阅读说明：本技术 一种催化裂化油剂分离设备、反应再生系统及应用 (Catalytic cracking oil separating equipment, reaction regeneration system and application ) 是由 于敬川 崔守业 刘宪龙 于 2018-06-22 设计创作，主要内容包括：本发明涉及一种催化裂化油剂分离设备、反应再生系统及应用,该设备由上至下包括流体连通的沉降段、稀相汽提段和密相汽提段,所述沉降段设置有第一旋风分离器和催化剂分布柱,所述沉降段和稀相汽提段通过分布板所隔开,所述分布板上设置有用于通过催化剂的分布孔；所述沉降段的侧壁设置有反应油剂入口,顶部设置有油气出口,所述密相汽提段的底部设置有催化剂出口和汽提气入口；所述催化剂分布柱由下至上伸入所述第一旋风分离器的催化剂出口中并与所述催化剂出口的内壁之间形成有将催化剂分散至分布板上的环隙。本发明的油剂分离设备能够提高汽提效率。(The invention relates to a catalytic cracking oil separating device, a reaction regeneration system and application, wherein the device comprises a settling section, a dilute phase stripping section and a dense phase stripping section which are communicated with each other by fluid from top to bottom, the settling section is provided with a first cyclone separator and a catalyst distribution column, the settling section and the dilute phase stripping section are separated by a distribution plate, and the distribution plate is provided with distribution holes for passing a catalyst; the side wall of the settling section is provided with a reaction oil inlet, the top of the settling section is provided with an oil gas outlet, and the bottom of the dense phase stripping section is provided with a catalyst outlet and a stripping gas inlet; the catalyst distribution column extends into the catalyst outlet of the first cyclone separator from bottom to top, and an annular space for dispersing the catalyst to the distribution plate is formed between the catalyst distribution column and the inner wall of the catalyst outlet. The oil separating equipment can improve the stripping efficiency.)

1. A catalytic cracking oil agent separation device comprises a settling section (28), a dilute phase stripping section (23) and a dense phase stripping section (24) which are communicated with each other, wherein a first cyclone separator (18) and a catalyst distribution column (21) are arranged in the settling section (28), the settling section (28) and the dilute phase stripping section (23) are separated by a distribution plate (22), and distribution holes (6) for passing a catalyst are formed in the distribution plate (22);

the side wall of the settling section (28) is provided with a reaction oil agent inlet, the top of the settling section is provided with an oil gas outlet, and the bottom of the dense phase stripping section (24) is provided with a catalyst outlet and a stripping gas inlet;

the first cyclone separator (18) is provided with an oil agent inlet, an oil gas outlet and a catalyst outlet which is arranged downwards, and the oil agent inlet of the first cyclone separator (18) is in fluid communication with the reaction oil agent inlet of the settling section (28);

the catalyst distribution column (21) extends into the catalyst outlet of the first cyclone separator (18) from bottom to top, and an annular gap (4) for dispersing the catalyst to the distribution plate (22) is formed between the catalyst distribution column and the inner wall of the catalyst outlet.

2. An apparatus according to claim 1, wherein the cross-sectional area of the annulus (4) is 10-60% of the cross-sectional area of the catalyst outlet of the first cyclone (18).

3. The apparatus of claim 1, wherein the upper end of the catalyst distribution column (21) is formed in a tapered shape.

4. The apparatus according to claim 3, wherein the catalyst distribution column (21) is formed as a spindle-shaped structure which is arranged vertically in the axial direction and has a tip which projects into the catalyst outlet of the first cyclone (18).

5. The apparatus of claim 4, wherein the fusiform distribution column has a top angle of 30-70 ° and a bottom angle of 20-60 ° on a vertical through-axis plane.

6. The apparatus according to claim 4, wherein the ratio of the maximum diameter of the fusiform distribution column to the internal diameter of the dilute phase stripping section (23) is between 0.1 and 0.3, and the ratio of the length of the fusiform distribution column to the internal diameter of the dilute phase stripping section (23) is between 0.2 and 1.0.

7. The apparatus of claim 1 wherein the centrally upwardly projecting distributor plate (22) is formed as a first conical structure having a top cone angle of 80-160 °.

8. The apparatus according to claim 1, wherein the total open area of the distribution holes (6) amounts to 40-80% of the area of the bottom surface of the distribution plate (22);

the bottom wall of the distribution plate (22) is provided with a first connecting pipe (8) communicated with the distribution holes (6).

