Apparatus and method for adjusting deep catalytic cracking reverse-reheat balance

Abstract

The application provides a device and method for adjusting deep catalytic cracking reaction-reheat balance, and relates to the technical field of deep catalytic cracking. The device for adjusting deep catalytic cracking reaction-reheat balance comprises a deep catalytic cracking reaction system, a catalyst regeneration system and a concentrated oil slurry pipeline. The catalyst regeneration system comprises a spent catalyst inclined pipe, a coke burning tank, a regenerator and a regenerated catalyst inclined pipe which are sequentially connected. The end of the spent catalyst inclined pipe, which is far away from the coke burning tank, is connected with the deep catalytic cracking reaction system, and a spent catalyst slide valve is arranged on the spent catalyst inclined pipe. The outlet of the concentrated oil slurry pipeline is connected with the spent catalyst inclined pipe which is located between the spent catalyst slide valve and the coke burning tank, and the end of the regenerated catalyst inclined pipe, which is far away from the regenerator, is connected with the deep catalytic cracking reaction system. The application provides heat for the deep catalytic cracking reaction system, and reuses the oil slurry generated by the deep catalytic cracking reaction system. The application not only solves the heat balance problem of the deep catalytic cracking reaction, but also increases the production of steam, and achieves high economic benefits.

Description

Technical Field

[0001] This invention relates to the field of deep catalytic cracking technology, and specifically to an apparatus and method for regulating the reverse reheat balance in deep catalytic cracking. Background Technology

[0002] Deep catalytic cracking units consume more steam than conventional catalytic cracking. Conventional catalytic cracking uses approximately 10% steam for back-recycle (relative to fresh feedstock). For a 3 million tons / year catalytic cracking plant, this translates to approximately 37 t / h of back-recycle steam. However, deep catalytic cracking processes, which primarily produce low-carbon olefins such as propylene, require lower hydrocarbon partial pressures. Therefore, maintaining lower reaction pressures necessitates the injection of a large amount of steam to reduce hydrocarbon partial pressures. Typically, deep catalytic cracking processes use approximately 25% steam. In a 3 million tons / year deep catalytic cracking unit, the back-recycle portion consumes approximately 93 t / h of steam, a significant increase compared to conventional catalytic cracking. Therefore, deep catalytic cracking units differ from conventional catalytic cracking units, requiring higher temperatures and lower pressures.

[0003] As mentioned above, deep catalytic cracking processes require significant heat of reaction. Deep catalytic cracking units primarily produce low-carbon olefins such as propylene, necessitating further cracking of gasoline into these olefins. This requires more heat of reaction than conventional catalytic cracking, which has a heat of reaction of approximately 200 kJ / kg feedstock. In contrast, deep catalytic cracking requires approximately 600 kJ / kg feedstock, leading to insufficient heat output in the regenerator and reduced steam generation. For example, a company's 3.4 million tons / year catalytic cracking unit has an external heat exchanger saturated steam generation of approximately 40 t / h, while a 3 million tons / year deep catalytic cracking unit has an external steam generation of approximately 5 t / h, representing a significant decrease in steam generation.

[0004] In addition, in the existing technology, the concentrated slurry produced by the oil slurry from the deep catalytic cracking unit after passing through the desolidification facility is mostly treated as waste or fed into the coking unit, resulting in low utilization. Summary of the Invention

[0005] Based on the above analysis, the present invention aims to provide an apparatus and method for adjusting the reverse reheat balance of deep catalytic cracking, in order to solve at least one of the following problems existing in the prior art: adjusting the reverse reheat balance of deep catalytic cracking, increasing steam production, and reusing concentrated oil slurry.

[0006] The objective of this invention is mainly achieved through the following technical solutions.

