CN211999578U

CN211999578U - Novel catalytic cracking device

Info

Publication number: CN211999578U
Application number: CN202020139873.1U
Authority: CN
Inventors: 毛文茂; 任培杰
Original assignee: SHANDONG CHANGYI PETROCHEMICAL CO Ltd
Current assignee: SHANDONG CHANGYI PETROCHEMICAL CO Ltd
Priority date: 2020-01-21
Filing date: 2020-01-21
Publication date: 2020-11-24
Anticipated expiration: 2030-01-21

Abstract

The utility model discloses a novel catalytic cracking device, including a jar body, jar internal according to the preface be provided with settler, strip mechanism and regenerator, through the reactor intercommunication between the top of settler and the bottom of regenerator, the upper portion intercommunication of reactor has the terminator pipeline, and the terminator pipeline includes the main line, and the end of producing oil of main line communicates with the upper portion of the riser of reactor, and the oil inlet end and the fractionating tower intercommunication of main line are equipped with flowmeter, gate valve and terminator pump on the main line in proper order. The utility model discloses make the remill than reducing, strengthened raw materials initial reaction condition simultaneously, optimized the product and distributed, reduce the green burnt, reduce flue gas NOx and waste water ammonia nitrogen and discharge.

Description

Novel catalytic cracking device

Technical Field

The utility model relates to a novel catalytic cracking device.

Background

A1.4 mt/a heavy oil catalytic cracking device of the company is designed by a design institute according to a gasoline production scheme, and is built in 2018 in 2 months and successfully driven once. With the increasing proportion of the residual oil, the recycle ratio is also increasing, and the properties of the raw material are increasingly poor. Mainly characterized by high carbon residue value, large specific gravity, large viscosity and high heavy metal content. During catalytic cracking, a large amount of basic nitrogen compounds are adsorbed by the catalyst and transferred to the coke, which is oxidized when regenerated in a regenerator to form NOx. When the feeding property is heavier or the recycling ratio is increased, the numerical values of the flue gas NOx and the waste water ammonia nitrogen are obviously increased, and the environment-friendly discharge pressure is increased. The specific gravity is high, the reaction difficulty is increased, and the product is difficult to achieve reasonability and quality optimization. High heavy metal content, and easy to cause catalyst pollution. Resulting in a decrease in catalyst capacity and a decrease in plant throughput.

Disclosure of Invention

The utility model aims to solve the technical problem that a novel catalytic cracking device is provided, realize the purpose that the remill ratio reduces, strengthened raw materials initial reaction condition simultaneously, optimized the product distribution, reduced the green coke, reduce flue gas NOx and waste water ammonia nitrogen and discharge.

For solving foretell technical problem, the utility model discloses a jar body, internal settler, strip mechanism and the regenerator of being provided with according to the preface of jar, the top of settler with through the reactor intercommunication between the bottom of regenerator, its structural feature is the upper portion intercommunication of reactor has the terminator pipeline, the terminator pipeline includes the main line, the end of giving vent to anger of main line with the upper portion intercommunication of the riser of reactor, the oil feed end and the fractionating tower intercommunication of main line, be equipped with flowmeter, gate valve and terminator pump on the main line in proper order.

Be equipped with the branch road between the oil inlet end of gate valve and the oil outlet end, be equipped with the control valve on the branch road, be equipped with the gate valve on the branch road at control valve both ends.

The settler comprises a coarse cyclone separator and a single-stage cyclone separator, wherein each coarse cyclone separator is correspondingly communicated with two single-stage cyclone separators, the oil inlet end of each coarse cyclone separator is communicated with the gas outlet end of the reactor, the gas outlet end of each coarse cyclone separator is communicated with the gas inlet end of the single-stage cyclone separator through a gas riser, and catalyst flows delivered by the legs of the coarse cyclone separators and the single-stage cyclone separators are fluidized by a fluidized ring.

The stripping mechanism comprises a stripping section and a stripping steam ring, the stripping steam ring is arranged at the lower part of the stripping section, the spent catalyst subjected to fluidization treatment is sent to the stripping section to replace oil gas, the bottom of the stripping steam ring is communicated with the regenerator through a spent riser, and a plurality of scattered caps are uniformly arranged in the stripping section.