9. The apparatus according to claim 1, wherein a dust cover (19) for separating the settling section (28) into an upper settling section (1) and a lower settling section (2) is further arranged in the settling section (28), and oil and gas holes (5) for passing oil and gas are arranged on the dust cover (19);

the first cyclone separator (18) penetrates through the dust cover (19) from top to bottom, an oil agent inlet and an oil gas outlet of the first cyclone separator (18) are located in the upper settling section (1), and a catalyst outlet is located in the lower settling section (2).

10. The apparatus of claim 9 wherein the ratio of the minimum vertical spacing of the dust caps (19) from the distributor plate (22) to the internal diameter of the dilute phase stripping section (23) is from 0.9 to 2.6.

11. Apparatus according to claim 9, wherein the dust shield (19) is formed with an upwardly projecting central part in a second conical configuration with a top cone angle of 90-170 °.

12. The apparatus of claim 9, wherein the open area of the oil and gas holes (5) accounts for 30-75% of the area of the dust cover (19) bottom surface;

the diapire of dust cover (19) is provided with the intercommunication second connecting pipe (7) of oil gas hole (5).

13. The apparatus of claim 1, wherein a second cyclone (29) is further provided in the settling section (28) above the first cyclone (18), the second cyclone (29) being provided with a finish inlet, an oil and gas outlet and a catalyst outlet, the oil and gas outlet of the second cyclone (29) being in fluid communication with the oil and gas outlet of the settling section (28).

14. Apparatus according to claim 13, wherein the first cyclone (18) and the second cyclone (29) each independently comprise a communicating cyclone body and dipleg; the oil agent inlet and the oil gas outlet of the first cyclone separator (18) and the second cyclone separator (29) are arranged on the cyclone separator body, and the catalyst outlet is arranged at the bottom end of the dipleg; the dipleg of the second cyclone (29) extends into the dipleg of the first cyclone (18).

15. The apparatus of claim 1, wherein the ratio of the height of the dilute phase stripping section (23) to the internal diameter of the dilute phase stripping section (23) is 1.1-3.6.

16. A catalytic cracking reaction regeneration system, comprising a riser reactor (17), a regenerator and the catalytic cracking oil separation device of any one of claims 1 to 15, wherein the riser reactor (17) is provided with a raw oil inlet at the lower part, a reaction oil outlet at the top part and a regenerated catalyst inlet at the bottom part, the regenerator is provided with a spent catalyst inlet and a regenerated catalyst outlet, the regenerated catalyst inlet at the bottom part of the riser reactor (17) is communicated with the regenerated catalyst outlet of the regenerator, the reaction oil outlet at the top part of the riser reactor (17) is in fluid communication with the reaction oil inlet of the settling section (28), and the catalyst outlet of the dense phase stripping section (24) is communicated with the spent catalyst inlet of the regenerator.

17. A catalytic cracking oil separation process using the separation apparatus of any one of claims 1 to 15, the separation process comprising:

introducing a reaction oil to be separated into a settling section (28) from a reaction oil inlet of the settling section (28) and separating the reaction oil by a first cyclone separator (18), allowing the obtained catalyst to enter a dilute phase stripping section (23) and a dense phase stripping section (24) through the settling section (28) and a distribution plate (22) to contact with stripping gas entering from a stripping gas inlet at the bottom of the dense phase stripping section (24) and perform countercurrent dilute phase stripping and dense phase stripping from top to bottom, leading the stripped catalyst out of a catalyst outlet of the dense phase stripping section (24), and leading the obtained stripping oil gas out of an oil gas outlet at the top of the settling section (28).

18. The separation process of claim 17, wherein the stripping conditions comprise: the stripping gas superficial velocity of the dilute phase stripping zone (23) is 0.05-0.40 m/s, the relative velocity of the catalyst and the stripping gas is 0.45-0.85 m/s, and the density of the catalyst is 10-100 kg/m³；

The dense phase stripping zone (24) has a catalyst density of 200-900 kg/m³。

19. A method of catalytic cracking, the method of catalytic cracking comprising:

introducing raw oil into the lower part of a riser reactor to contact with a regenerated catalyst from the bottom of the riser reactor and carrying out catalytic cracking reaction, leading out the obtained reaction oil from the top of the riser reactor and separating by adopting the separation method of claim 17 or 18, introducing the obtained reaction oil gas into a subsequent separation unit, introducing the obtained catalyst to be regenerated into a regenerator for regeneration, and introducing the regenerated catalyst obtained by regeneration into the bottom of the riser reactor.

Technical Field

The invention relates to a catalytic cracking oil separating device, a reaction regeneration system and application.