[0007] In a first aspect, the present invention provides an apparatus for adjusting the reverse reheat balance of deep catalytic cracking, comprising a deep catalytic cracking reaction system, a catalyst regeneration system, and a concentrated oil slurry pipeline connected in sequence. The catalyst regeneration system comprises a pre-regeneration inclined tube, a coke burner, a regenerator, and a regeneration inclined tube connected in sequence. The end of the pre-regeneration inclined tube away from the coke burner is connected to the deep catalytic cracking reaction system, and a pre-regeneration slide valve is provided on the pre-regeneration inclined tube. The outlet of the concentrated oil slurry pipeline is connected to the pre-regeneration inclined tube located between the pre-regeneration slide valve and the coke burner. The ratio of the length l1 of the pre-regeneration inclined tube between the connection point and the pre-regeneration slide valve to the length l0 of the pre-regeneration inclined tube between the pre-regeneration slide valve and the coke burner is l1 / l0 = 1 / 2 to 2 / 3. The end of the regeneration inclined tube away from the regenerator is connected to the deep catalytic cracking reaction system.

[0008] Preferably, the angle α between the outlet of the concentrated oil slurry pipeline and the inclined tube to be generated is 45°-55°.

[0009] Preferably, a waiting-to-be-distributed device is provided inside the coking tank, and the waiting-to-be-distributed inclined tube is connected to the waiting-to-be-distributed device.

[0010] Preferably, a hot air injection port is provided at the bottom of the coking tank.

[0011] Preferably, the outlet of the concentrated oil slurry pipeline is connected to the pre-generation inclined tube via a nozzle.

[0012] Preferably, the nozzle is a throat-type nozzle.

[0013] Preferably, the apparatus further includes a fractionation tower and an oil slurry desolidification device. The fractionation tower includes a raw material inlet and an oil slurry outlet, and the oil slurry desolidification device includes an oil slurry inlet and a concentrated oil slurry outlet. The raw material inlet of the fractionation tower is connected to the product outlet of the deep catalytic cracking reaction system. The fractionation tower is used to fractionate the reaction products to obtain oil slurry and discharge the oil slurry from the oil slurry outlet. The oil slurry outlet of the fractionation tower is connected to the oil slurry inlet of the oil slurry desolidification device. The oil slurry desolidification device is used to desolidify the oil slurry to obtain the concentrated oil slurry and discharge the concentrated oil slurry from the concentrated oil slurry outlet. The concentrated oil slurry outlet is connected to the inlet of the concentrated oil slurry pipeline.

[0014] In a second aspect, the present invention provides a method for adjusting the reverse reheat balance of deep catalytic cracking, performed in the apparatus, comprising the following steps:

[0015] Step 1: Inject the concentrated oil slurry into the waiting inclined tube through the concentrated oil slurry pipeline and mix it with the waiting catalyst from the deep catalytic cracking reaction system;

[0016] Step 2: The mixture discharged from the inclined tube is burned in the coking vessel;

[0017] Step 3: After combustion treatment, the catalyst enters the regenerator for regeneration and then returns to the deep catalytic cracking reaction system through the regeneration inclined tube.

[0018] Preferably, the density of the concentrated oil slurry in step 1 is 950-1050 kg / m³. 3 .

[0019] Preferably, the concentrated oil slurry in step 1 is derived from the product obtained by fractionating the deep catalytic cracking reaction product and then performing a desolidification step.

[0020] Preferably, the mass flow rate of the concentrated oil slurry is 20%-100% of the mass flow rate of the oil slurry.

[0021] Preferably, the temperature of the concentrated oil slurry injected into the inclined tube in step 1 is 180-250℃.

[0022] Preferably, the pressure of the concentrated oil slurry injected into the inclined tube to be formed in step 1 is 0.5-2 MPaG.

[0023] Preferably, the mixture described in step 2 is burned in contact with a hot air stream inside a coking tank.

[0024] Preferably, the temperature of the hot air stream is 150–200°C.

[0025] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

[0026] A) According to the apparatus and method provided by the present invention, the concentrated oil slurry is injected into the catalyst regeneration line, and after being fully mixed with the catalyst, it enters the catalyst regeneration system for combustion and heat release. This can further provide heat for the deep catalytic cracking reaction system and realize the reuse of the oil slurry generated by the deep catalytic cracking reaction system. This solves the heat balance problem of the deep catalytic cracking reaction, increases steam production, and achieves high economic benefits.