The regenerator includes waiting to give birth to sleeve and main air distributing plate, it has the stand of waiting to give birth to that is used for connecting the strip mechanism to wait to give birth to telescopic top cartridge, it is equipped with the stopper valve of waiting to give birth to be equipped with on the discharge end of stand of waiting to give birth to, it wears out to give birth to the sleeve the bottom of the jar body sets up, the main air distributing plate is located the bottom of the jar body, just the main air distributing plate encircles and establishes waiting to give birth to telescopic outside setting, it is equipped with a plurality of catalyst distributors of waiting to give birth to fit with a contraceptive ring to wait to give birth to telescopic lateral wall, the bottom intercommunication of main air distributing plate has the main tuber pipe of burning, be equipped with the auxiliary combustion chamber on the main tuber pipe of burning, the lower part intercommunication of waiting to give birth to.

The tank body is internally provided with a plurality of cyclone separators corresponding to the sleeves to be grown.

The reactor comprises a lifting pipe, the lower part of the lifting pipe is communicated with the lower part of the to-be-regenerated sleeve through a regeneration inclined pipe, and a regeneration single-acting slide valve and a CRC-regenerated catalyst cooler are arranged on the regeneration inclined pipe.

After the structure is adopted, raw oil is treated and then mixed with recycle oil and then enters a reactor, the raw oil is contacted with a high-temperature catalyst to complete the heating, vaporization and reaction of the raw material, oil gas and the catalyst after reaction enter a settler, the catalyst and the oil gas are quickly separated, a spent catalyst is in countercurrent contact with stripping steam in a stripping section to replace oil gas carried by the catalyst, the spent catalyst after stripping enters a regenerator to be regenerated, then the regenerated catalyst enters the bottom of the reactor to complete circulation, in the process, a terminator pipeline can inject gasoline in one step into the reactor as a terminator, the gasoline in the other step is a mixture of the head of the recycle oil and the tail of light diesel oil, and is non-product fraction; it can inhibit the secondary cracking of light diesel oil or gasoline produced initially, convert itself into product and increase the yield of target product. Since the recycle of the oil inevitably leads to the reduction of the distillate quantity of the recycle oil, the purpose of reducing the recycle ratio is finally realized. Meanwhile, the initial reaction conditions of the raw materials are strengthened, the product distribution is optimized, the coke formation is reduced, and the emission of flue gas NOx and wastewater ammonia nitrogen is reduced.

Drawings

The invention will be further explained with reference to the following figures and examples:

fig. 1 is a schematic structural diagram of the present invention;

in the figure: 1-tank body, 2-settler, 3-stripping mechanism, 4-regenerator, 5-reactor, 6-riser, 7-regeneration inclined tube, 8-regeneration single-acting slide valve, 9-CRC-regenerated catalyst cooler, 10-terminator pipeline, 11-main pipeline, 12-flowmeter, 13-gate valve, 14-terminator pump, 15-branch, 16-control valve, 17-coarse cyclone quick separator, 18-single-stage cyclone separator, 19-fluidization ring, 20-stripping section, 21-spent riser, 22-spent plug valve, 23-spent sleeve, 24-main air distribution plate, 25-cyclone separator, 26-coke-burning main air pipe, 27-auxiliary combustion chamber, 28-fluidization main air pipe, 29-main fan, 30-steam pipeline, 31-riser, 32-terminator nozzle, 33-stripping steam ring, 34-dispersing cap and 35-booster pump.