Background

The outlet of the riser reactor of the catalytic cracking device is connected with various fast separation devices for realizing the purpose of terminating the reaction. The inertial fast-separation device realizes gas-solid separation by means of inertial difference caused by density difference of gas-solid phases when the flow direction of oil gas containing the catalyst is changed rapidly, and has the defects that the separation efficiency is low and is only 70-80%, the rebound speed of the catalyst after separation is high, the catalyst is easy to rise very high in a settler, namely the catalyst is seriously mixed back, the device needs a high settling section, and the retention time of the catalyst in the settler is overlong. The centrifugal separation device realizes the rapid separation of gas and solid by means of strong centrifugal force formed by the rapid rotation of the mixture of gas and solid phases. Generally, a riser horizontally enters a settler, the outlet of the riser is directly connected with a simple cyclone separator, the separation efficiency is over 95 percent, and the pressure drop is below 10 kPa. The conveying process of spent agent to dense phase stripping section of centrifugal method includes: from the diplegs directly to the dense phase stripping section and from the outer edge of the stripping section to the dense phase stripping section. The spent catalyst is not stripped in the process of conveying to the dense phase stripping section, so that the overall stripping efficiency is too low, and the stripping time is too long. In addition, under the condition that the separation efficiency of the cyclone separator is certain, the catalyst density at the inlet of the cyclone separator directly influences the separation rate of the catalyst, and the existing patent technologies for reducing the retention time of oil gas in the settler easily cause the excessive catalyst loss due to the overlarge catalyst density at the inlet of the cyclone separator. At present, in the aspect of improving the stripping effect of spent catalyst in the catalytic cracking technology, the increasing of a stripping section turning plate is mainly considered to improve the linear speed of stripping gas, improve the total linear speed of stripping gas, increase the load of stripping gas and increase the blowing speed of oil gas.

Chinese patent CN1072979C provides a method and a device for fast separation of cyclone gas-solid and fast extraction of steam stripping in a riser fluidized reaction system, which are used for fast separation of catalyst and oil gas after reaction and fast extraction of oil gas. The problem is that the quickly-separated oil gas and the catalyst are separated in a space with a smaller diameter, the oil gas is blown upwards by higher stripping gas, the linear speed reaches 0.3-0.4 m/s, the quickly-separated catalyst is blown up again, and the cyclone separator is connected with the closed space at the upper part of the quick separation outlet, so that the effect of reducing the catalyst density of a settling section is lost, the catalyst density entering the cyclone separator is too high, and the separation efficiency of the cyclone separator is reduced or the separation difficulty is improved.

US patent US5552120 provides a riser reactor with an upward outlet, the outlet being a dome-shaped bouncing hood, the stripper is in a semi-closed state with the settler, the stripped catalyst overflows to the settler for secondary stripping, the separation efficiency of the fast separation is poor due to the upward gas flow of the primary stripping, and the inlet of the cyclone is closer to the outlet of the fast separation, and the higher density catalyst enters the cyclone, increasing the separation efficiency of the cyclone.

U.S. Pat. No. 4, 201510005553, 1 discloses a multi-riser outlet fast separation method, wherein a main riser is centrifugally separated by a relative rotating spray pipe, other riser outlets enter centrifugal separation along the tangent line of a stripper, a settling section is omitted, and stripping gas is easy to carry a large amount of catalyst into a cyclone separator, so that the separation difficulty is improved.

Patents for fast split addition stripping also include CN1055492, CN1082392C, CN1228137C, EP0593827B 1.

Disclosure of Invention

The invention aims to provide catalytic cracking oil separating equipment, a reaction regeneration system and application.

In order to achieve the above purpose, the present invention provides a catalytic cracking oil separating apparatus, which comprises a settling section, a dilute phase stripping section and a dense phase stripping section which are in fluid communication from top to bottom, wherein a first cyclone separator and a catalyst distribution column are arranged in the settling section, the settling section and the dilute phase stripping section are separated by a distribution plate, and the distribution plate is provided with distribution holes for passing a catalyst;

the side wall of the settling section is provided with a reaction oil inlet, the top of the settling section is provided with an oil gas outlet, and the bottom of the dense phase stripping section is provided with a catalyst outlet and a stripping gas inlet;

the first cyclone separator is provided with an oil agent inlet, an oil gas outlet and a catalyst outlet which is arranged downwards, and the oil agent inlet of the first cyclone separator is in fluid communication with the reaction oil agent inlet of the settling section;

the catalyst distribution column extends into the catalyst outlet of the first cyclone separator from bottom to top, and an annular space for dispersing the catalyst to the distribution plate is formed between the catalyst distribution column and the inner wall of the catalyst outlet.

