have the contained angle.

Furthermore, one end of the injection channel, which is far away from the injection inlet, is provided with an impact bottom plate; or the radial sectional area of the injection channel is gradually reduced along the direction far away from the injection inlet, and the other end of the injection channel is closed.

Further, a non-submerged impinging stream assembly is disposed at the top of the main column vessel near the rectifying section.

Furthermore, the sub-reactors are of tubular structures, a plurality of pipeline cavitation plates are further arranged inside the sub-reactors, and a plurality of second hole structures are arranged on the pipeline cavitation plates.

Furthermore, the main tower kettle comprises a tower kettle body, a stripping section and a feeding section from bottom to top in sequence, the injection inlet is arranged at the feeding section, the first outlet is arranged at the tower kettle body, and the feeding section is also provided with an atmospheric residue inlet.

The utility model provides a vacuum rectification tower with a satellite type tower kettle, which specifically comprises a satellite surrounding type vacuum tower kettle and a rectification section. The satellite surrounding type pressure reduction tower kettle comprises a main tower kettle and a plurality of sub-reactors which are small in volume and are arranged outside the main tower kettle in a satellite surrounding manner. In the process of carrying out vacuum rectification on the atmospheric residue, the atmospheric residue raw material can enter through the sub-reactors, the residue entering the vacuum tower kettle is circulated for many times through the plurality of sub-reactors, or fresh atmospheric residue and oil returned from the first outlet of the main tower kettle are mixed in the sub-reactors and then are sent to the main tower kettle, so that a circulation state is formed. On one hand, the continuous circulation of the fresh atmospheric residue and the oil in the kettle can enable the materials to meet the process requirements on mass transfer, heat transfer and energy transfer in the most rapid and simple mode, and the reactor is an efficient reactor. On the other hand, after the fresh atmospheric residue and the oil material in the kettle enter the injection inlets through the sub-reactors, at least two materials collide after being injected in the actual injection process because the injection direction of each injection inlet can be adjusted or the injection directions of at least two injection inlets are crossed. And the collision is carried out in a gas phase environment due to the fact that a liquid phase is in a non-submerged collision process, so that a certain hydrogen transfer reaction can be carried out, the light weight reaction of the atmospheric residue oil and the circulating oil can be promoted, and the high-pressure oil-gas separation device has a good effect on improving the quality and the extraction rate of the hydrogen component of the vacuum distillation tower. The atmospheric residue and the tower bottom oil entering the vacuum tower bottom are continuously circulated, collided and flashed through the sub-reactors to generate gas-phase light oil, and the gas-phase light oil enters the upper rectifying section for vacuum rectification to separate gasoline fraction, diesel fraction and residual fraction, and the top of the rectifying tower is used for extracting a light-component gas phase.

The atmospheric residue oil is treated by the vacuum distillation tower with the satellite tower kettle, the light oil extraction rate can be effectively improved under relatively mild temperature and pressure environments, and the method is a breakthrough change for energy consumption-benefit data.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the utility model and, together with the description, serve to explain the utility model and not to limit the utility model. In the drawings:

FIG. 1 shows a schematic diagram of a vacuum distillation column with satellite bottoms according to an embodiment of the utility model; and

FIG. 2 shows a schematic diagram of a satellite-encircled vacuum column bottom in a vacuum rectification column with a satellite-based bottom according to an embodiment of the utility model;

FIG. 3 shows a schematic diagram of a satellite-surrounded vacuum distillation column vessel in a vacuum distillation column with a satellite vessel according to another embodiment of the present invention;

fig. 4 shows a schematic structural view of a vacuum distillation column with satellite bottoms according to another embodiment of the present invention.

Wherein the figures include the following reference numerals:

10. a satellite surrounding type pressure reducing tower kettle; 11. a main tower kettle; 12. a sub-reactor; 13. a non-submerged impinging stream assembly; 14. a forced circulation pump; 111. a tower kettle body; 112. a stripping section; 113. a feeding section; 20. a rectifying section; 30. a vacuum pump; 40. an exhaust gas tank; 50. a gasoline storage tank; 60. a diesel storage tank; 70. a residual distillate oil storage tank; 80. a balancing tank; 90. a first delivery pump; 100. a second delivery pump; 110. a liquefied gas tank.