Detailed Description

Referring to fig. 1, the novel catalytic cracking device comprises a tank body 1, a settler 2, a stripping mechanism 3 and a regenerator 4 are sequentially arranged in the tank body 1 from top to bottom, the top of the settler 2 is communicated with the bottom of the regenerator 4 through a reactor 5, the reactor 5 comprises a riser 6, the lower part of the riser 6 is communicated with the lower part of the regenerator 4 through a regeneration inclined tube 7, a regeneration single-acting slide valve 8 and a CRC-regenerated catalyst cooler 9 are arranged on the regeneration inclined tube 7, the upper part of the riser 6 is communicated with a steam pipeline 30 and a terminator pipeline 10, the steam pipeline 30 converts liquid gasoline in the riser 6 into gaseous gasoline, the terminator pipeline 10 comprises a main pipeline 11, the gas outlet end of the main pipeline 11 is communicated with the upper part of the riser 6 of the reactor 5, a terminator nozzle 32 is arranged on the gas outlet end of the main pipeline 11, the oil inlet end of the main pipeline 11 is communicated with the oil outlet end of a fractionating tower, the fractionating tower is not shown in the figure, a flowmeter 12, a gate valve 13 and a terminator pump 14 are sequentially arranged on a main pipeline 11, a steam pipeline 30 is arranged on the main pipeline 11, steam in the steam pipeline 30 enables gasoline in the main pipeline 11 to be converted from liquid state to gaseous state, a branch 15 is arranged between a feeding end and a discharging end of the gate valve 13, and the gate valve 13, a control valve 16 and the gate valve 13 are sequentially arranged on the branch 15; feeding a gaseous medium gasoline, which is a mixture of the head of the recycle oil and the tail of the light diesel oil, into the reactor 5 through a main pipeline 11 by a terminator pump 14, wherein the gaseous medium gasoline is a non-product fraction; the device can inhibit secondary cracking of light diesel oil or gasoline produced initially from raw materials, can convert the light diesel oil or gasoline into products, and increases target products and yield, the flow meter 12 can obtain the flow of the gasoline entering the reactor 5, the gate valve 13 can control whether the gasoline is fed into the reactor 5, the terminator pump 14 can provide power for the flow of the gasoline, and the branch 15 is used for flexibly adjusting the injection amount of the terminator according to reaction effects.

The settler 2 comprises coarse cyclone separators 17 and single-stage cyclone separators 18, each coarse cyclone separator 17 is correspondingly communicated with two single-stage cyclone separators 18, the oil inlet end of each coarse cyclone separator 17 is communicated with the gas outlet end of the reactor 5, the gas outlet end of each coarse cyclone separator 17 is communicated with the gas inlet end of each single-stage cyclone separator 18 through a gas riser 31, and catalysts sent out from the diplegs of the coarse cyclone separators 17 and the single-stage cyclone separators 18 are fluidized by a fluidizing ring 19. The coarse cyclone separators 17 are provided with two groups, the single-stage cyclone separators 18 are provided with four groups, the two groups of coarse cyclone separators 17 rapidly separate the catalyst and the oil gas to stop the secondary reaction mainly based on the thermal cracking reaction, the dry gas yield is reduced, and the catalyst to be generated enters the stripping section 20 arranged at the lower part through the coarse cyclone legs. The riser 31 of two groups of coarse cyclone separator 17 and four groups of single-stage cyclone separator adopt a one-to-two direct connection mode, the reaction oil gas and the entrained catalyst fine powder which are discharged from the coarse cyclone separator 17 are directly led into the single-stage cyclone separator 18, the reaction oil gas after the catalyst fine powder is further separated by the single-stage cyclone separator 18 of the settler 2 enters the lower part of the fractionating tower through a large oil gas pipeline at the top of the settler 2, and the catalyst separated by the coarse cyclone separator 17 and the single-stage cyclone separator 18 flows through a fluidization ring 19 arranged at the lower part for fluidization, thereby fundamentally avoiding the coking phenomenon of the settler 2 caused by the overflow of the oil gas.

The stripping mechanism 3 comprises a stripping section 20 and a stripping steam ring 33, the stripping steam ring 33 is arranged at the lower part of the stripping section 20, the fluidized spent catalyst is sent to the stripping section 20 for oil gas replacement, the bottom of the stripping steam ring 33 is communicated with the regenerator 4 through a spent riser 21, and a plurality of scattered caps 34 are uniformly arranged in the stripping section 20. The stripped spent catalyst enters the regenerator 4 along a spent riser 21.