Optionally, the cross-sectional area of the annulus is 10-60% of the cross-sectional area of the catalyst outlet of the first cyclone.

Optionally, the upper end of the catalyst distribution column is formed in a tapered shape.

Optionally, the catalyst distribution column is formed into a spindle-shaped structure, the spindle-shaped structure is vertically arranged along the axial direction, and the top end of the spindle-shaped structure extends into the catalyst outlet of the first cyclone separator.

Optionally, on the vertical plane passing through the axis, the top angle of the fusiform distribution column is 30-70 degrees, and the bottom angle is 20-60 degrees.

Optionally, the ratio of the maximum diameter of the fusiform distribution column to the inner diameter of the dilute phase stripping section is 0.1-0.3, and the ratio of the length of the fusiform distribution column to the inner diameter of the dilute phase stripping section is 0.2-1.0.

Optionally, the middle part of the distribution plate protrudes upwards to form a first conical structure, and the angle of the top cone angle of the first conical structure is 80-160 °.

Optionally, the total open area of the distribution holes accounts for 40-80% of the area of the bottom surface of the distribution plate;

the bottom wall of the distribution plate is provided with a first connecting pipe communicated with the distribution holes.

Optionally, a dust cover for separating the settling section into an upper settling section and a lower settling section is further arranged in the settling section, and an oil-gas hole for oil gas to pass through is formed in the dust cover;

the first cyclone separator penetrates through the dust cover from top to bottom, an oil agent inlet and an oil gas outlet of the first cyclone separator are located in the upper settling section, and a catalyst outlet is located in the lower settling section.

Optionally, the ratio of the minimum vertical spacing of the dust cover from the distributor plate to the inner diameter of the dilute phase stripping section is 0.9-2.6.

Optionally, the middle part of the dust cover protrudes upwards to form a second conical structure, and the angle of the top conical angle of the second conical structure is 90-170 degrees.

Optionally, the open area of the oil and gas holes accounts for 30-75% of the area of the bottom surface of the dust cover;

the diapire of dust cover is provided with the intercommunication the second connecting pipe in oil gas hole.

Optionally, a second cyclone separator located above the first cyclone separator is further arranged in the settling section, the second cyclone separator is provided with an oil agent inlet, an oil gas outlet and a catalyst outlet, and the oil gas outlet of the second cyclone separator is in fluid communication with the oil gas outlet of the settling section.

Optionally, the first cyclone separator and the second cyclone separator each independently comprise a cyclone separator body and a dipleg which are communicated; the oil agent inlet and the oil gas outlet of the first cyclone separator and the second cyclone separator are arranged on the cyclone separator body, and the catalyst outlet is arranged at the bottom end of the dipleg; the dipleg of the second cyclone extends into the dipleg of the first cyclone.

Optionally, the ratio of the height of the dilute phase stripping section to the internal diameter of the dilute phase stripping section is 1.1-3.6.

The invention also provides a catalytic cracking reaction regeneration system, which comprises a riser reactor, a regenerator and the catalytic cracking oil separating equipment provided by the invention, wherein the riser reactor is provided with a raw oil inlet at the lower part, a reaction oil outlet at the top part and a regenerated catalyst inlet at the bottom part, the regenerator is provided with a spent catalyst inlet and a regenerated catalyst outlet, the regenerated catalyst inlet at the bottom part of the riser reactor is communicated with the regenerated catalyst outlet of the regenerator, the reaction oil outlet at the top part of the riser reactor is in fluid communication with the reaction oil inlet of the settling section, and the catalyst outlet of the dense phase stripping section is communicated with the spent catalyst inlet of the regenerator.

The invention also provides a method for separating the catalytic cracking oil agent by adopting the separation equipment provided by the invention, which comprises the following steps:

introducing a reaction oil to be separated into a settling section from a reaction oil inlet of the settling section, separating by a first cyclone separator, allowing the obtained catalyst to enter a dilute phase stripping section and a dense phase stripping section through the settling section and a distribution plate to contact with stripping gas entering from a stripping gas inlet at the bottom of the dense phase stripping section, and performing countercurrent dilute phase stripping and dense phase stripping from top to bottom, wherein the stripped catalyst is led out from a catalyst outlet of the dense phase stripping section, and the obtained stripping oil gas is led out from an oil gas outlet at the top of the settling section.