Detailed Description

It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.

The problems of low light oil extraction rate, harsh operation conditions and huge energy consumption existing in the prior art when atmospheric residue is subjected to vacuum distillation in a vacuum tower. In addition, in a common vacuum tower of a refinery, the diameter of a vacuum tower kettle is about 5-8 meters, the volume of the vacuum tower kettle is 25-250 cubic meters, and the traditional vacuum tower kettle only has a function of receiving vacuum residue. In order to increase the light oil extraction rate of the vacuum column, the vacuum column still needs to take the function of the reactor. However, when the ultra-large-volume pressure reduction tower kettle is used as a reactor, the heat transfer, the mass transfer and the momentum transfer of materials in the kettle have serious imbalance phenomena.

In order to solve the above problems, the present invention provides a vacuum distillation column having a satellite type column bottom, as shown in fig. 1, comprising: a satellite surrounding type decompression tower kettle 10 and a rectification section 20; the satellite-surrounded decompression tower bottom 10 comprises a main tower bottom 11 and a plurality of sub-reactors 12 (shown in figures 2 and 3) which are arranged outside the main tower bottom 11 in a satellite-surrounded manner; the main tower kettle 11 is provided with a first outlet and a plurality of injection inlets, and the top of the main tower kettle 11 is provided with an opening; the sub-reactors 12 are provided with second outlets and first inlets, the injection inlets are communicated with the second outlets of the sub-reactors 12 in a one-to-one correspondence manner, and the first outlets are communicated with the first inlets; wherein the injection direction of each injection inlet can be adjusted or the injection directions of at least two injection inlets are crossed, and the volume of the sub-reactor 12 is smaller than that of the main tower 11; the rectifying section 20 is positioned above the main tower kettle 11 and is communicated with the top opening of the main tower kettle 11, and the top of the rectifying section 20 is provided with a light component outlet.

Regarding the hydrogen transfer reaction, part of heavy oil in the atmospheric residue can transfer hydrogen carried by the heavy oil to other components in the collision process, and the hydrogen transfer under the non-hydrogen state is completed, so that one part of heavy oil is heavier, and the other part of heavy oil is lighter. Especially in the process of multiple circulation, injection and impact of the sub-reactors, the hydrogen transfer reaction is more obvious, so that the shallowness and lightness of the atmospheric residue and the circulating oil are realized, and the satellite surrounding type pressure reduction tower kettle plays a role in bearing materials and also plays a role in the reactor.

In order to further improve the light weight of the atmospheric residue and the circulating oil, in a preferred embodiment, as shown in fig. 1, a non-submerged impinging stream assembly 13 is further disposed in the main tower 11, and the non-submerged impinging stream assembly 13 is disposed in the jetting direction of each jet inlet for non-submerged impinging, cavitation and shearing of the jetted material from the jet inlet. By utilizing the assembly, stronger non-submerged impact, cavitation and shearing can be generated in the non-submerged impact flow assembly 13 by the normal pressure residual oil sprayed from the spraying inlet and the oil circularly entering the sub-reactor, so that the reaction efficiency is further enhanced, the light weight degree is improved, and the light oil extraction rate is further improved. Preferably, each first outlet is connected to the first inlet by a circulation line, and a forced circulation pump 14 is further disposed on the circulation line. The forced circulation pump 14 can circulate the oil in the main tower more stably and provide the circulation kinetic energy, even provide the kinetic energy for the injection of the material in the sub-reactors.

In a preferred embodiment, the volume of the sub-reactor 12 is denoted as V1, and the volume of the main column bottom 11 is denoted as V2, V1/V2 is 1/20 to 1/10000. On one hand, the mixing of materials in the sub-reactors is more facilitated, and on the other hand, the treatment efficiency is also improved. In practical application, the volume of the sub-reactors can be adjusted according to the treatment scale, for example, in laboratory scale, V1/V2 is more suitable at 1/20-1/100. On an industrial scale, the value of V1/V2 is lower, preferably 1/100-1/10000. More preferably, the sub-reactors 12 have a volume of 0.025m or less³A pressurized micro-reactor with an inner diameter less than 0.1m or a volume less than or equal to 0.1m³And a normal pressure micro-reactor with an inner diameter less than 0.1 m. By adopting the micro-reactor as a sub-reactor, the problem of non-equilibrium of materials can be solved more effectively, so that the materials are more efficiently and evenly transferred in the aspects of mass transfer, heat transfer and energy transfer, and the effect of light reaction is further improved. In actual production, the specific number of the sub-reactors 12 can be adjusted to at least one according to the treatment amount.

