Separator and method for separating crude oil

Abstract

The present invention relates to a separator and a method for separating crude oil. The separator comprises: a shell and a second support member having a gap with the wall of the separation chamber, a first support member sealed and connected to the shell being spaced apart above the second support member along the height direction of the separation chamber; the second support member is an impermeable support member, and an overflow plate is provided at one end of the gap, the overflow plate, the second support member and the wall of the separation chamber together form a second phase separation zone; each first support member comprises a permeable support portion and an impermeable support portion, an overflow plate is provided between the permeable support portion and the impermeable support portion, so that the overflow plate and the wall of the separation chamber together form a first phase separation zone, and a decompression medium is provided in the first phase separation zone and the second phase separation zone. The separator of the present invention can separate different components in crude oil using carbon dioxide at a relatively low temperature.

Description

Technical Field

[0001] The present invention relates to the field of crude oil separation and refining, and in particular to a separator and a method for separating crude oil. Background Art

[0002] Crude oil is a mixture of multiple components that require separation before it can be processed into various chemical products, such as gasoline and diesel refining and catalytic reforming. Crude oil fractions can be classified by carbon number. These components are classified from light to heavy, i.e., naphtha, gasoline, kerosene, diesel, and residual oil.

[0003] Atmospheric distillation is a traditional crude oil separation process. After dehydration, desalting, and initial distillation and stripping, crude oil enters an atmospheric distillation tower. The bottom of the tower is heated to 300-450°C. Some of the heated crude oil vaporizes and flows upward. The remaining portion, a mixture of heavy components containing a large amount of residual oil and wax oil, exits the tower as the bottom oil product. The vaporized components cool as they flow upward, and the cooled oil phase is discharged as a side stream. These products are arranged from low to high carbon number, from heavy to light. Atmospheric distillation effectively separates crude oil components by exploiting their different boiling points. However, atmospheric distillation requires heating the crude oil to high temperatures, which consumes significant fossil energy and emits significant amounts of CO2. In an era of increasingly stringent environmental requirements and rising carbon emissions costs, new crude oil separation technologies are needed to reduce the temperature and energy consumption during crude oil separation, while also lowering the carbon emissions of separation and refining. Summary of the Invention

[0004] The present invention aims to overcome the problems of high operating temperature and high carbon emissions in crude oil separation techniques in the prior art, and to provide a separator and a method for separating crude oil. The separator is characterized by low operating temperature, high carbon dioxide utilization, high oil separation efficiency, large crude oil processing capacity, and good continuity for crude oil separation. Research has found that components in crude oil can dissolve in high-pressure carbon dioxide at relatively low temperatures, and that different components in crude oil have different solubilities and partition coefficients in carbon dioxide, especially supercritical carbon dioxide. The solubility and partition coefficient of the same component in carbon dioxide vary with temperature, pressure, and the ratio of carbon dioxide to crude oil.

[0005] In order to achieve the above object, the present invention provides a separator in a first aspect, comprising:

[0006] The shell and the shell peripheral wall surround a defined separation chamber, the shell top is provided with a gas phase and / or supercritical phase product outflow outlet, and the bottom is provided with a liquid phase product outflow outlet;

[0007] A second support member is horizontally arranged in the separation chamber, with a gap between one side and the chamber wall of the separation chamber. At least one first support member is spaced apart and horizontally sealed with the shell above the second support member along the height direction of the separation chamber.

[0008] The second support member is an impermeable support member. The second support member (17) is provided with an overflow plate (23) at one end of the gap. Both sides of the overflow plate (23) are sealed and connected to the shell, so that the overflow plate, the second support member and the cavity wall of the separation chamber are surrounded to form a second phase separation zone. The second phase separation zone is used for mixing raw materials, forming a low-density material flow and a high-density material flow, and enriching the high-density material flow and overflowing through the gap to the liquid product flow outlet;

[0009] Each of the first support members includes a permeable support portion and an impermeable support portion, an overflow plate sealedly connected to the shell on both sides is provided between the permeable support portion and the impermeable support portion, so that the overflow plate and the cavity wall of the separation cavity located on one side of the permeable support portion together form a first phase separation zone, and the overflow plate and the cavity wall of the separation cavity located on the side of the impermeable support portion together form a liquid collection zone, wherein the first phase separation zone is used to form a low-density material flow and a high-density material flow and to enrich the high-density material flow, and the liquid collection zone is used to collect the high-density material flow overflowing from the first phase separation zone; a side product outlet is provided on the shell located in the liquid collection zone;

[0010] A decompression medium is provided in the first phase separation zone and the second phase separation zone;

[0011] The second phase separation zone is provided with a first feed inlet for feeding liquid-phase raw materials and a second feed inlet located below the first feed inlet for feeding gas-phase and / or supercritical-phase raw materials.

[0012] A second aspect of the present invention provides a method for separating crude oil, which is carried out in an apparatus comprising the separator of the present invention, comprising:

[0013] a. Injecting the pretreated crude oil into the second phase separation zone through the first feed port, and injecting the carbon dioxide-containing feedstock into the second phase separation zone through the second feed port, wherein the crude oil and the carbon dioxide-containing feedstock are mixed in the second phase separation zone to form a high-density oil-rich phase material flow and a low-density carbon dioxide-rich phase material flow;

[0014] b. The oil-rich phase formed in step a accumulates on the decompression medium in the second phase separation zone, flows from the gap to the bottom of the tower after the accumulated height exceeds the overflow plate, and exits the separation tower through the liquid product outlet; the carbon dioxide-rich phase formed in step a flows upward, passes through the first support member and the decompression medium, and precipitates a side product and a carbon dioxide phase to be separated;

[0015] c. The side product from the previous step accumulates on the buffer medium in the first phase separation zone. When the accumulated height exceeds the overflow plate, the overflow falls into the liquid collection zone and is output from the separation tower through the side product outlet of the liquid collection zone. The carbon dioxide-rich phase to be separated from the previous step flows upward, passes through the first support member and the pressure-reducing medium of the next stage, and precipitates into the next stage side product and the next stage carbon dioxide-rich phase.

[0016] d. After step c is completed, optionally repeat step c at least once;

[0017] e. The carbon dioxide-rich phase obtained in the last step is output from the separation tower through the gas phase and / or supercritical phase product flow outlet, and optionally input into the separation tower through the second feed port after heat exchange.