[0027] B) According to the apparatus and method provided by the present invention, the injection of concentrated oil slurry through a new process not only solves the thermal balance problem of deep catalytic cracking reaction, but also avoids the catalyst thermal collapse caused by the traditional method of increasing coking and can eliminate its impact on product distribution. This ensures the stable operation of the apparatus for a long period of time and increases steam production. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of the device for adjusting the reverse reheat balance of deep catalytic cracking provided by the present invention.

[0029] Among them, 100, deep catalytic cracking reaction system; 200, catalyst regeneration system; 1, reaction product stream; 2, bed reactor; 3, second riser; 4, first riser; 5, first steam stream; 6, raw material stream; 7, second steam stream; 8, C4 reprocessing stream; 9, light gasoline reprocessing stream; 10, concentrated oil slurry pipeline; 11, hot air stream; 12, coke burner; 13, regenerator; 14, flue gas stream; 15, waiting slide valve; 16, waiting inclined tube; 17, waiting distributor; 18, regeneration inclined tube; 19, hot air inlet; 20, nozzle; 21, external heat exchanger. Detailed Implementation

[0030] Preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which form part of the present invention and, together with the embodiments of the present invention, serve to illustrate the principles of the present invention.

[0031] In this invention, the term "deep catalytic cracking regeneration thermal equilibrium" refers to "deep catalytic cracking reaction-regeneration system thermal equilibrium".

[0032] In a first aspect, the present invention provides an apparatus for adjusting the reverse reheat balance of deep catalytic cracking, comprising a deep catalytic cracking reaction system, a catalyst regeneration system, and a concentrated oil slurry pipeline connected in sequence. The catalyst regeneration system comprises a pre-regeneration inclined tube, a coke burner, a regenerator, and a regeneration inclined tube connected in sequence. The end of the pre-regeneration inclined tube away from the coke burner is connected to the deep catalytic cracking reaction system, and a pre-regeneration slide valve is provided on the pre-regeneration inclined tube. The outlet of the concentrated oil slurry pipeline is connected to the pre-regeneration inclined tube located between the pre-regeneration slide valve and the coke burner. The ratio of the length l1 of the pre-regeneration inclined tube between the connection point and the pre-regeneration slide valve to the length l0 of the pre-regeneration inclined tube between the pre-regeneration slide valve and the coke burner is l1 / l0 = 1 / 2 to 2 / 3. The end of the regeneration inclined tube away from the regenerator is connected to the deep catalytic cracking reaction system.

[0033] Figure 1 This invention illustrates one embodiment of the apparatus for regulating the reverse reheat balance of deep catalytic cracking.

[0034] Reference Figure 1 The device for adjusting the reheat balance of deep catalytic cracking provided by the present invention includes a deep catalytic cracking reaction system 100, a catalyst regeneration system 200, and a concentrated oil slurry pipeline 10.

[0035] The deep catalytic cracking reaction system 100 is used to carry out deep catalytic cracking reaction, the catalyst regeneration system 200 is used to regenerate the catalyst, and the concentrated oil slurry pipeline 10 is used to transport concentrated oil slurry.

[0036] The catalyst regeneration system 200 includes a pre-regeneration inclined tube 16, a regeneration inclined tube 18, a coke burner 12, and a regenerator 13. The outlet of the coke burner 12 is connected to the inlet of the regenerator 13. One end of the pre-regeneration inclined tube 16 is connected to the coke burner 12, and the other end of the pre-regeneration inclined tube 16 is connected to the deep catalytic cracking reaction system 100. A pre-regeneration slide valve 15 is provided on the pre-regeneration inclined tube 16.

[0037] The outlet of the concentrated oil slurry pipeline 10 is connected to the waiting inclined pipe 16 at 1 / 2 to 2 / 3 of the length of the inclined pipe after the waiting slide valve 15. One end of the regeneration inclined pipe 18 is connected to the regenerator 13, and the other end is connected to the deep catalytic cracking reaction system 100. Figure 1 In this context, l0 represents the length of the inclined tube between the waiting-to-be-born slide valve 15 and the coking tank 12, and l1 represents the length of the inclined tube between the waiting-to-be-born slide valve 15 and the connection point between the concentrated slurry pipeline 10 and the inclined tube 16. The ratio of l1 to l0 satisfies l1 / l0 = 1 / 2 to 2 / 3. For example, the values ​​between 1 / 2 and 2 / 3 can be 0.52, 0.54, 0.56, 0.58, 0.6, 0.62, 0.64, 0.66, etc.

