Method for replacing sequencing valve of regeneration unit of catalytic reforming device without shutdown

Abstract

The invention discloses a method for replacing a sequencing valve of a regeneration unit of a catalytic reforming device without shutdown, which comprises the following steps of: stopping the circulation of a catalyst, reducing the flow of the catalyst, and temporarily storing the catalyst in a catalyst buffer hopper after the catalyst in a catalyst dust separation hopper is subjected to three regeneration steps of scorching, oxychlorination and drying in a regenerator; the valve is replaced when the catalyst is temporarily stored in the catalyst buffer hopper, after the valve is replaced, circulation of the catalyst is recovered, and the catalyst flow is adjusted to a normal value. According to the method, the technical problem that the regeneration internal network is damaged due to frequent shutdown of the regeneration device is solved, and obvious economic benefits are obtained after the method is implemented.

Description

Technical Field

[0001] The present invention relates to the technical field of catalytic reforming, and in particular to a method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation. Background Art

[0002] The catalytic reforming unit uses naphtha as raw material, and undergoes reactions such as cycloalkane dehydrogenation and alkane dehydrogenation (molecular reintegration) in the reactor to generate benzene, toluene, xylene, etc. for use in the downstream PX unit, and produces hydrogen as a by-product. Due to the carbon deposition side reaction during the catalytic reforming reaction, the catalyst activity will gradually decrease. Therefore, it is necessary to use catalyst continuous regeneration technology to restore the catalyst activity to the level of fresh catalyst.

[0003] The process flow of catalyst continuous regeneration technology is as follows: Figure 1 and Figure 2 , the catalyst to be regenerated flowing out of the reactor enters the regeneration device, and is restored to the level of fresh catalyst through the four-step regeneration process. The catalyst with restored activity enters the reactor again for catalytic reaction. The four-step regeneration process includes charring, oxychlorination, drying and reduction processes connected in sequence, of which the first three steps are completed in the regenerator and the fourth step is completed in the reactor. In order to safely circulate the catalyst between the reactor and the regenerator, the 32 programmable valves of the regeneration device constitute a transportation system, which safely achieves the purpose of catalyst circulation through a series of step procedures. However, programmable valves often fail due to various reasons such as wear, internal leakage, diaphragm damage, and actuator abnormality. Once a programmable valve fails, the regeneration device has to be shut down and the valve replaced. During the shutdown and valve replacement period, the temperature of the charred bed layer dropped rapidly from 580℃ to about 460℃ within 20 minutes, with a cooling rate of about 360℃ / h, far exceeding the temperature increase and decrease index of <50℃ / h in the technical regulations, which caused a serious impact on the regenerator internal network; after the valve replacement is completed, the temperature needs to be raised back to 580℃, which will impact the regeneration internal network again. Once the regeneration inner net is deformed or damaged, the catalyst will be damaged and a large amount of dust will be generated, leading to a series of consequences such as increased pressure drop in the reactor, blockage of the regeneration inner net, and difficulty in lifting the catalyst. Summary of the invention

[0004] In order to solve the technical problem that the internal network of the existing catalytic reforming device may be deformed or damaged when the device is shut down for valve replacement, the present invention provides a method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without shutting down the device.

[0005] The technical solution adopted by the present invention is:

[0006] A method for replacing a programmable valve in a regeneration unit of a catalytic reforming device without stopping operation, reducing the flow rate of the catalyst so that the catalyst in the catalyst dust separation hopper is temporarily stored in the catalyst buffer hopper after completing the three regeneration steps of charring, oxychlorination and drying in the regenerator; the valve is replaced during the temporary storage of the catalyst in the catalyst buffer hopper, and after the valve is replaced, the circulation of the catalyst is restored and the flow rate of the catalyst is increased to return to its original value.

[0007] See also Figure 1 The process flow of catalyst recycling regeneration is: dust separation hopper → regenerator → catalyst buffer hopper → 2# lock hopper → 2# lifting tank → reactor → 1# lock hopper → 1# lifting tank → dust separation hopper. The inventive concept of the present invention is: a radioactive source level detector is installed in the lower middle part of the dust separation hopper. During normal production, the radioactive source detector needs to detect the material level, that is, a certain amount of catalyst is always stored in the dust separation hopper. The diameter of the dust separation hopper is 2200mm, the height of the radioactive source level detector is generally set to 935mm, and the bulk density of the reforming catalyst is 0.56t / m 3 , then the amount of catalyst retained above the bottom head of the dust separation hopper is 3.14×(2.2 / 2)2×0.935×0.56=1.98 tons. Since the area below the bottom head of the dust separation hopper is still full of catalyst, the presence of this part of the catalyst can seal the feed pipe. Therefore, the 1.98 tons of catalyst above the bottom head of the dust separation hopper can be used as a buffer for production adjustment. When the regeneration device is in normal production, the catalyst circulates at a rate of 100%. If the circulation rate of the catalyst is reduced to 60%, that is, the catalyst flow rate is 544.2kg / h, and the two locking hoppers are stopped, without adding catalyst to the dust separation hopper, the regeneration device can theoretically maintain safe operation for 1.98 / 0.544=3.65 hours. Based on the above analysis, when a certain programmable valve fails, the circulation rate is reduced to 60% to continue to maintain high-temperature charring. By preparing tools and equipment in advance and increasing construction manpower, the valve replacement was completed in 3 hours and the regeneration device did not need to stop working, thus avoiding the impact of rapid temperature rise and fall on the regeneration internal network and effectively solving problems such as damage to the regeneration internal network caused by frequent shutdowns of the regeneration device.