The regenerator 4 comprises a spent sleeve 23 and a main air distribution plate 24, a spent vertical pipe 21 used for communicating a stripping section 20 is inserted at the top of the spent sleeve 23, the upper part of the spent vertical pipe 21 is communicated with the lower part of the stripping mechanism 3, the discharge end of the spent vertical pipe 21 is positioned in the middle of the spent sleeve 23, a spent plug valve 22 is arranged at the discharge end of the spent vertical pipe 21, a valve seat is arranged at the discharge end of the spent vertical pipe 21, the spent plug valve 22 is arranged on the valve seat, the upper end of the spent plug valve 22 is conical, the maximum diameter of the upper end of the spent plug valve 22 is larger than the inner diameter of the discharge end of the spent vertical pipe 21, the spent plug valve 22 is arranged to avoid the backflow of the catalyst, the spent catalyst is in countercurrent contact with stripping steam in the stripping section 20 to replace oil gas carried by the catalyst, the spent sleeve 23 penetrates out of the bottom of the tank body 1, the main air distribution plate 24 is arranged at the bottom of the tank body 1, a plurality of spent catalyst distributors, the bottom of the main air distribution plate 24 is communicated with a main coke burning air pipe 26, an auxiliary combustion chamber 27 is arranged on the main coke burning air pipe 26, the lower part of the sleeve to be generated 23 is communicated with a main fluidizing air pipe 28, the main coke burning air pipe 26 and the main fluidizing air pipe 28 are both communicated with a main fan 29, a plurality of cyclone separators 25 corresponding to the sleeve to be generated 23 are arranged in the tank body 1, and the cyclone separators 25 are arranged above the sleeve to be generated 23. The stripped spent catalyst flows through a spent plug valve 22 along a spent riser 21 and enters a spent sleeve 23 of the regenerator 4, enters a spent catalyst distributor arranged at the upper part of the regenerator 4 under the fluidization action of sleeve fluidization wind, and is uniformly distributed on the upper part of the regenerator 4 through the spent catalyst distributor; the spent catalyst is subjected to countercurrent conventional regeneration at a regeneration temperature of about DEG C under the condition of oxygen deficiency; the regenerated catalyst is sent to a cyclone separator 25 for separation by the air flow blown by a main air distribution plate 24, the catalyst separated by the cyclone separator 25 flows to the bottom of the tank body 1 through a dipleg of the cyclone separator 25, the regenerated catalyst enters the bottom of the riser pipe 6 through a regeneration slide valve after being cooled by a CRC-regenerated catalyst cooler 9, dry gas is used as a lifting medium to finish the acceleration and rectification processes of the catalyst, and then the catalyst is contacted with an atomized raw material to finish circulation. The main air required by the burning of the regenerator 4 is provided by a main air blower 29, wherein a part of the main air is led out from the front of a main air main pipe damping one-way valve and is pressurized by a booster pump 35 to be used as the air for fluidizing the to-be-generated sleeve 23; the other part of the main air enters the lower part of the regenerator 4 through the auxiliary combustion chamber 27, is uniformly distributed through the main air distribution plate 24 and then enters the regenerator 4 for charring, and when the heat generated after the charring of the regenerator 4 is enough to heat the main air to the reaction temperature, the auxiliary combustion chamber 27 stops heating the main air; the flue gas generated by the coke burning of the regenerator 4 is firstly separated from the catalyst carried in the flue gas by the cyclone separator 25.

The structures and the working principles of the settler 2 (model: R1101), the regenerator 4 (model: R1202), the reactor 5 (model: R1101A), the cyclone separator 25 (model: CY 1104), the stripping section 20 and the CRC-regenerated catalyst cooler 9 are well known and well known to those skilled in the art, and are not described herein again.

When the utility model is used, when raw oil is mixed with recycle oil after being processed and enters the reactor 5, the terminator pipeline 10 can inject a middle gasoline into the reactor 5 as a terminator, and the middle gasoline is a mixture of the head of the recycle oil and the tail of light diesel oil and is non-product fraction; the method can inhibit secondary cracking of light diesel oil or gasoline produced initially from raw materials, and can convert the light diesel oil or gasoline into products, thereby increasing the target products and yield; the recycle oil distillation amount is reduced due to the recycle of the oil, and the purpose of reducing the recycle ratio is finally realized; meanwhile, the initial reaction condition of the raw materials is strengthened, the product distribution is optimized, the coking is reduced, the emission of flue gas NOx and waste water ammonia nitrogen is reduced, the mixed raw oil is contacted with a high-temperature catalyst to complete the heating, vaporization and reaction of the raw materials, the reacted oil gas and the catalyst enter a settler 2, the catalyst and the oil gas are rapidly separated through a coarse cyclone separator 17 and a single-stage cyclone separator 18, the spent catalyst is in countercurrent contact with stripping steam in a stripping section 20 to replace the oil gas carried by the catalyst, the stripped spent catalyst enters a regenerator 4 to be regenerated, and the regenerated catalyst enters the bottom of a reactor 5 to complete the circulation.