[0038] In this invention, the pre-regenerated inclined tube 16 is used to transport the catalyst to be regenerated from the deep catalytic cracking reaction system 100 to the catalyst regeneration system 200. The pre-regenerated slide valve 15 is generally located at 3 / 5 to 2 / 3 of the total length of the pre-regenerated inclined tube 16 (starting from the connection point between the pre-regenerated inclined tube 16 and the deep catalytic cracking reaction system 100), and is a control valve for the pre-regenerated catalyst. In this invention, the injection of concentrated slurry does not affect the catalyst flow rate in the pre-regenerated catalyst line. By ensuring a constant pressure differential at the pre-regenerated slide valve, the catalyst flow rate can be ensured to be stable.

[0039] In this invention, a mixture including concentrated oil slurry and a catalyst to be recycled is discharged from the incised tube 16 and burned in the coking tank 12. The burned catalyst enters the regenerator 13 for regeneration. The regenerated catalyst, along with the heat released by combustion, is transported from the regeneration incised tube 18 to the deep catalytic cracking reaction system 100 to provide heat for the reaction system. The regenerated catalyst serves as the heat carrier for the heat released by combustion.

[0040] As a specific embodiment of the present invention, the catalyst regeneration system 200 may further include an external heat exchanger 21, which is disposed outside the coke burner 12 and communicates with the regenerator 13 and the coke burner 12, for circulating the high-temperature regenerated catalyst and increasing steam production.

[0041] Therefore, based on adjusting the reheat balance of deep catalytic cracking, the device provided by this invention can also increase steam production, and the increased steam production can be further utilized to improve economic efficiency.

[0042] Furthermore, regarding the connection point between the outlet of the concentrated slurry pipeline 10 and the pre-generation inclined pipe 16, the injection location of the concentrated slurry must consider factors such as the stable flow rate of the pre-generation catalyst after exiting the pre-generation slide valve, the on-site piping, and the thorough mixing of the concentrated slurry and the pre-generation catalyst. If the concentrated slurry is injected before the halfway point of the line after the pre-generation slide valve, the flow rate of the pre-generation catalyst will be unstable, resulting in poor mixing between the concentrated slurry and the pre-generation catalyst, which will worsen the effect of regulating the deep catalytic cracking back-reheat balance and reduce the steam production. If the concentrated slurry is injected after the two-thirds point of the line after the pre-generation slide valve, the mixture between the concentrated slurry and the pre-generation catalyst will be insufficient, leading to a worse effect of regulating the deep catalytic cracking back-reheat balance and reducing the steam production. In addition, the concentrated slurry cannot be injected before the pre-generation slide valve 15 because the concentrated slurry will wear down the pre-generation slide valve, affecting its normal operation.

[0043] In one specific embodiment of the present invention, the angle α between the outlet of the concentrated oil slurry pipeline 10 and the pre-calcined inclined pipe 16 is 45°-55°, such as 46°, 47°, 48°, 49°, 50°, 51°, 52°, 53°, 54°, etc. If the angle is too small (less than 45°) or too large (greater than 55°), it will lead to insufficient contact between the concentrated oil slurry and the pre-calcined catalyst, resulting in local combustion in the coking tank and the formation of a high-temperature zone above 800°C, causing thermal deactivation of the catalyst and increasing catalyst loss.

[0044] As a specific embodiment of the present invention, a waiting distributor 17 is provided in the lower part of the coking tank 12. The waiting inclined tube 16 is connected to the waiting distributor 17. The waiting distributor 17 is used to evenly distribute the material from the waiting inclined tube 16 into the coking tank 12.