In a preferred embodiment, the vacuum distillation column with satellite tower still further comprises: a vacuum pump 30 connected to the light component outlet; and an offgas tank 40 having a light component inlet connected to an outlet of the vacuum pump 30. Thus, the vacuum pump 30 can provide vacuum environment for the rectifying section 20 and the main tower 11, and also promote the light gas obtained by impacting and flashing to separate different distillate oil in the rectifying section, and the waste gas tank 40 can be used for collecting the light component gas discharged from the top of the rectifying section 20.

More preferably, the off-gas tank 40 also has an outlet for the liquid phase component and an off-gas outlet, which is connected to the first inlet of at least part of the sub-reactors 12. After completion of the rectification in the rectification section 20, the light fraction outlet discharge into the fraction normally comprises a dry gas such as H₂(if hydrogenated), CO₂、CH₄And the like, normal-temperature non-condensable gas such as C2, and a plurality of condensed C3, C4, a small amount of C5 and the like at normal temperature. After being collected in the offgas tank 40, the noncondensable gas component H thereof₂(if hydrogenated), CO₂、CH₄And a small amount of uncondensed C3, C4, etc. can be returned to, for example, main column 11 through at least a portion of sub-reactors 12. Therefore, the waste gas can be used as return gas for gas stripping to replace steam gas stripping (in order to generate more gas phases in the existing pressure reducing tower, a small amount of moisture can be added in the feeding material, water is changed into steam to escape from the liquid at a high speed after entering the pressure reducing tower, light components of hydrocarbons are brought out while the steam comes out, and the extraction rate of the pressure reducing tower is increased), the treatment capacity of waste liquid generated by the steam can be reduced, and the extraction rate of the pressure reducing rectifying tower is further increased. Meanwhile, according to the Dalton law, the partial pressure of oil gas larger than C5 hydrocarbon is reduced by the return of the waste gas, and the pressure in the device is stabilized correspondingly. And the low-carbon hydrocarbons such as methane in the waste gas are likely to participate in the reaction in the sub-reactors again, so that the quantity of the low-carbon hydrocarbons such as methane is reduced. Further, as shown in fig. 1, a balance tank 80 is further provided on a line connecting the light component inlet and the vacuum pump 30 to maintain the vacuum environment stable. The pipeline connecting the waste gas outlet and at least part of the sub-reactors 12 is also provided with a first material conveying pump 90 for providing power.

In order to collect the distillate oil separated from the rectifying section 20, in a preferred embodiment, the side of the rectifying section 20 further has a side draw outlet, the side draw outlet includes a gasoline fraction draw outlet, a diesel fraction draw outlet and a residual distillate draw outlet which are arranged from top to bottom, and the vacuum rectifying tower with the satellite tower still further includes: a gasoline storage tank 50 connected to the gasoline fraction extraction port; a diesel storage tank 60 connected to the diesel fraction extraction port; and a residual distillate oil storage tank 70 connected with the residual distillate oil extraction outlet.

In a preferred embodiment, as shown in fig. 1, the outlet of the residual distillate storage tank 70 is further connected to the first inlet of at least part of the sub-reactor 12. Thus, part of the participated distillate oil (usually 350-500 ℃) can be returned to the sub-reactor and then enters the main tower kettle 11 again for reaction and decompression rectification.

As mentioned above, in the non-submerged impact process, the atmospheric residue and the circulating oil can have a certain degree of hydrogen transfer reaction in the non-hydrogen state, so as to achieve the purpose of light weight. Of course, in order to further enhance the effect of light-weight, in a preferred embodiment, the vacuum distillation column with the satellite tower still further comprises a hydrogen supply unit, and the hydrogen supply unit is connected with the first inlet of at least part of the sub-reactors 12. Thus, new hydrogen can be put into the process of the lightening reaction to promote the lightening reaction of the atmospheric residue oil and the circulating oil stock in the hydrogen state. In practical application, a warming unit may be disposed on the hydrogen supply flow path for warming the hydrogen in advance and then allowing the hydrogen to enter the sub-reactors 12.