Claims

1. The utility model provides a novel catalytic cracking device, includes a jar body (1), be provided with settler (2), stripping mechanism (3) and regenerator (4) in proper order in jar body (1), the top of settler (2) with communicate through reactor (5) between the bottom of regenerator (4), its characterized in that the upper portion intercommunication of reactor (5) has terminator pipeline (10), terminator pipeline (10) include main line (11), the end of giving vent to anger of main line (11) with the upper portion intercommunication of riser (6) of reactor (5), the oil feed end and the fractionating tower intercommunication of main line (11), be equipped with flowmeter (12), gate valve (13) and terminator pump (14) on main line (11) in proper order.

2. The catalytic cracking unit according to claim 1, wherein a branch (15) is provided between the oil inlet end and the oil outlet end of the gate valve (13), a control valve (16) is provided on the branch (15), and the gate valve (13) is provided on the branch (15) at both ends of the control valve (16).

3. The novel catalytic cracking unit according to claim 1, wherein the settler (2) comprises a coarse cyclone separator (17) and a single-stage cyclone separator (18), each coarse cyclone separator (17) is correspondingly communicated with two single-stage cyclone separators (18), the feeding end of the coarse cyclone separator (17) is communicated with the gas outlet end of the reactor (5), the gas outlet end of the coarse cyclone separator (17) is communicated with the gas inlet end of the single-stage cyclone separator (18) through a gas riser (31), and the catalyst sent out from the dipleg of the coarse cyclone separator (17) and the single-stage cyclone separator (18) is fluidized by a fluidizing ring (19).

4. The novel catalytic cracking unit according to claim 1, wherein the stripping unit (3) comprises a stripping section (20) and a stripping steam ring (33), the stripping steam ring (33) is disposed at the lower part of the stripping section (20), the fluidized spent catalyst is sent to the stripping section (20) for replacing oil gas, the bottom of the stripping steam ring (33) is communicated with the regenerator (4) through a spent riser (21), and a plurality of scattered caps (34) are uniformly disposed in the stripping section (20).

5. The novel catalytic cracking device according to claim 4, wherein the regenerator (4) comprises a spent sleeve (23) and a main air distribution plate (24), a spent riser (21) for communicating the stripping mechanism (3) is inserted into the top of the spent sleeve (23), a spent plug valve (22) is arranged at the discharge end of the spent riser (21), the spent sleeve (23) penetrates out of the bottom of the tank body (1), the main air distribution plate (24) is arranged at the bottom of the tank body (1), the main air distribution plate (24) is annularly arranged outside the spent sleeve (23), a plurality of spent catalyst distributors are annularly arranged on the side wall of the spent sleeve (23), the bottom of the main air distribution plate (24) is communicated with a main coke-burning air pipe (26), and an auxiliary combustion chamber (27) is arranged on the main coke-burning air pipe (26), the lower part of the to-be-generated sleeve (23) is communicated with a main fluidizing air pipe (28), and the main scorching air pipe (26) and the main fluidizing air pipe (28) are both communicated with a main fan (29).

6. A new catalytic cracking unit according to claim 5, characterized in that a plurality of cyclones (25) corresponding to the spent sleeves (23) are provided in the vessel (1).

7. The new catalytic cracking unit according to claim 1, characterized in that the reactor (5) comprises a riser (6), the lower part of the riser (6) is connected to the lower part of the regenerator (4) through a regeneration inclined tube (7), and a regeneration single-acting slide valve (8) and a CRC-regenerated catalyst cooler (9) are arranged on the regeneration inclined tube (7).