[0045] According to the device provided by the present invention, the outlet of the concentrated slurry pipeline 10 is connected to the pre-regenerated inclined tube 16 after the pre-regenerated slide valve 15. The catalyst temperature after the pre-regenerated slide valve is relatively low (500°C), and there is a long mixing space from the pre-regenerated inclined tube to the regenerator. The outlet of the inclined tube is equipped with a pre-regenerated distributor, which can make the injected slurry more fully and evenly mixed with the catalyst, prevent the catalyst from collapsing and breaking due to local high temperature caused by combustion in the coking tank, reduce catalyst loss, and eliminate the impact of concentrated slurry entering the riser and coking on product distribution and settling tank coking.

[0046] As a specific embodiment of the present invention, a hot air injection port 19 is provided at the bottom of the coking tank 12 for injecting hot air stream 11. The stream from the waiting inclined tube 16 contacts and burns with the hot air stream 11 inside the coking tank 12.

[0047] As a specific embodiment of the present invention, a nozzle 20 may be provided at the outlet of the concentrated oil slurry pipeline 10. The nozzle 20 is connected to the inclined tube 16 to be generated. The nozzle 20 may be a throat-type nozzle.

[0048] As a specific embodiment of the present invention, the apparatus provided by the present invention may further include a fractionation tower ( Figure 1 (not shown in the text) and oil slurry desoldering device ( Figure 1 (Not shown in the text) The fractionation tower is provided with a raw material inlet and an oil slurry outlet. The oil slurry desolidification device is provided with an oil slurry inlet and a concentrated oil slurry outlet. The raw material inlet of the fractionation tower is connected to the product outlet of the deep catalytic cracking reaction system. The fractionation tower fractionates the catalytic cracking reaction products to obtain heavy component product oil slurry, which is discharged from the oil slurry outlet. The oil slurry outlet of the fractionation tower is connected to the oil slurry inlet of the oil slurry desolidification device to desolidify and purify the oil slurry to obtain purified oil slurry and concentrated oil slurry. The concentrated oil slurry is discharged from the concentrated oil slurry outlet. The inlet of the concentrated oil slurry pipeline is connected to the concentrated oil slurry outlet of the oil slurry desolidification device.

[0049] In one specific embodiment of the present invention, the flue gas stream 14 generated by the catalyst regeneration system 200 is discharged from the regenerator 13.

[0050] This invention does not limit the structure of the deep catalytic cracking reaction system 100. As a specific embodiment of this invention, the deep catalytic cracking reaction system 100 may include a bed reactor 2, a second riser 3, and a first riser 4. The inlet of the bed reactor 2 is connected to the outlet of the first riser 4, and one end of the second riser 3 is connected to the bed reactor 2. A first water vapor stream 5 and a feedstock stream 6 enter the first riser 4, and a second water vapor stream 7 enters the second riser 3. Additionally, a C4 recycled stream 8 and a light gasoline recycled stream 9 may also enter the second riser 3. The reaction product stream 1 is discharged from the bed reactor 2. The feedstock stream 6 may include one or more of diesel oil, wax oil, and residual oil, etc., and the reaction product stream 1 may include one or more of ethane, ethylene, propylene, liquefied petroleum gas, gasoline, diesel oil, and slurry oil, etc.

[0051] Secondly, the present invention provides a method for adjusting the reverse reheat equilibrium of deep catalytic cracking, comprising the following steps:

[0052] Step 1: Inject the concentrated oil slurry into the waiting inclined tube 16 through the concentrated oil slurry pipeline 10, and mix it with the waiting catalyst from the deep catalytic cracking reaction system 100;

[0053] Step 2: The mixture of concentrated oil slurry and catalyst discharged from the pre-cooking inclined tube 16 is burned in the coking tank 12, releasing heat;

[0054] Step 3: After combustion treatment, the catalyst is regenerated in the regenerator 13 and then carries the heat back from the regeneration inclined tube 18 to the deep catalytic cracking reaction system 100 for heating.

[0055] As a specific embodiment of the present invention, a mixture of concentrated oil slurry and spent catalyst is brought into contact with hot air stream 11 and burned in coking tank 12.