After many cycles, vacuum residue will accumulate at the bottom of the main tower 11, and preferably, a vacuum residue discharge port is further provided at the bottom of the main tower 11 for discharging the vacuum residue periodically. As shown in fig. 1, a second feed pump 100 is further disposed on a pipeline where a vacuum residue discharge port is located at the bottom of the main tower 11, for stably discharging vacuum residue.

In order to make the impact, flash evaporation and reaction of the atmospheric residue and the circulating oil more sufficient, in a preferred embodiment, the injection direction of any one injection inlet is crossed with the injection direction of at least one of the rest injection inlets. Thus, each jet material entering can generate non-submerged impact, and the lightening effect is further improved.

To further enhance the non-submerged impingement process, in a preferred embodiment, the non-submerged impingement flow assembly 13 comprises: the casing, the inner chamber of casing is used for providing non-submerged formula striking place, and the casing includes a plurality of injection channels that set up with each injection inlet one-to-one, is provided with a plurality of first pore structures on injection channel's the outer wall, and the axial of first pore structure and injection channel's axial direction have the contained angle. In this way, after the material in each sub-reactor 12 enters the main tower 11, the material can complete the impact in the injection channel, and the secondary fluid generated after the impact enters the first hole structure of the injection channel. Because the axial direction of the first hole structure and the axial direction of the jet channel form an included angle, shearing and cavitation can be formed on the secondary fluid, so that the non-submerged impact effect is further enhanced, and the light reaction effect is improved. The light components after impact, shear and cavitation are flashed to form gas, which enters the rectification section 20 to complete fraction separation.

More preferably, the end of the injection channel remote from the injection inlet is provided with an impingement baseplate; or the radial sectional area of the injection channel is gradually reduced along the direction far away from the injection inlet, and the other end of the injection channel is closed. So set up, be favorable to further improving the striking effect to further improve reaction efficiency, improve the light oil extraction rate.

The non-submerged impinging stream module 13 may be provided as described in patent 201911175767.7, as long as it can achieve non-submerged impingement, shear, and cavitation of the injected material from the sub-reactors 12, and will not be described herein again.

During continuous circulation operation, a portion of the liquid phase material is retained in main column 11, and in order to allow non-submerged impingement of the injected atmospheric residuum and circulating oil in a gaseous environment, in a preferred embodiment, non-submerged impingement flow assembly 13 is disposed at the top of main column 11 adjacent to rectifying section 20. This improves the non-submerged impingement effect and promotes the impingement, reaction and flash to form a gas of lighter components that is immediately introduced into the rectifying section 20.

In a preferred embodiment, the sub-reactors 12 are tubular structures, and a plurality of duct cavitation plates are further disposed inside the sub-reactors 12, and a plurality of second hole structures are disposed on the duct cavitation plates. The use of the pipeline cavitation plate is beneficial to further enhancing the material mixing in the sub-reactor 12, thereby further improving the light reaction effect and increasing the light oil extraction rate. The specific arrangement of the duct cavitation plate may also be as described in patent 201911175767.7, and will not be described herein.

In order to save cost, the vacuum rectification tower with the satellite tower kettle provided by the utility model can be modified on the basis of the existing vacuum rectification tower, such as: as shown in fig. 4, the main tower 11 includes a tower body 111, a stripping section 112 and a feeding section 113 from bottom to top in sequence, the injection inlet is disposed at the feeding section 113, the first outlet is disposed at the tower body 111, and the feeding section 113 is further provided with an atmospheric residue inlet. With such arrangement, on the basis of the existing vacuum rectification tower, the sub-reactor 12, an optional non-submerged impact component and other components are added, and the circulating oil material of the sub-reactor 12 can cross over the stripping section (only 4 left and right trays) and enter from the tray where the raw material is input (the feeding section 113 and the position with the largest tower diameter). During this period, fresh atmospheric residue can also enter only through the atmospheric residue inlet, and the sub-reactor 12 circulates the oil at the column body 111.