[0018] Through the above technical solution, the present invention has the following beneficial effects:

[0019] The separator of the present invention can use carbon dioxide to separate and purify different components in crude oil at a relatively low temperature. By adjusting the temperature, pressure, and material ratio parameters, the mixture of crude oil and carbon dioxide is divided into a high-density oil-rich phase and a low-density carbon dioxide-rich phase. The carbon dioxide-rich phase moves upward in the separation tower. By reducing the carbon dioxide phase pressure, the dissolved oil phase is separated from the carbon dioxide in descending order of component weight. By collecting the separated and precipitated oil phase, a separated and purified oil phase product is obtained. The carbon dioxide, which serves as an oil separation carrier, can be reused, thereby improving carbon dioxide utilization. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 is a separation tower according to a preferred embodiment of the present invention;

[0021] Figure 2 It is a float valve on an ordinary float valve tray;

[0022] Figure 3 It is a float valve with a pressure control spring installed on the tower plate;

[0023] Figure 4 It is the first supporting member with a pressure control device spring.

[0024] Description of Reference Numerals

[0025] 1. Shell;

[0026] 2. First feed port;

[0027] 3. External carbon dioxide pipeline;

[0028] 4. Second feed port;

[0029] 5. Liquid product outflow port;

[0030] 6. Gas phase and / or supercritical phase product outflow port;

[0031] 7-9, side line product export;

[0032] 10-14, pressure control device;

[0033] 15. The first phase zone;

[0034] 16. Liquid collection area;

[0035] 17. Second support member;

[0036] 18. First support member;

[0037] 19. Booster device;

[0038] 20. Second phase zone;

[0039] 21. Permeable support portion;

[0040] 22. Impermeable support portion;

[0041] 23. Overflow plate;

[0042] 24. Spring;

[0043] 25. Sealing piece;

[0044] 26. Sealed partition. DETAILED DESCRIPTION

[0045] The endpoints of the ranges and any values ​​disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered to be specifically disclosed herein.

[0046] In the present invention, unless otherwise specified, the "bottom" of the housing refers to the position 90-100% from the top to the bottom of the housing, and the "top" refers to the position 0-10% from the top to the bottom of the housing.

[0047] In the present invention, unless otherwise specified, directional words such as "up, down, left, right" generally refer to up, down, left, right as shown in the reference drawings; "inside, outside" refer to inside and outside relative to the outline of each component itself.

[0048] In the present invention, the terms "high" and "low" in the low-density material flow and high-density material flow are relative concepts, that is, they are used to distinguish two material flows with different densities formed in the phase separation zone.

[0049] like Figure 1The first aspect of the present invention provides a separator, comprising:

[0050] The shell 1 and the shell peripheral wall surround a defined separation chamber, the shell top is provided with a gas phase and / or supercritical phase product outflow outlet 6, and the bottom is provided with a liquid phase product outflow outlet 5;

[0051] A second support member 17 is horizontally arranged in the separation chamber, with a gap between one side and the chamber wall of the separation chamber. Above the second support member 17, at least one first support member 18 is spaced apart along the height direction of the separation chamber and is horizontally sealed and connected to the shell.

[0052] The second support member 17 is an impermeable support member. An overflow plate 23 is provided at one end of the gap of the second support member 17. Both sides of the overflow plate 23 are sealedly connected to the overflow plate 23 of the shell, so that the overflow plate 23, the second support member 17 and the cavity wall of the separation chamber form a second phase separation zone 20. The second phase separation zone 20 is used for mixing raw materials and forming a low-density material flow and a high-density material flow, and enriching the high-density material flow and overflowing through the gap to the liquid product flow outlet 5;

[0053] Each first support member 18 includes a permeable support portion 21 and an impermeable support portion 22, and an overflow plate 23 is provided between the permeable support portion 21 and the impermeable support portion 22, with both sides sealingly connected to the shell, so that the overflow plate 23 and the cavity wall of the separation chamber located on the side of the permeable support portion 21 are surrounded to form a first phase separation zone 15, and the overflow plate 23 and the cavity wall of the separation chamber located on the side of the impermeable support portion 22 are surrounded to form a liquid collection zone 16, wherein the first phase separation zone 15 is used to form a low-density material flow and a high-density material flow and to enrich the high-density material flow, and the liquid collection zone 16 is used to collect the high-density material flow overflowing from the first phase separation zone 15; a side line product outlet is provided on the shell located in the liquid collection zone 16;

[0054] A decompression medium is provided in the first phase separation zone 15 and the second phase separation zone 20;

[0055] The second phase separation zone 20 is provided with a first feed inlet 2 for feeding liquid-phase raw materials and a second feed inlet 4 located below the first feed inlet 2 for feeding gas-phase and / or supercritical-phase raw materials.

[0056] The separator of the present invention can use carbon dioxide to separate and purify different components in crude oil at a relatively low temperature. By adjusting the temperature, pressure, and material ratio parameters, the mixture of crude oil and carbon dioxide will be divided into a high-density oil-rich phase and a low-density carbon dioxide-rich phase. The carbon dioxide-rich phase will move upward in the separation tower. By reducing the pressure of the carbon dioxide-rich phase, the dissolved oil phase will precipitate from the carbon dioxide according to the components from heavy to light. By collecting the separated and precipitated oil phase, a separated and purified oil phase product is obtained. The separation tower has the characteristics of low operating temperature, high carbon dioxide utilization rate, high oil separation efficiency, large crude oil processing capacity, and good continuity.

[0057] In the present invention, there is no particular limitation on the height at which the decompression medium is positioned, as long as the objectives of the present invention can be achieved. According to a preferred embodiment of the present invention, the decompression medium is positioned 1-1000 cm below the height of the overflow plate 23, preferably 2-100 cm below the height of the overflow plate 23, and more preferably 3-50 cm below the height of the overflow plate 23. By adopting this preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and separation energy consumption can be reduced.

[0058] In the present invention, the decompression medium can enhance gas-liquid mass transfer and reduce the pressure of the gas after passing through. There are many types of decompression media to choose from, as long as they can achieve the aforementioned purpose of the present invention.