[0056] In one specific embodiment of the present invention, the density of the concentrated oil slurry is 950-1050 kg / m³. 3 For example, 960, 970, 980, 990, 1000, 1010, 1020, 1030, 1040 kg / m³ 3 The preferred density range is 950-1000 kg / m³. 3 .

[0057] In this invention, the concentrated slurry can be recycled from the slurry obtained from the reaction products of the same deep catalytic cracking reaction system. For example, the slurry obtained after fractionation of the reaction product stream 1 generated by the deep catalytic cracking reaction system 100, and after desolidification and purification, is obtained as purified slurry and concentrated slurry. The concentrated slurry enters the concentrated slurry pipeline 10. The concentrated slurry can also be obtained from the slurry obtained from the reaction products of other deep catalytic cracking reaction systems.

[0058] In one specific embodiment of the present invention, the concentrated slurry is obtained by fractionating the products of a deep catalytic cracking reaction and then subjecting it to a desolidification step. Specifically, the deep catalytic cracking reaction products are fractionated to obtain the slurry, which is then subjected to a desolidification step to obtain purified slurry and concentrated slurry. In one specific embodiment of the present invention, the mass flow rate of the concentrated slurry is 20%-100% of the mass flow rate of the slurry, for example, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, etc.

[0059] In this invention, the injection flow rate of the concentrated slurry can be selected based on the heat required to adjust the reverse reheat balance or the required increase in steam production. It can be selected that all of the produced concentrated slurry is injected into the pre-cooking inclined tube 16, or only a portion of the produced concentrated slurry is injected into the pre-cooking inclined tube 16. It should be noted that when more than 60% of the mass flow rate of the concentrated slurry is injected into the pre-cooking inclined tube 16, although this will further increase steam production, it may lead to insufficient contact between the concentrated slurry and the pre-cooking catalyst, resulting in localized combustion in the coking tank and the formation of a high-temperature zone above 800°C, causing thermal deactivation of the catalyst and increasing catalyst loss.

[0060] As a specific embodiment of the present invention, taking an oil slurry flow rate of 17.1 t / h as an example, the flow rate of concentrated oil slurry is 3.42-17.1 t / h.

[0061] In one specific embodiment of the present invention, the temperature of the concentrated slurry injected into the inclined tube 16 to be formed in step 1 is 180-250°C, for example, 190, 200, 210, 220, 230, 240°C, etc., preferably 220-250°C; the pressure of the concentrated slurry injected into the inclined tube 16 to be formed in step 1 is 0.5-2 MPaG, for example, 0.7, 0.9, 1.1, 1.3, 1.5, 1.7, 1.9 MPaG, etc., preferably 1.0-1.5 MPaG.

[0062] As a specific embodiment of the present invention, the temperature range of the hot air flow 11 is 150 to 200°C, the pressure range is 1.0 to 1.2 MPaG, and the amount of hot air flow 11 is mainly to ensure that the catalyst to be generated and the concentrated oil slurry are fully combusted.

[0063] The method provided by this invention allows a 3 million tons / year deep catalytic cracking unit to solve the problem of reverse reheat balance in deep catalytic cracking while simultaneously increasing the production of 4.2MPa steam by 40-60 t / h.

[0064] According to the method provided by the present invention, the slurry from the deep catalytic cracking unit is purified by a slurry desolidification device to obtain purified slurry and concentrated slurry. The concentrated slurry is returned to the regeneration system for coking and heat extraction. Through a nozzle, the concentrated slurry is injected into the catalyst regeneration line after the catalyst regeneration valve, mixing with the catalyst. It then enters the catalyst regeneration system through a regeneration distributor, where it comes into contact with hot air in the coking tank and burns, releasing heat which is sent to the reaction system to provide reaction heat. While increasing the regenerator's heat output, this process does not affect the main reaction in the riser or cause localized high temperatures in the regenerator, thus preventing catalyst damage. The method provided by the present invention, through a new process flow for injecting concentrated slurry, not only solves the thermal balance problem of the deep catalytic cracking reaction but also avoids the catalyst thermal collapse and its impact on product distribution caused by traditional coking methods. This ensures stable long-term operation of the unit and further increases steam production.