It should be noted that the number of the sub-reactors 12 can be designed according to the volume of the main tower 11, the volume of the sub-reactors 12, the number of cycles, etc., as long as the corresponding number of cycles at the corresponding residence time can be achieved under the corresponding process conditions, and of course, a certain backup capacity can be considered, which is understood by those skilled in the art.

Preferably, the liquid-phase component outlet of the offgas tank 40 is connected to the liquefied gas tank 110 for collecting the components condensed at the normal temperature.

According to another aspect of the present invention, there is also provided a vacuum distillation method for atmospheric residue, which uses the vacuum distillation tower with satellite tower bottom to process atmospheric residue, and the processing process includes the following steps: step S1, introducing the atmospheric residue into at least one sub-reactor 12 through a first inlet, and then further into the main tower bottom 11 through a jet inlet in a jet state; discharging the oil in the main tower 11 from the first outlet, and circulating the oil to at least one sub-reactor 12 to pass through the injection inlet again to enter the main tower 11 in an injection state, and circulating for multiple times; wherein the sub-reactor 12 for introducing the atmospheric residue is the same as or different from the sub-reactor 12 for circulating the oil in the main tower 11; and step S2, the gas-phase light oil obtained in the step S1 enters a rectifying section 20 for vacuum rectification to obtain a gasoline fraction, a diesel fraction, a residual fraction and light component gas.

By using the method, the atmospheric residue raw material can enter through the sub-reactors, the residue entering the vacuum tower kettle can be circulated for many times through a plurality of sub-reactors, or fresh atmospheric residue and the oil returned from the first outlet of the main tower kettle can be mixed in the sub-reactors and then are sent to the main tower kettle, thereby forming a circulation state. On one hand, the continuous circulation of the fresh atmospheric residue and the oil in the kettle can enable the materials to meet the process requirements on mass transfer, heat transfer and energy transfer in the most rapid and simple mode, and the reactor is an efficient reactor. On the other hand, after the fresh atmospheric residue and the oil material in the kettle enter the injection inlets through the sub-reactors, at least two materials collide after being injected in the actual injection process because the injection direction of each injection inlet can be adjusted or the injection directions of at least two injection inlets are crossed. And the collision is carried out in a gas phase environment due to the fact that a liquid phase is in a non-submerged collision process, so that a certain hydrogen transfer reaction can be carried out, the light weight reaction of the atmospheric residue oil and the circulating oil can be promoted, and the high-pressure oil-gas separation device has a good effect on improving the quality and the extraction rate of the hydrogen component of the vacuum distillation tower. The atmospheric residue and the tower bottom oil entering the vacuum tower bottom are continuously circulated, collided and flashed through the sub-reactors to generate gas-phase light oil, the gas-phase light oil enters the upper rectifying section for vacuum rectification to separate gasoline fraction, diesel fraction and residual fraction (usually distillate oil at 350-500 ℃), and the light-component gas phase is collected at the top of the rectifying tower. The atmospheric residue oil is treated by the vacuum distillation tower with the satellite tower kettle, the light oil extraction rate can be effectively improved under relatively mild temperature and pressure environments, and the method is a breakthrough change for energy consumption-benefit data.

In the actual treatment process, the material circularly input by the sub-reactors is oil (residual oil) in the main tower kettle, one or more sub-reactors can also serve as the raw material of the atmospheric residual oil heated by the vacuum furnace, the sub-reactors can also circularly input the material in the tower kettle, and the circulating amount of the sub-reactors is lower than that of the sub-reactors without the raw material.

In order to further enhance the effect of the lightening reaction, in a preferred embodiment, in step S1, the atmospheric residue and the circulating oil in the main column 11 are introduced from the injection inlet and then subjected to non-submerged impingement, cavitation and shearing by the non-submerged impingement flow module 13.

Preferably, the aperture of the spraying inlet is 1-50 mm, and the flow speed of the liquid material entering the spraying inlet is 5-100 m/s.

Considering the factors of energy consumption, light oil extraction rate and the like comprehensively, in a preferred embodiment, the tower top vacuum degree of the rectifying section 20 is 2-5 kPa (micro negative pressure), the reaction temperature in the main tower kettle 11 is 350-400 ℃, the feeding temperature of the atmospheric residue is 380-400 ℃, and the material retention time in the main tower kettle 11 is 0.5-1 h.