[0059] According to a preferred embodiment of the present invention, the decompression medium is a tray, and the theoretical number of trays in the separation tower is 1-100, preferably 2-80, and more preferably 3-70. By adopting the above preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0060] According to a preferred embodiment of the present invention, the decompression medium is a tray, and each tray within the first phase separation zone 15 and the second phase separation zone 20 is provided with a first pressure control device for reducing the pressure of the gas after passing through. Preferably, the first pressure control device has an opening pressure difference of 0.01-5 MPa, more preferably 0.05-4 MPa, and even more preferably 0.08-2 MPa. By adopting this preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0061] According to a preferred embodiment of the present invention, when the decompression medium is a tray 56, trays 1-16 are located in the second phase separation zone 20, trays 17-21 are located in the first phase separation zone 15 of the first stage, trays 22-36 are located in the first phase separation zone 15 of the second stage, trays 37-56 are located in the first phase separation zone 15 of the third stage, wherein trays 1-16 are ordinary float valve trays (such as Figure 2 ), the 17-56 stage tower plates are valve tower plates equipped with pressure control devices (such as Figure 3 ).

[0062] According to a preferred embodiment of the present invention, the first pressure control device is selected from at least one of a spring, a pressure reducing valve, an unloading valve, a low-permeability filler, a throttle hole, and a needle valve.

[0063] According to a preferred embodiment of the present invention, the decompression medium is a filler, and the permeability of the filler in each of the first phase separation zone 15 and the second phase separation zone 20 is 0.01-100 Darcy, preferably 0.05-70 Darcy, and more preferably 0.1-40 Darcy. By adopting this preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0064] In the present invention, the number of first support members 18 can be selected according to conventional methods in the art. According to a preferred embodiment of the present invention, the number of first support members 18 is N, where N is a positive integer not less than 1, preferably 1-21, more preferably 1-11, and even more preferably 2-6. By adopting this preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and separation energy consumption can be reduced.

[0065] According to a preferred embodiment of the present invention, a second pressure control device is provided on the permeable support portion 21 of the first support member 18 to reduce the pressure of the gas after passing through. By adopting the above preferred solution, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0066] According to a preferred embodiment of the present invention, the opening pressure difference of the second pressure control device is 0.1-20 MPa, more preferably 0.5-10 MPa, and even more preferably 0.8-5 MPa. By adopting the above preferred solution, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0067] According to a preferred embodiment of the present invention, the second pressure control device is selected from at least one of a spring, a pressure reducing valve, an unloading valve, a low-permeability filler, a throttle hole, and a needle valve.

[0068] like Figure 4 , a spring is provided on the permeable support portion 21 of the first support member 18.

[0069] According to a preferred embodiment of the present invention, a pressurizing device 19 is provided on the feed pipeline of the second feed port 4 .

[0070] According to a preferred embodiment of the present invention, a heat exchange device is provided on the pipelines of the first feed port 2 and the second feed port 4. By adopting the above preferred solution, energy consumption can be further reduced.

[0071] According to a preferred embodiment of the present invention, each of the side product outlets, the gas phase and / or supercritical phase product flow outlet 6 and the liquid phase product flow outlet 5 is provided with an outlet pressure control device.

[0072] According to a preferred embodiment of the present invention, when the number of the first support members 18 is 3, there are three side product outlets 7, 8, and 9 on the outer wall of the separation tower from top to bottom, and are respectively provided with pressure control devices 11, 12, and 13; the gas phase and / or supercritical phase product flow outlet 6 of the separation tower is provided with a pressure control device 14, and the liquid phase product flow outlet 5 is provided with a pressure control device 10.

[0073] According to a preferred embodiment of the present invention, the gas phase and / or supercritical phase product outflow port 6 is connected to the second feed port 4 for reuse of the oil-separated carrier carbon dioxide.

[0074] A second aspect of the present invention provides a method for separating crude oil, which is carried out in a device comprising the separator of the present invention, comprising:

[0075] a. Injecting the pretreated crude oil into the second phase separation zone 20 through the first feed port 2, and injecting the carbon dioxide-containing feedstock into the second phase separation zone 20 through the second feed port 4. The crude oil and the carbon dioxide-containing feedstock are mixed in the second phase separation zone 20 to form a high-density oil-rich phase material flow and a low-density carbon dioxide-rich phase material flow;

[0076] b. The oil-rich phase formed in step a accumulates on the decompression medium in the second phase separation zone 20. After the accumulated height exceeds the overflow plate 23, it flows into the bottom of the tower from the gap and exits the separation tower through the liquid product outlet 5. The carbon dioxide-rich phase formed in step a flows upward, passes through the first support member and the decompression medium, and precipitates a side product and a carbon dioxide-rich phase to be separated.

[0077] c. The side product from the previous step accumulates on the buffer medium in the first phase separation zone 15. After the accumulated height exceeds the overflow plate 23, it overflows into the liquid collection zone 16 and is output from the separation tower through the side product outlet of the liquid collection zone 16. The carbon dioxide-rich phase to be separated from the previous step flows upward, passes through the first support member 18 of the next stage and the decompression medium, and precipitates into the next stage side product and the next stage carbon dioxide-rich phase.

[0078] d. After step c is completed, the new side product and the carbon dioxide-rich phase may be optionally treated at least once according to the process of step c;

[0079] e. The carbon dioxide-rich phase obtained in the last step is output from the separation tower through the gas phase and / or supercritical phase product outlet 6, and optionally input into the separation tower through the second feed port 4 after heat exchange.

[0080] The step d can be understood as follows: the product obtained in the previous step is subjected to the same process as in step c, i.e., the side product is accumulated on the buffer medium in the new first phase separation zone 15, and after the accumulation height exceeds the overflow plate 23, the overflow falls into the new liquid collecting zone 16 and is then output from the separation tower; the carbon dioxide-rich phase to be separated flows upward, passes through the next-stage first support member 18 and the pressure-reducing medium to precipitate the next-stage side product and the next-stage carbon dioxide-rich phase. This process can be performed once or more than once. When it is performed more than once, the second time is to perform the same process as in step c on the product obtained in the first step, and so on.

[0081] By adopting the method of the present invention to separate crude oil, the utilization rate of carbon dioxide and the oil separation efficiency can be improved, and the separation energy consumption can be reduced.

[0082] According to a preferred embodiment of the present invention, in step a, the pretreatment includes dehydration, desalination and removal of impurity gases.

[0083] In the present invention, the carbon dioxide raw material in step a can be an external carbon dioxide material flow 3 and / or a gas phase and / or supercritical phase product flow from the top of a separation tower.