[0065] The following detailed description of preferred embodiments of the present invention illustrates the principles of the invention and is not intended to limit the scope of the invention.

[0066] Example 1

[0067] This embodiment provides an apparatus and method for adjusting the reheat balance of deep catalytic cracking.

[0068] Firstly, the apparatus for deep catalytic cracking reverse reheat equilibrium, such as... Figure 1 As shown, the outlet of the concentrated oil slurry pipeline 10 is connected to the pre-generation inclined tube 16 via the nozzle 20 at 2 / 3 of the length of the inclined tube after the pre-generation slide valve 15. The angle α between the outlet of the concentrated oil slurry pipeline 10 and the pre-generation inclined tube 16 is 55°.

[0069] Secondly, according to Figure 1 The process shown, the method for achieving reverse reheat equilibrium in deep catalytic cracking, is as follows: A 3 million tons / year deep catalytic cracking unit uses wax oil and residue oil as feedstock, with ethylene and propylene as the main target products. The slurry discharge rate is 17.1 t / h. Based on the total weight of the discharged slurry, the amount of concentrated slurry is 20% of the total weight of the discharged slurry. Approximately 3.42 t / h of the reprocessed concentrated slurry is injected into the waiting inclined tube. The density of the concentrated slurry is 990.7 kg / m³. 3 The concentrated oil slurry injection temperature was 220℃, the pressure was 1.47 MPaG, and the mass flow rate of the catalyst in the inclined tube was 2321 t / (m²). 2 The temperature of the hot air stream is 180℃, the pressure is 0.23MPa, and the flow rate is 7240Nm³. 3 / min.

[0070] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by about 45t / h.

[0071] Example 2

[0072] This embodiment is basically the same as Embodiment 1, except that in the deep catalytic cracking reverse reheat balance device, the concentrated oil slurry is injected at 1 / 2 of the line after the waiting slide valve 15.

[0073] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by approximately 41t / h.

[0074] Example 3

[0075] This embodiment is basically the same as Embodiment 1, except that in the deep catalytic cracking reverse reheat equilibrium method, the amount of concentrated slurry is 60% of the total weight of the externally thrown slurry, and the density of the concentrated slurry is 967.5 kg / m³. 3 A portion of the concentrated oil slurry is injected into the inclined tube to be generated, with a flow rate of approximately 3.42 t / h.

[0076] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by approximately 44t / h.

[0077] Example 4

[0078] This embodiment is basically the same as Embodiment 1, except that in the deep catalytic cracking reverse reheat equilibrium method, the amount of concentrated slurry is 25% of the total weight of the externally thrown slurry, and the density of the concentrated slurry is 985.7 kg / m³. 3 Approximately 4.28 t / h of concentrated oil slurry from the refining process is injected into the inclined tube awaiting regeneration.

[0079] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by approximately 56t / h.

[0080] Example 5

[0081] This embodiment is basically the same as Embodiment 1, except that in the deep catalytic cracking reverse reheat balance device, the angle α between the outlet of the concentrated oil slurry pipeline 10 and the waiting inclined tube 16 is 46°.

[0082] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by approximately 44t / h.

[0083] Example 6

[0084] This embodiment is basically the same as Embodiment 1, except that in the deep catalytic cracking reverse reheat equilibrium method, the injection pressure of the concentrated oil slurry is 1.0 MPaG.

[0085] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam is increased by approximately 43.5 / h.

[0086] Comparative Example 1

[0087] This comparative example is basically the same as Example 1, except that the concentrated oil slurry is directly injected into the coking tank as fuel oil for combustion. A high temperature zone of over 800°C will be formed around the injection site, causing the catalyst to thermally deactivate and increasing catalyst loss.

[0088] Based on solving the problem of reverse reheat balance in deep catalytic cracking, the production of 4.2MPa steam increased by approximately 38t / h.

[0089] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.