In order to improve the lightening effect of the atmospheric residue, improve the balance of materials and improve the treatment efficiency, in a preferred embodiment, in step S1, the oil circulation time in the main tower 11 is 100 to 300 times/h. Of course, it should be noted that the cycle number is for vacuum distillation of atmospheric residue, and the cycle number can be adjusted according to actual conditions for other different raw materials and different reaction conditions. Of course, the number of cycles can be appropriately changed according to the injection speed of the material, and the number of cycles can be appropriately reduced when the injection speed is high, or vice versa.

In a preferred embodiment, in step S1, at least one sub-reactor 12 is selected for introducing hydrogen while introducing atmospheric residue and oil in the main tower 11, and the volume ratio of hydrogen to atmospheric residue is 80-200: 1. Thus, new hydrogen can be put into the process of the lightening reaction to promote the lightening reaction of the atmospheric residue oil and the circulating oil stock in the hydrogen state.

Preferably, the step S2 further includes, after obtaining the light component gas, introducing the light component gas into the waste gas tank 40, and liquefying at normal temperature (20-30 ℃) to obtain liquefied gas and waste gas; the exhaust gas is recycled to at least one of the sub-reactors 12. Therefore, the waste gas can be used as the return gas for gas stripping to replace steam gas stripping, the treatment capacity of the waste liquid generated by steam can be reduced, and the extraction rate of the reduced pressure distillation tower is further increased. Simultaneously, according to dalton's law, waste gas is returned and is reduced and is greater than the oil gas partial pressure of C5 hydrocarbons, has stabilized the operating pressure inside the device correspondingly. And the low-carbon hydrocarbons such as methane in the waste gas are likely to participate in the reaction in the sub-reactors again, so that the quantity of the low-carbon hydrocarbons such as methane is reduced.

When hydrogen is introduced, the new hydrogen entering the main tower kettle participates in the tower kettle waste gas after primary reaction, enters the tower kettle again through a certain sub-reactor, and participates in the continuous circulation process until the hydrogen is completely combined with the residual oil. Therefore, the hydrogen-oil ratio is actually a hydrogen consumption in the process of lightening.

More preferably, in step S1, atmospheric residue is simultaneously passed into main column 11 from an atmospheric residue inlet provided at feed section 113. Thus, the conventional vacuum distillation tower can be transformed to form the vacuum distillation tower, the stripping section 112 and the feeding section 113 are reserved, and the sub-reactor 12 and the optional non-submerged impinging stream assembly 13 are added, so that the energy consumption is saved. In the actual treatment process, the first reduction line of the traditional vacuum distillation tower can be changed into top recovery, and gasoline fraction is output; reducing the second line to output diesel oil fraction; and the wax oil output of the three-line reduction and the four-line reduction is reserved and is used as the distillate oil output.

The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the utility model as claimed.

Example 1

The vacuum rectification tower with satellite tower still shown in figure 1 is adopted for processing, 3 sub-reactors which are arranged in a satellite surrounding way are arranged on the periphery of the main tower still of the vacuum rectification tower, and the sub-reactors are 1/20 of the volume of the main tower still. The non-submerged impingement flow assembly is a housing having an interior for providing a non-submerged impingement site, and the housing includes jet inletsThe plurality of injection channels that mouthful one-to-one set up, the aperture of injection entry is 6 ~ 10mm, and the jet velocity of liquid material is 8 ~ 12 ms, is provided with a plurality of first pore structures (aperture 1 ~ 3mm) on the outer wall of injection channel, and the axial of first pore structure and the axial direction of injection channel have the contained angle. The spray channels all intersect at the central position, and the one end (corresponding to the middle position of each spray channel in the shell) far away from the spray inlet of each spray channel is provided with an impact bottom plate. The volume of the sub-reactor is less than or equal to 0.025m³The pressure microreactor with the inner diameter less than 0.1m is of a tubular structure, a plurality of pipeline cavitation plates are further arranged inside the microreactor, and a plurality of second hole structures (the hole diameter is 1-3 mm) are arranged on the pipeline cavitation plates

Raw materials: venezuela crude oil; treatment capacity: the pilot scale of a laboratory has the raw material treatment capacity of 3-7 kg/h.