[0084] In the present invention, the mass concentration of carbon dioxide in the carbon dioxide-containing feedstock is not particularly limited as long as the objectives of the present invention can be achieved. According to a preferred embodiment of the present invention, in step a, the mass concentration of carbon dioxide in the carbon dioxide-containing feedstock is 60-100wt%, preferably 70-100wt%, and more preferably 90-100wt%. By adopting the above preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0085] In the present invention, the ratio of the crude oil injection rate to the CO2-containing feedstock injection rate in step a is not particularly limited. According to a preferred embodiment of the present invention, in step a, the ratio of the crude oil injection rate to the CO2-containing feedstock injection rate is 2:1 to 1:40. By adopting this preferred embodiment, the CO2 utilization rate and oil separation efficiency can be further improved, and separation energy consumption can be reduced.

[0086] According to a preferred embodiment of the present invention, the pressure range of the liquid product outlet 5 is 3-30 MPa, preferably 4-25 MPa, and more preferably 10-15 MPa, and the pressure range of the gas and / or supercritical product outlet 6 is 1-25 MPa, preferably 2-20 MPa, and more preferably 3-10 MPa. By adopting the above preferred embodiment, the carbon dioxide utilization rate and oil separation efficiency can be further improved, and the separation energy consumption can be reduced.

[0087] In the present invention, the feed conditions of the crude oil and the carbon dioxide-containing raw material in step a can be conventional choices in the art. According to a preferred embodiment of the present invention, the feed conditions of the crude oil and the carbon dioxide-containing raw material in step a include: a feed temperature of 0-200°C, preferably 10-180°C, and more preferably 20-150°C.

[0088] According to a preferred embodiment of the present invention, the feed pressure is 3-30 MPa, preferably 4-25 MPa, and more preferably 10-15 MPa.

[0089] The present invention will be described in detail below through examples. In the following examples, the content parameters of each component were measured by mass spectrometry and chromatography analysis methods.

[0090] Example 1

[0091] The composition of crude oil A after dehydration, desalting and degassing pretreatment is shown in Table 1 below:

[0092] Table 1

[0093] Components Quality score Components Quality score Components Quality score C4 cut 0.00％ C12 cut 4.87％ C20 cut 2.78％ C5 cut 0.30％ C13 cut 5.43％ C21 cut 2.92％ C6 cut 0.67％ C14 cut 5.22％ C22 cut 3.05％ C7 cut 1.84％ C15 cut 5.05％ C24 cut 3.33％ C8 cut 3.67％ C16 cut 4.27％ C28 cut 3.88％ C9 cut 3.78％ C17 cut 4.07％ C32 cut 13.29％ C10cut 3.50％ C18 cut 4.22％ C36+cut 14.95％ C11cut 4.98％ C19 cut 3.94％

[0094] Separation device such as Figure 1 shown.

[0095] The internal temperature of the separation tower is stabilized at 50°C. The crude oil inlet is between trays 6 and 7, and the CO2-containing gaseous feedstock (including overhead gas and external pure CO2) is inlet between the first tray and an impermeable second support member (one side of which has a gap with the wall of the separation chamber, and an overflow plate with two sides sealed to the shell is located at one end of the gap, so that the overflow plate, the second support member, and the wall of the separation chamber enclose a second phase separation zone, the same below). The outlets for the bottom oil (liquid product stream) and top gas (gas or supercritical product stream) are installed at the bottom and top of the tower, respectively. The three side product oil outlets are located between the 17th, 22nd, and 37th tower plates and the corresponding first support members (a combination of a permeable support portion and an impermeable support portion, with an overflow plate sealed on both sides connected to the shell between the permeable support portion and the impermeable support portion, so that the overflow plate and the cavity wall of the separation chamber located on one side of the permeable support portion together form a first phase separation zone, and the overflow plate and the cavity wall of the separation chamber located on the side of the impermeable support portion together form a liquid collection zone, the same below). Each outlet is equipped with a backpressure valve. The backpressure control range of the backpressure valve for the bottom oil outlet is 10-11 MPa, the backpressure control range of the backpressure valve for the top gas outlet is 3-4 MPa, and the backpressure control ranges of the three side product outlets are 8.5-9.5 MPa, 6-7 MPa, and 3-4 MPa, respectively. There are 56 stages in the separation tower, which are divided into four parts: stages 1-16 correspond to the bottom oil, stages 17-21 correspond to the side 1 product oil, stages 22-36 correspond to the side 2 product, and stages 37-56 correspond to the side 3 product and the top gas (in this embodiment, the gaseous carbon dioxide-rich phase). Stages 1-16 are ordinary float valve trays, and stages 17-56 are float valve trays equipped with a pressure control device. The pressure control device here is a strong spring, such as Figure 2 As shown. The opening pressure difference of an ordinary float valve is basically zero, and the opening pressure difference of a float valve with a pressure-controlling spring is 0.1 MPa, that is, the pressure of the CO2 phase remains basically unchanged when passing through an ordinary float valve tray, while the pressure is reduced by 0.1 MPa when passing through a layer of pressure-controlling float valve tray. The top of each overflow plate is 10 cm higher than the adjacent tray, the side is aligned and sealed with the adjacent tray, one end of the bottom is aligned and sealed with the adjacent support plate, and the other end is aligned and sealed with the side product oil outlet. In this embodiment, the support plate corresponding to the bottom oil is the second support member of the impermeable support, and the support corresponding to the side product oil is the first support member composed of a permeable support part and an impermeable support part, and the permeable support part of the first support member is provided with a strong spring pressure control device, such as Figure 3 The spring opening pressure is 1 MPa. A compression pump and heat exchanger are installed at the feed inlet to maintain the feed temperature and pressure at 50°C and 11 MPa respectively.

[0096] After stable operation, the feed and discharge flow rates are shown in Table 2. The bottom oil and side product oil produced from the separation tower contain a large amount of CO2. The composition and purity change rate of the bottom oil and side product oil after degassing are shown in Table 3. The composition of the overhead gas in the feed and discharge remains unchanged, as shown in Table 4. After oil separation in this example, the bottom oil obtained is rich in C28-C36+ components, and the purity of the corresponding components is increased by 59.71-125.2%. The obtained side product oil 1 is rich in C16-C24 components, and the purity of the corresponding components is increased by 44.58-74.43%. The obtained side product oil 2 is rich in C5-C16 components, and the purity of the corresponding components is increased by 43.20-120.67%. The obtained side product oil 3 is rich in C5-C13 components, and the purity of the components is increased by 51.04-299.45%. Therefore, the apparatus of this embodiment can achieve continuous and effective separation of large quantities of crude oil at 50°C, reducing the energy consumption and safety risks associated with high distillation temperatures. The overhead gas, which contains a large amount of CO2, is recycled, thus achieving high CO2 utilization. The CO2 generated after product degassing can be collected and reinjected, achieving net-zero CO2 emissions from the process.