Optionally, the stripping conditions include: the linear speed of the stripping gas empty tower in the dilute phase stripping zone is 0.05-0.40 m/s, the relative speed of the catalyst and the stripping gas is 0.45-0.85 m/s, and the density of the catalyst is 10-100 kg/m³；

The catalyst density of the dense phase stripping zone is 200-900 kg/m³。

The present invention also provides a catalytic cracking process, comprising:

raw oil is introduced into the lower part of a riser reactor to contact with a regenerated catalyst from the bottom of the riser reactor and carry out catalytic cracking reaction, the obtained reaction oil is led out from the top of the riser reactor and is separated by adopting the separation method provided by the invention, the obtained reaction oil gas is introduced into a subsequent separation unit, the obtained catalyst to be regenerated is introduced into a regenerator to be regenerated, and the regenerated catalyst obtained by regeneration is introduced into the bottom of the riser reactor.

Compared with the prior art, the invention has the following advantages:

1. the space of the stripping section and the settling section of the existing device is utilized to increase the dilute phase stripping section of the countercurrent stripping, so that the process is efficient, simple and feasible;

2. the stripping efficiency of the spent catalyst is greatly improved, the linear speed of stripping gas in a dense phase stripping section can be reduced, the stripping time is shortened, and the load of the stripping gas is reduced;

3. the oil gas retention time of the dilute phase stripping section and the dense phase stripping section is reduced, the secondary reaction is reduced, and the generation of coke and dry gas is reduced.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 includes a schematic structural diagram of an embodiment of a catalytic cracking oil separation device of the present invention, and also includes a schematic structural diagram of an embodiment of a catalytic cracking reaction regeneration system of the present invention.

Figure 2 is a schematic structural view of one embodiment of the lower settling section of the present invention.

FIG. 3 is a schematic structural view of one embodiment of the dust shield, cyclone diplegs and catalyst distribution columns of the present invention.

FIG. 4 is a schematic diagram of the structure of one embodiment of the distribution plate and the catalyst distribution columns of the present invention.

FIG. 5 is a schematic structural diagram (top view) of an embodiment of a distribution plate according to the present invention.

FIG. 6 is a schematic structural view (top view) of one embodiment of a dust boot of the present invention.

Description of the reference numerals

1 upper settling section and 2 lower settling section

4 annular gap 5 oil gas hole 6 distribution hole

7 second connecting pipe 8 first connecting pipe

10 pre-lift steam 11 regeneration inclined tube 12 regeneration slide valve

13 pre-lifting section 14 raw oil and atomized steam 15 raw material and atomized water nozzle

16 oil agent contact section 17 riser reactor 18 first cyclone separator

19 dust cover 20 first cyclone dipleg 21 catalyst distribution post

22 distributor plate 23 dilute phase stripping section 24 dense phase stripping section

25-spent inclined tube 26-spent slide valve

28 settling section 29 second cyclone separator 30 plenum chamber

31 stripping gas 41 round hole 42 pore channel

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

In the present invention, unless otherwise specified, the terms of orientation such as "upper, lower, bottom, top" are generally used to refer to "upper, lower, bottom, top" of the device in actual use, and the specific orientation may refer to the direction of the drawing in fig. 1. In the present invention, the inner diameter is by default a description object having a circular cross section.

As shown in fig. 1-6, the present invention provides a catalytic cracking oil separating apparatus, which comprises a settling section 28, a dilute phase stripping section 23 and a dense phase stripping section 24 which are in fluid communication from top to bottom, wherein a first cyclone separator 18 and a catalyst distribution column 21 are arranged in the settling section 28, the settling section 28 and the dilute phase stripping section 23 are separated by a distribution plate 22, and distribution holes 6 for passing a catalyst are arranged on the distribution plate 22;

the side wall of the settling section 28 is provided with a reaction oil agent inlet, the top of the settling section is provided with an oil gas outlet, and the bottom of the dense phase stripping section 24 is provided with a catalyst outlet and a stripping gas inlet;

the first cyclone separator 18 is provided with an oil agent inlet, an oil gas outlet and a catalyst outlet which is arranged downwards, and the oil agent inlet of the first cyclone separator 18 is in fluid communication with the reaction oil agent inlet of the settling section 28;

the catalyst distribution column 21 extends into the catalyst outlet of the first cyclone separator 18 from bottom to top, and an annular space 4 for dispersing the catalyst to the distribution plate 22 is formed between the catalyst distribution column and the inner wall of the catalyst outlet.