Reaction temperature: 370 deg.C

Reaction pressure: low vacuum: the vacuum degree is 2-5 KPa

In the actual operation process, Venezuela crude oil with the temperature of 365-375 ℃ enters from 1 sub-reactor, and oil in the main tower kettle circulates from the other 2 sub-reactors, wherein the circulation frequency is 200-300 times/h. And (3) introducing hydrogen into 1 of the rest 2 sub-reactors, wherein the volume of the hydrogen and the raw oil is 100:1, and circularly rectifying the waste gas in the light component gas for 1.

The actual boiling point of the raw material is approximately equal to 375 DEG C

Light oil extraction rate: 70 percent of

Distillation range of the extracted light oil: IBP-350 ℃ (gasoline and diesel fractions): 100 percent.

Comparative example 1

The method adopts the existing oil refinery vacuum tower and sequentially comprises a vacuum tower kettle, a gas stripping section, a raw material feeding section and a rectifying section from bottom to top. 30 ten thousand tons/a vacuum tower of a certain oil refinery; raw materials: venezuela crude oil;

description of the drawings: venezuela is the country with the most petroleum reserves in the world, but Venezuela crude oil is one of the worst crude oils in the world (API ≈ 10, belonging to heavy oil or extra heavy oil, equivalent to atmospheric residue). Generally, Venezuela crude oil imported China is mainly used for producing road asphalt.

Therefore, the crude oil at the inlet of Venezuela enters a vacuum tower directly for vacuum deep drawing without being treated by a primary distillation tower and an atmospheric tower. Light gasoline and diesel oil and distillate oil with the temperature less than 500 ℃ are obtained after the light oil (wax oil) is extracted and is subjected to hydrocracking; the bottom oil (tail oil) after the wax oil is pulled out is used for producing various asphalts.

The technological parameters are as follows:

equipment: typical 30 ten thousand tons/a vacuum rectification tower

Raw material treatment capacity: 300 KT/a-37.5T/h

Reaction temperature: 385 deg.C

Reaction pressure: high vacuum: the vacuum degree is 92-94 KPa,

the true boiling point of the raw materials: 520 to 540 DEG C

The light oil extraction rate is less than or equal to 50 percent

Distillation range of the extracted light oil:

IBP-350 ℃: 25 percent; 350-500 ℃: 65 percent; the temperature is more than or equal to 500 ℃: 10 percent. Comparative example 1 has harsh conditions of temperature and pressure, 75 percent of distillate oil with temperature higher than 350 ℃ is extracted from the product, and the lightening effect is not good.

And (4) conclusion: the investment-cost-benefit analysis is used for inspecting the traditional vacuum tower and the vacuum rectification tower with the satellite tower kettle, the latter is comprehensively superior to the former, and the light oil extraction rate is 20-50% higher than that of the existing vacuum tower. The utility model provides an improved scheme of the existing vacuum tower, and the investment recovery period of the improved scheme is less than 12 months.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A vacuum rectification column with a satellite type column bottom is characterized by comprising:

the satellite surrounding type pressure reduction tower kettle (10) comprises a main tower kettle (11) and a plurality of sub-reactors (12) which are arranged outside the main tower kettle (11) in a satellite surrounding manner; the main tower kettle (11) is provided with a first outlet and a plurality of injection inlets, and the top of the main tower kettle (11) is provided with an opening; the sub-reactors (12) are provided with second outlets and first inlets, the injection inlets are communicated with the second outlets of the sub-reactors (12) in a one-to-one correspondence manner, and the first outlets are communicated with the first inlets; wherein the injection direction of each injection inlet is adjustable or the injection directions of at least two injection inlets are crossed, and the volume of the sub-reactor (12) is smaller than that of the main tower kettle (11);

the rectifying section (20) is positioned above the main tower kettle (11) and communicated with the top opening of the main tower kettle (11), and the top of the rectifying section (20) is provided with a light component outlet.

2. The vacuum distillation tower with satellite tower bottom according to claim 1, wherein a non-submerged impinging stream assembly (13) is further disposed in the main tower bottom (11), and the non-submerged impinging stream assembly (13) is disposed in the jetting direction of each jetting inlet for non-submerged impinging, cavitation and shearing of the jetted material of the jetting inlet.