[0097] Table 2

[0098] Feed Flow rate (t / h) Discharging Flow rate (t / h) crude 25.6 tower bottom oil 16.0 <![CDATA[Pure CO2]]> 14.2 Side 1 line oil 13.6 Top gas 960.2 Side 2 line oil 9.05 Side 3 line oil 1.18 Top gas 960.2

[0099] Table 3

[0100]

[0101] Table 4

[0102] Components Feed Discharging C5 cut 0.10％ 0.10％ C6 cut 0.10％ 0.10％ C7 cut 0.16％ 0.16％ C8 cut 0.17％ 0.17％ C9 cut 0.09％ 0.09％ C10cut 0.04％ 0.04％ <![CDATA[CO2]]> 99.34％ 99.34％

[0103] Example 2

[0104] The crude oil B component after dehydration, desalting and degassing pretreatment is shown in Table 5.

[0105] Table 5

[0106] Components Quality score Components Quality score Components Quality score C4 cut 0.00％ C12 cut 4.10％ C20 cut 2.35％ C5 cut 2.10％ C13 cut 4.47％ C21 cut 2.48％ C6 cut 2.72％ C14 cut 4.28％ C22 cut 2.61％ C7 cut 5.14％ C15 cut 4.16％ C24 cut 2.86％ C8 cut 7.09％ C16 cut 3.52％ C28 cut 3.38％ C9 cut 5.26％ C17 cut 3.40％ C32 cut 11.68％ C10cut 3.78％ C18 cut 3.52％ C36+cut 13.22％ C11cut 4.56％ C19 cut 3.32％

[0107] The separation tower structure used in this embodiment is different from that used in Example 1 in that:

[0108] The separation tower in this example lacks a heat exchanger, so the temperature inside the tower gradually decreases with increasing height. After stable operation, the temperatures at the 1st, 17th, 27th, and 37th trays were 50°C, 47.3°C, 45.8°C, and 40.5°C, respectively. Furthermore, conventional trays were used, relying solely on permeable supports for pressure control. A detailed description follows.

[0109] The crude oil inlet is located between trays 6 and 7, while CO2 is injected along with the overhead gas between the first tray and the impermeable support. The bottom oil (liquid product stream) and overhead gas (gas or supercritical product stream) outlets are located at the bottom and top of the tower, respectively. The three side product oil outlets are located between trays 17, 27, and 37 and their corresponding first support members. Each outlet is equipped with a backpressure valve. The control range for the bottom oil outlet is 12-13 MPa, the control range for the overhead gas outlet is 7-8 MPa, and the control ranges for the three side product outlets are 9.5-10.5 MPa, 8.5-9.5 MPa, and 7-8 MPa, respectively. There are 46 stages in the separation tower, which are divided into four parts: stages 1-16 correspond to the bottom oil, stages 17-26 correspond to the side 1 product oil, stages 27-36 correspond to the side 2 product, stages 37-46 correspond to the side 3 product and the top gas (supercritical carbon dioxide-rich phase in this embodiment). All stages are ordinary stages, and their pressure drop can be ignored. The top of each overflow plate is 10 cm higher than the adjacent stage, the side is aligned and sealed with the adjacent stage, one end of the bottom is aligned and sealed with the adjacent support plate, and the other end is aligned and sealed with the side product oil outlet. In this embodiment, the support plate corresponding to the bottom oil is a second support member of an impermeable support, and the support corresponding to the side product oil is a first support member composed of a permeable support portion and an impermeable support portion, and the permeable support portion of the first support member is provided with a strong spring pressure control device. The permeable support element for the product oil in side line 1 has a pressure-control spring opening differential pressure of 2.5 MPa; the permeable support element for the product oil in side line 2 has a pressure-control spring opening differential pressure of 1 MPa; and the permeable support element for the product oil in side line 3 has a pressure-control spring opening differential pressure of 1.5 MPa. A compression pump and heat exchanger are installed at the feed inlet to maintain the feed temperature and pressure at 50°C and 13 MPa, respectively.

[0110] After stable operation, the feed and discharge flow rates are shown in Table 6. The bottom oil and side product oil produced from the separation tower contain a large amount of CO2. The composition and purity change rate of the degassed bottom oil and side product oil are shown in Table 7. The composition of the inlet and outlet overhead gases remained unchanged, as shown in Table 8. The resulting bottom oil was enriched in C28-C36+ components, and the purity of these components increased by 33.48-66.33%. The resulting side product 1 was enriched in C20-C32 components, and the purity of these components increased by 20.71-33.00%. The resulting side product 2 was enriched in C14-C28 components, and the purity of these components increased by 20.88-41.45%. The resulting side product 3 was enriched in C5-C13 components, and the purity of these components increased by 37.87-119.10%. Therefore, the apparatus of this embodiment can achieve continuous and effective separation of large quantities of crude oil without heating the separation tower, reducing the energy consumption and safety risks associated with high distillation temperatures. The overhead gas containing a large amount of CO2 is recycled, so the device of this embodiment can achieve a high utilization rate of CO2. The CO2 generated after product degassing can be collected and reinjected, thus achieving net zero CO2 emissions in the process.

[0111] Table 6

[0112] Feed Flow rate (t / h) Discharging Flow rate (t / h) crude 152.4 tower bottom oil 137.4 <![CDATA[Pure CO2]]> 286.9 Side 1 line oil 52.4 Top gas 560.7 Side 2 line oil 22.4 Side 3 line oil 227.1 Top gas 560.7

[0113] Table 7

[0114]

[0115]

[0116] Table 8

[0117] Components Feed Discharging C5 cut 0.36％ 0.36％ C6 cut 0.29％ 0.29％ C7 cut 0.38％ 0.38％ C8 cut 0.36％ 0.36％ C9 cut 0.19％ 0.19％ C10cut 0.09％ 0.09％ C11cut 0.08％ 0.08％ C12cut 0.05％ 0.05％ C13cut 0.03％ 0.03％ C14cut 0.02％ 0.02％ C15cut 0.01％ 0.01％ C16cut 0.01％ 0.01％ C17cut 0.01％ 0.01％ <![CDATA[CO2]]> 98.12％ 98.12％

[0118] The crude oil C component after dehydration and desalting pretreatment in Example 3 is shown in Table 9.