Claims

1. An apparatus for regulating the reverse reheat equilibrium of deep catalytic cracking, characterized in that, It includes a deep catalytic cracking reaction system (100), a catalyst regeneration system (200), and a concentrated oil slurry pipeline (10). The catalyst regeneration system (200) includes a pre-regeneration inclined tube (16), a coke burner (12), a regenerator (13), and a regeneration inclined tube (18) connected in sequence. The end of the waiting-to-be-born inclined tube (16) away from the coking tank (12) is connected to the deep catalytic cracking reaction system (100), and a waiting-to-be-born sliding valve (15) is provided on the waiting-to-be-born inclined tube (16); The outlet of the concentrated slurry pipeline (10) is connected to the pre-cooking inclined pipe (16) located between the pre-cooking slide valve (15) and the coking tank (12). The ratio of the length l1 of the pre-cooking inclined pipe between the connection point and the pre-cooking slide valve (15) to the length l0 of the pre-cooking inclined pipe between the pre-cooking slide valve (15) and the coking tank (12) is l1 / l0 = 1 / 2 to 2 / 3. The end of the regeneration inclined tube (18) away from the regenerator (13) is connected to the deep catalytic cracking reaction system (100).

2. The apparatus according to claim 1, characterized in that, The angle α between the outlet of the concentrated slurry pipeline (10) and the inclined tube (16) is 45°-55°.

3. The apparatus according to any one of claims 1-2, characterized in that, The coking tank (12) is equipped with a waiting distributor (17), and the waiting inclined tube (16) is connected to the waiting distributor (17). Preferably, a hot air injection port (19) is provided at the bottom of the coking tank (12).

4. The apparatus according to any one of claims 1-3, characterized in that, The outlet of the concentrated slurry pipeline (10) is connected to the inclined tube (16) to be generated through a nozzle (20). Preferably, the nozzle (20) is a throat nozzle.

5. The apparatus according to any one of claims 1-4, characterized in that, The apparatus also includes a fractionation tower and an oil slurry desolidification device. The fractionation tower includes a raw material inlet and an oil slurry outlet, and the oil slurry desolidification device includes an oil slurry inlet and a concentrated oil slurry outlet. The feed inlet of the fractionation tower is connected to the product outlet of the deep catalytic cracking reaction system (100). The fractionation tower is used to fractionate the reaction products to obtain slurry and discharge the slurry from the slurry outlet. The oil slurry outlet of the fractionation tower is connected to the oil slurry inlet of the oil slurry desolidification device. The oil slurry desolidification device is used to desolidify the oil slurry to obtain the concentrated oil slurry and discharge the concentrated oil slurry from the concentrated oil slurry outlet. The concentrated oil slurry outlet is connected to the inlet of the concentrated oil slurry pipeline (10).

6. A method for regulating the reverse reheat equilibrium of deep catalytic cracking, characterized in that, The procedure performed in the apparatus according to any one of claims 1-5 includes the following steps: Step 1: The concentrated oil slurry is injected into the pre-cure inclined tube (16) via the concentrated oil slurry pipeline (10) and mixed with the pre-cure catalyst from the deep catalytic cracking reaction system (100); Step 2: The mixture discharged from the calcining tube (16) is burned in the coking vessel (12); Step 3: After combustion, the catalyst enters the regenerator (13) for regeneration and then returns to the deep catalytic cracking reaction system (100) through the regeneration inclined tube (18).

7. The method according to claim 6, characterized in that, The density of the concentrated oil slurry mentioned in step 1 is 950-1050 kg / m³. 3 .

8. The method according to claim 6 or 7, characterized in that, The concentrated oil slurry mentioned in step 1 is derived from: the product obtained by fractionating the oil slurry from the deep catalytic cracking reaction products and then performing a solidification treatment. Preferably, the mass flow rate of the concentrated oil slurry is 20%-100% of the mass flow rate of the oil slurry.

9. The method according to any one of claims 6-8, characterized in that, The temperature of the concentrated oil slurry injected into the inclined tube (16) in step 1 is 180-250℃; And / or, the pressure of the concentrated slurry injected into the inclined tube (16) in step 1 is 0.5-2 MPaG.

10. The method according to any one of claims 6-9, characterized in that, The mixture described in step 2 is combusted in contact with the hot air stream (11) inside the coking tank (12). Preferably, the temperature of the hot air stream (11) is 150-200°C.

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