3. The vacuum rectification column with satellite type tower bottom according to claim 1, wherein each first outlet is connected with the first inlet through a circulating pipeline, and a forced circulating pump (14) is further arranged on the circulating pipeline.

4. The vacuum distillation column with a satellite column bottom according to any of claims 1 to 3, wherein the volume of the sub-reactor (12) is designated as V1, and the volume of the main column bottom (11) is designated as V2, V1/V2 is 1/20-1/10000.

5. The vacuum distillation column with satellite column bottom according to claim 4, wherein the volume of the sub-reactor (12) is less than or equal to 0.025m³Inner diameter <A pressure micro-reactor with a volume of 0.1m or less³And a normal pressure micro-reactor with an inner diameter less than 0.1 m.

6. The vacuum rectification column with satellite bottoms of any one of claims 1-3, further comprising:

a vacuum pump (30) connected to the light fraction outlet;

an off-gas tank (40) having a light fraction inlet connected to an outlet of the vacuum pump (30).

7. The vacuum distillation column with satellite bottoms of claim 6, wherein said off-gas tank (40) further has a liquid phase component outlet and an off-gas outlet, said off-gas outlet being connected to said first inlet of at least a portion of said sub-reactors (12).

8. The vacuum rectification tower with the satellite type tower bottom as claimed in claim 6, wherein the side of the rectification section (20) is further provided with a side draw outlet, the side draw outlet comprises a gasoline fraction draw outlet, a diesel fraction draw outlet and a residual distillate draw outlet which are arranged from top to bottom, and the vacuum rectification tower with the satellite type tower bottom further comprises:

a gasoline storage tank (50) connected with the gasoline fraction extraction port;

a diesel storage tank (60) connected to the diesel fraction extraction port;

and the residual distillate oil storage tank (70) is connected with the residual distillate oil extraction outlet.

9. The vacuum distillation column with satellite bottoms of claim 8, wherein an outlet of said residual-fraction oil storage tank (70) is further connected to said first inlet of at least a portion of said sub-reactors (12).

10. The vacuum distillation column with satellite bottoms of claim 6, further comprising a hydrogen supply unit connected to said first inlet of at least a portion of said sub-reactors (12).

11. The vacuum rectification column with satellite bottoms of claim 6 wherein the bottom of the main bottom (11) also has a vacuum residue discharge.

12. The vacuum rectification column with a satellite type column bottom according to claim 2, wherein the injection direction of any one of the injection inlets is intersected with the injection direction of at least one of the remaining injection inlets.

13. The vacuum distillation column with satellite bottoms of claim 2, wherein the non-submerged impinging stream assembly (13) comprises:

the inner cavity of the shell is used for providing a non-submerged impact place, the shell comprises a plurality of injection channels which are arranged in one-to-one correspondence with the injection inlets, a plurality of first hole structures are arranged on the outer wall of each injection channel, and included angles are formed between the axial direction of each first hole structure and the axial direction of each injection channel.

14. The vacuum rectification column with satellite tower still as claimed in claim 13, wherein one end of the injection channel away from the injection inlet is provided with an impact bottom plate; or the radial sectional area of the injection channel is gradually reduced along the direction far away from the injection inlet, and the other end of the injection channel is closed.

15. The vacuum distillation column with satellite bottoms of claim 2, wherein the non-submerged impinging stream assembly (13) is disposed at the top end of the main bottom (11) near the rectifying section (20).

16. The vacuum rectification column with satellite tower bottom according to any one of claims 1 to 3, characterized in that the sub-reactor (12) is of a tubular structure, and a plurality of pipeline cavitation plates are further arranged inside the sub-reactor (12), and a plurality of second hole structures are arranged on the pipeline cavitation plates.

17. The vacuum rectification column with satellite tower bottom according to any one of claims 1 to 3, characterized in that the main tower bottom (11) comprises a tower bottom body (111), a stripping section (112) and a feeding section (113) from bottom to top, the injection inlet is arranged at the feeding section (113), the first outlet is arranged at the tower bottom body (111), and the feeding section (113) is further provided with an atmospheric residue inlet.