[0119] Table 9

[0120] Components Quality score Components Quality score Components Quality score C4 cut 0.26％ C14 cut 4.87％ C24 cut 3.20％ C5 cut 0.37％ C15 cut 4.77％ C25 cut 3.33％ C6 cut 0.81％ C16 cut 4.04％ C26 cut 3.47％ C7 cut 2.15％ C17 cut 3.91％ C27 cut 3.60％ C8 cut 4.07％ C18 cut 4.04％ C28 cut 3.73％ C9 cut 3.90％ C19 cut 3.78％ C29 cut 3.86％ C10cut 3.36％ C20 cut 2.67％ C30 cut 4.00％ C11cut 4.57％ C21 cut 2.80％ C32 cut 4.26％ C12cut 4.41％ C22 cut 2.93％ C36+cut 4.80％ C13cut 5.00％ C23 cut 3.07％

[0121] The separation tower structure used in this embodiment is different from that used in Example 1 in that:

[0122] The internal temperature of the separation tower is stabilized at 60°C. The crude oil inlet is between the 6th and 7th stage trays, and the CO2 and overhead gas inlets are between the 1st stage tray and the non-permeable support. The bottom oil (liquid product stream) and overhead gas (gas phase or supercritical product stream) outlets are installed at the bottom and top of the tower, respectively, and the two side product oil outlet heights are located at the 17th and 27th stage trays, respectively. Each outlet is equipped with a back pressure valve. The back pressure valve control range of the bottom oil outlet is 12-13MPa, the back pressure valve control range of the overhead gas outlet is 6-7MPa, and the back pressure valve control range of the two side product outlets is 11-12MPa and 6-7MPa, respectively. There are 46 stages in the separation tower, which are divided into three parts: stages 1-16 correspond to the bottom oil, stages 17-26 correspond to the side 1 product oil, and stages 27-46 correspond to the side 2 product and overhead gas (supercritical carbon dioxide-rich phase in this embodiment). Trays 1-16 are standard valve trays, while trays 17-46 are valve trays equipped with a pressure-control device. The pressure-control device is a powerful spring. The opening differential pressure for standard valves is essentially zero, while the opening differential pressure for valves equipped with pressure-control springs is 0.1 MPa. This means that the CO2 phase maintains essentially constant pressure as it passes through a standard valve tray, but decreases by 0.1 MPa after passing through a pressure-control valve tray. The top of each liquid collector is 15 cm higher than the adjacent tray, its sides are aligned and sealed with the adjacent trays, one end of its bottom is aligned and sealed with the adjacent support plate, and the other end is aligned and sealed with the side product oil outlet. In this embodiment, the support plate corresponding to the bottom oil is an impermeable support. The permeable portion of the support corresponding to the side product oil is replaced by the 17th pressure-control valve tray. The support corresponding to the side product oil is a first support composed of a permeable and impermeable support portion, with the permeable support portion equipped with a powerful spring pressure-control device. The spring-opening differential pressure is 3 MPa. A compression pump and a heat exchanger are installed at the feed inlet to maintain the feed temperature and pressure at 60°C and 13 MPa respectively.

[0123] After stable operation, the feed and discharge flow rates are shown in Table 10. The bottom oil and side product oil produced from the separation tower contain significant amounts of CO2. The composition and purity change rates of the degassed bottom oil and side product oils are shown in Table 11. The composition of the inlet and outlet overhead gases remained unchanged, as shown in Table 12. The resulting bottom oil was enriched in C26-C36+ components, with the purity of these components increased by 41.54-149.49%. The resulting side product oil (1) was enriched in C22-C29 components, with the purity of these components increased by 44.45-60.41%. The resulting side product oil (2) was enriched in C5-C16 components, with the purity of these components increased by 34.77-71.68%. Therefore, the apparatus of this embodiment can achieve continuous and efficient separation of large quantities of crude oil at 60°C, reducing the energy consumption and safety risks associated with high distillation temperatures. The overhead gas, which contains significant amounts of CO2, is recycled, thus achieving high CO2 utilization. The CO2 generated after product degassing can be collected and reinjected, thus achieving net zero CO2 emissions in the process.

[0124] Table 10

[0125] Feed Flow rate (t / h) Discharging Flow rate (t / h) crude 36.87 tower bottom oil 21.15 <![CDATA[Pure CO2]]> 18.34 Side 1 line oil 10.61 Top gas 944.78 Side 2 line oil 23.45 Top gas 944.78

[0126] Table 11

[0127]

[0128]

[0129] Table 12

[0130] Components Feed Discharging C4 cut 0.17％ 0.17％ C5 cut 0.14％ 0.14％ C6 cut 0.14％ 0.14％ C7 cut 0.21％ 0.21％ C8 cut 0.22％ 0.22％ C9 cut 0.12％ 0.12％ C10cut 0.06％ 0.06％ C11cut 0.04％ 0.04％ C12cut 0.02％ 0.02％ C13cut 0.01％ 0.01％ C14cut 0.01％ 0.01％ <![CDATA[CO2]]> 98.88％ 98.88％

[0131] Example 4

[0132] The crude oil, operating conditions and equipment are the same as those in Example 1. The difference is that the plates are replaced with packing. The packing in the separation tower is equivalent to 56 theoretical plates and is divided into four parts: the packing of the 1-16 theoretical plates corresponds to the bottom oil, the packing of the 17-21 theoretical plates corresponds to the side 1 product oil, the packing of the 22-36 theoretical plates corresponds to the side 2 product, and the packing of the 37-56 theoretical plates corresponds to the side 3 product and the top gas. The packing of the 1-16 theoretical plates is ordinary corrugated packing, so the pressure drop of the fluid on the 1-16 theoretical plates is basically zero. The packing of the 17-56 theoretical plates is a low-permeability corrugated packing with a pore size of 0.1-0.5 mm, which is much smaller than that of ordinary corrugated packing. Therefore, the permeability is reduced to 1-10 Darcy, resulting in a pressure drop of 0.1 MPa through each theoretical plate packing. Other conditions are the same as in Example 1.

[0133] After stable operation, the components and flow rates of the bottom oil, side product oil, and top gas were the same as those in Example 1, as shown in Tables 3 and 4. Therefore, after using packing instead of trays, the performance of this embodiment is the same as that of Example 1.

[0134] Example 5

[0135] The crude oil, operating conditions, and apparatus were the same as in Example 2. The difference was that the trays in Example 2 were replaced with packing with the same theoretical number of trays, such as conventional ceramic corrugated packing. The pressure drop of the fluid across conventional packing is essentially zero, so the pressure change is still controlled by the pressure-control support plate. All other conditions were the same as in Example 2.

[0136] After stable operation, the components and flow rates of the bottom oil, side product oil, and overhead gas were the same as those in Example 2, as shown in Tables 7 and 8. Therefore, after using packing instead of trays, the performance of this embodiment was the same as that of Example 2.

[0137] Example 6

[0138] The components of crude oil D after dehydration, desalting and degassing pretreatment are shown in Table 13.

[0139] Table 13

[0140]

[0141]

[0142] The separation tower structure used in this embodiment is different from that used in Example 1 in that:

[0143] The temperature in the separation tower of this embodiment is kept constant at 80° C. Conventional trays are used, and pressure control is achieved by means of permeable supports. A detailed description is as follows.

[0144] The crude oil inlet is located between trays 6 and 7, while CO2 is injected along with the overhead gas between the first tray and the impermeable support. The bottom oil (liquid product stream) and overhead gas (gas or supercritical product stream) outlets are located at the bottom and top of the tower, respectively. The three side product oil outlets are located between trays 17, 27, and 37 and the corresponding first support. Each outlet is equipped with a backpressure valve. The control range of the backpressure valve for the bottom oil outlet is 20-21 MPa, the control range of the backpressure valve for the overhead gas outlet is 11-12 MPa, and the control range of the backpressure valves for the three side product outlets is 17-18 MPa, 14-15 MPa, and 11-12 MPa, respectively. There are 46 stages in the separation tower, which are divided into four parts: stages 1-16 correspond to the bottom oil, stages 17-26 correspond to the side 1 product oil, stages 27-36 correspond to the side 2 product, stages 37-46 correspond to the side 3 product and the top gas (supercritical carbon dioxide-rich phase in this embodiment). All stages are ordinary stages, and their pressure drop can be ignored. The top of each overflow plate is 10 cm higher than the adjacent stage, the side is aligned and sealed with the adjacent stage, one end of the bottom is aligned and sealed with the adjacent support plate, and the other end is aligned and sealed with the side product oil outlet. In this embodiment, the support plate corresponding to the bottom oil is a second support member of an impermeable support, and the support corresponding to the side product oil is a first support member composed of a permeable support portion and an impermeable support portion, and the permeable support portion of the first support member is provided with a strong spring pressure control device. The permeable support element for the product oil in side line 1 has a pressure-control spring with an opening pressure differential of 3 MPa; the permeable support element for the product oil in side line 2 has a pressure-control spring with an opening pressure differential of 3 MPa; and the permeable support element for the product oil in side line 3 has a pressure-control spring with an opening pressure differential of 3 MPa. A compression pump and heat exchanger are installed at the feed inlet to maintain the feed temperature and pressure at 80°C and 21 MPa, respectively.

[0145] After stable operation, the feed and discharge flow rates are shown in Table 14. The bottom oil and side product oil produced from the separation column contain a large amount of CO2. The composition and purity change rate of the degassed bottom oil and side product oil are shown in Table 15. The composition of the inlet and outlet overhead gases remained unchanged, as shown in Table 16. The resulting bottom oil was enriched in C28-C36+ components, and the purity of these components increased by 19.68-65.82%. The resulting side product 1 was enriched in C24-C32 components, and the purity of these components increased by 13.12-29.06%. The resulting side product 2 was enriched in C14-C22 components, and the purity of these components increased by 21.35-27.67%. The resulting side product 3 was enriched in C5-C16 components, and the purity of these components increased by 30.79-95.39%. Although the separation purity was lower compared to Examples 1-3, this example still achieved continuous separation of large quantities of crude oil.

[0146] Table 14

[0147] Feed Flow rate (t / h) Discharging Flow rate (t / h) crude 137.8 tower bottom oil 79.7 <![CDATA[Pure CO2]]> 130.5 Side 1 line oil 98.3 Top gas 731.7 Side 2 line oil 58.2 Side 3 line oil 31.9 Top gas 731.7

[0148] Table 15

[0149]

[0150]

[0151] Table 16

[0152]

[0153]

[0154] The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, various simple variations of the technical solution of the present invention may be made, including combining the various technical features in any other appropriate manner. These simple variations and combinations should also be regarded as disclosed in the present invention and fall within the scope of protection of the present invention.

Claims

1. A separator, characterized in that: The separator comprises: The shell (1) and the shell surround a defined separation chamber, the shell is provided with a gas phase and / or supercritical phase product flow outlet (6) at the top and a liquid phase product flow outlet (5) at the bottom; A second support member (17) is horizontally arranged in the separation chamber, with a gap between one side and the chamber wall of the separation chamber, and at least one first support member (18) is spaced apart above the second support member (17) along the height direction of the separation chamber and is horizontally sealed and connected to the shell; The second support member (17) is an impermeable support member. The second support member (17) is provided with an overflow plate (23) at one end of the gap. Both sides of the overflow plate (23) are sealed and connected to the shell, so that the overflow plate (23), the second support member (17) and the cavity wall of the separation chamber are surrounded to form a second phase separation zone (20). The second phase separation zone (20) is used for mixing raw materials, forming a low-density material flow and a high-density material flow, and enriching the high-density material flow and overflowing through the gap to the liquid product flow outlet (5); Each of the first support members (18) includes a permeable support portion (21) and an impermeable support portion (22), and an overflow plate (23) is provided between the permeable support portion (21) and the impermeable support portion (22), the overflow plate (23) and the cavity wall of the separation cavity located on one side of the permeable support portion (21) are combined to form a first phase separation zone (15), and the overflow plate (23) and the cavity wall of the separation cavity located on one side of the impermeable support portion (22) are combined to form a liquid collection zone (16), wherein the first phase separation zone (15) is used to form a low-density material flow and a high-density material flow and to enrich the high-density material flow, and the liquid collection zone (16) is used to collect the high-density material flow overflowing from the first phase separation zone (15); a side line product outlet is provided on the shell located in the liquid collection zone (16); A decompression medium is provided in the first phase separation zone (15) and the second phase separation zone (20); The second phase separation zone (20) is provided with a first feed port (2) for feeding liquid phase raw materials and a second feed port (4) located below the first feed port (2) for feeding gas phase and / or supercritical phase raw materials.

2. The separator according to claim 1, wherein The height of the decompression medium is 1-1000 cm lower than the height of the overflow plate (23).

3. The separator according to claim 2, wherein The height of the decompression medium is 2-100 cm lower than the height of the overflow plate (23).

4. The separator according to claim 2, wherein The height of the decompression medium is 3-50 cm lower than the height of the overflow plate (23).

5. The separator according to claim 1, wherein The decompression medium is a tray, and the theoretical number of trays in the separation tower is 1-100; and / or The decompression medium is a tray, and each tray in the first phase separation zone (15) is provided with a first pressure control device for reducing the pressure of the gas after passing through; and / or The decompression medium is a filler, and the permeability of the filler in each of the first phase separation zone (15) and the second phase separation zone (20) is 0.01-100 Darcy.

6. The separator according to claim 5, wherein The theoretical number of trays in the separation column is 2-80; and / or The opening pressure difference of the first pressure control device is 0.01-5 MPa; and / or The permeability of the filler in each of the first phase separation zone (15) and the second phase separation zone (20) is 0.05-70 Darcy.

7. The separator according to claim 5, wherein The theoretical number of trays in the separation column is 3-70; and / or The opening pressure difference of the first pressure control device is 0.05-4 MPa; and / or The permeability of the filler in each of the first phase separation zone (15) and the second phase separation zone (20) is 0.1-40 Darcy.

8. The separator according to claim 5, wherein The opening pressure difference of the first pressure control device is 0.08-2MPa.

9. The separator according to claim 1, wherein The number of the first support members (18) is N, where N is a positive integer not less than 1.

10. The separator according to claim 9, wherein N is 1-21.

11. The separator according to claim 9, wherein N is 1-11.

12. The separator according to claim 9, wherein N is 2-6.

13. The separator according to claim 1, wherein A second pressure control device is provided on the permeable support portion (21) of the first support member (18) for reducing the pressure of the gas after the gas passes through.

14. The separator according to claim 13, wherein The opening pressure difference of the second pressure control device is 0.1-20 MPa.

15. The separator according to claim 13, wherein The opening pressure difference of the second pressure control device is 0.5-10 MPa.

16. The separator according to claim 13, wherein The opening pressure difference of the second pressure control device is 0.8-5 MPa.

17. The separator according to any one of claims 1 to 16, wherein: A pressure boosting device (19) is provided on the feed pipeline of the second feed port (4); and / or A heat exchange device is provided on the pipelines of the first feed port (2) and the second feed port (4); and / or Each of the side product outlets, gas phase and / or supercritical phase product flow outlet (6) and liquid phase product flow outlet (5) is provided with an outlet pressure control device; and / or The gas phase and / or supercritical phase product flow outlet (6) is communicated with the second feed inlet (4).

18. A method for separating crude oil, characterized in that: The method is carried out in a device comprising the separator according to any one of claims 1 to 17, comprising the following steps: a. Injecting the pretreated crude oil into the second phase separation zone (20) through the first feed port (2), and injecting the carbon dioxide-containing raw material into the second phase separation zone (20) through the second feed port (4), wherein the crude oil and the carbon dioxide-containing raw material are mixed in the second phase separation zone (20) to form a high-density oil-rich phase material flow and a low-density carbon dioxide-rich phase material flow; b. The oil-rich phase formed in step a accumulates on the decompression medium in the second phase separation zone (20). After the accumulated height exceeds the overflow plate (23), it flows into the bottom of the tower from the gap and is output from the separation tower through the liquid product outlet (5); the carbon dioxide-rich phase formed in step a flows upward, passes through the first support member and the decompression medium, and precipitates a side product and a carbon dioxide-rich phase to be separated; c. The side product of the previous step accumulates on the buffer medium in the first phase separation zone (15), and after the accumulation height exceeds the overflow plate (23), the overflow falls into the liquid collection zone (16) and is output from the separation tower through the side product outlet of the liquid collection zone (16); the carbon dioxide-rich phase to be separated in the previous step flows upward, passes through the first support member (18) of the next stage and the decompression medium, and precipitates the next stage side product and the next stage carbon dioxide-rich phase; e. The carbon dioxide-rich phase obtained in the last step is output from the separation tower through the gas phase and / or supercritical phase product outlet (6).

19. The method according to claim 18, wherein In step a, The carbon dioxide mass concentration in the carbon dioxide-containing raw material is 60-100 wt%; and / or The ratio of the injection rate of the crude oil to the injection rate of the carbon dioxide-containing raw material is 2:1-1:

40.

20. The method according to claim 19, wherein In step a, the mass concentration of carbon dioxide in the carbon dioxide-containing raw material is 70-100 wt%.

21. The method according to claim 19, wherein In step a, the mass concentration of carbon dioxide in the carbon dioxide-containing raw material is 90-100 wt%.

22. The method according to claim 18, wherein The pressure range of the liquid phase product flow outlet (5) is 3-30 MPa, and the pressure range of the gas phase and / or supercritical phase product flow outlet (6) is 1-25 MPa.

23. The method according to claim 22, wherein The pressure range of the liquid phase product outlet (5) is 4-25 MPa, and the pressure range of the gas phase and / or supercritical phase product outlet (6) is 2-20 MPa.

24. The method according to claim 22, wherein The pressure range of the liquid phase product flow outlet (5) is 10-15 MPa, and the pressure range of the gas phase and / or supercritical phase product flow outlet (6) is 3-10 MPa.

25. The method according to any one of claims 18 to 24, wherein: The feed conditions of the crude oil and carbon dioxide-containing raw material in step a include: a feed temperature of 0-200° C.; and / or a feed pressure of 3-30 MPa.

26. The method according to claim 25, wherein The feed conditions of the crude oil and carbon dioxide-containing raw material in step a include: a feed temperature of 10-180° C.; and / or a feed pressure of 4-25 MPa.

27. The method according to claim 25, wherein The feed conditions of the crude oil and carbon dioxide-containing raw material in step a include: a feed temperature of 20-150° C.; and / or a feed pressure of 10-15 MPa.

28. The method according to claim 18, wherein The method further comprises the steps between step c and step e: d. After step c is completed, the new side product and the carbon dioxide-rich phase are treated according to the process of step c.

29. The method according to claim 18, wherein In the step e, the carbon dioxide-rich phase obtained in the last step is fed into the separation tower through the second feed port (4) after heat exchange.

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