[0008] Furthermore, the method for replacing a programmable valve in a regeneration unit of a catalytic reforming device without stopping the operation specifically comprises the following steps:

[0009] (1) Calculate the catalyst inventory in the catalyst dust separation hopper at the top of the regenerator;

[0010] (2) adjusting the catalyst flow rate according to the catalyst inventory so that the regeneration device can maintain operation for more than 3 hours during the period when the catalyst circulation is stopped;

[0011] (3) adjusting the oxygen molar content in the charring zone and the chloride flow rate in the oxychlorination zone according to the adjusted catalyst flow rate;

[0012] (4) Stop the catalyst circulation, manually stop the No. 2 lock hopper program, and manually stop the No. 1 lock hopper program;

[0013] (5) Close the manual valve at the bottom outlet of the reactor;

[0014] (6) Replace the valve;

[0015] (7) After the valve is replaced, open the manual valve at the bottom outlet of the reactor, start the No. 1 lock hopper operation program, start the No. 2 lock hopper operation program, and resume the circulation of the catalyst;

[0016] (8) Gradually increase the catalyst flow rate until it returns to the original value, and at the same time increase the oxygen molar content in the charring zone and the chloride flow rate in the oxychlorination zone until they return to the original value.

[0017] Further, step (4) comprises:

[0018] (4.1) After the 2# lock hopper completes the catalyst lifting task, manually stop the 2# lock hopper program;

[0019] (4.2) After the 1# lock hopper completes the catalyst lifting task, manually stop the 1# lock hopper program.

[0020] If there is enough time, empty the catalyst in 2# lifting tank and 1# lifting tank through 2# locking hopper and 1# locking hopper to prevent the catalyst from running away and generating dust when inspecting the valve.

[0021] Furthermore, in step (1), the catalyst inventory is calculated based on the catalyst layer height detected by the radioactive source level detector and the size of the lower head of the catalyst dust separation hopper.

[0022] Furthermore, in step (2), the catalyst flow rate is reduced from an original value of 850-1000 kg / h to 500-600 kg / h.

[0023] When the catalyst flow rate is lower than 500kg / h, the temperature of the charred bed layer drops significantly, causing an impact on the regenerator inner network; and after the catalyst flow rate is reduced, the air volume must be reduced immediately, because the oxygen demand will decrease synchronously after the catalyst flow rate is reduced. If the air volume is adjusted too slowly, it will lead to excess oxygen molar content in the system. Excessive oxygen molar content will cause the combustion temperature to be too high, and the regenerator inner network will be deformed and damaged. The air must first enter the drying area to dry the catalyst, and then enter the charred area to supply oxygen. A lower air flow rate will affect the drying effect.

[0024] Furthermore, in step (3), the oxygen molar content is reduced from an original value of 1.1-1.2% to 0.7-1.0%, and the chloride flow rate is reduced from an original value of 1.1-1.3 kg / h to 0.6-0.8 kg / h.

[0025] The burning of the catalyst is a combustion reaction in the presence of oxygen, which produces carbon dioxide and water and releases heat. This reaction is necessary and useful for decoking, but it is easy to damage the catalyst. It causes the catalyst temperature to rise, and high temperature greatly increases the risk of permanent damage to the catalyst. Therefore, the burning temperature must be controlled, which is mainly achieved by controlling the oxygen molar content during combustion. If the oxygen molar content is higher than 1.3%, it is easy to cause the combustion temperature to be too high, but if the oxygen molar content is lower than 0.7%, the combustion speed is too slow.

[0026] Oxychlorination is the oxidation and dispersion of the metal platinum on the surface of the catalyst. The catalyst needs chlorides to maintain good activity of the acid function. The metal on the surface of the catalyst undergoes oxidation reaction and redispersion reaction under the conditions of oxygen and organic chloride. The more evenly the metal is distributed on the surface of the catalyst, the better the metal function of the catalyst. However, too much or too little chloride will have an adverse effect on the reforming reaction. A chloride flow rate lower than 0.6kg / h will lead to insufficient catalyst acid function and reduced catalyst activity. A chloride flow rate higher than 1.3kg / h will lead to enhanced hydrocracking reaction, reduced hydrogen purity, reduced liquid yield, and in severe cases, the color of the generated oil will become darker.

[0027] Furthermore, in step (8), the rate of increase of the catalyst flow rate is 10% / h of the original flow rate. When the catalyst flow rate is increased by more than 10% / h of the original flow rate, the burning speed increases accordingly, which will significantly increase the difficulty of matching and adjusting the air volume. If the air volume increase rate is not matched properly, it will cause the burning area to overheat. When the catalyst flow rate is increased by less than 10% / h of the original flow rate, the time it takes for the regeneration unit to resume normal production will be longer, increasing the energy consumption of the device.

[0028] Furthermore, in step (8), the rate of increase of the oxygen molar content is 0.1% / h, and the rate of increase of the chloride flow rate is 0.1kg / h. After the catalyst circulation rate is increased, the air volume must be increased immediately to ensure that the catalyst completes the exothermic reaction of charring in the low-oxygen environment of the charring zone. If the charring is not complete at this time, the residual carbon on the catalyst enters the high-oxygen environment of the oxychlorination zone, and will burn rapidly and violently and release a large amount of heat, resulting in over-temperature damage and deformation of the regenerator inner network and over-temperature agglomeration and failure of the catalyst.

[0029] Furthermore, in step (8), while increasing the catalyst flow rate, the temperature of the hydrogen used for reduction in the reactor is increased, and when the catalyst flow rate returns to a normal flow rate, the temperature of the reducing hydrogen is lowered to a normal value.

[0030] Since valve replacement was performed without stopping production, part of the catalyst stayed in the catalyst buffer hopper for about 3 hours longer. This part of the catalyst suffered temperature loss. When the fourth step reduction process was carried out to restore activity, the hydrogen heating jacket in the catalyst reduction zone was opened to increase the temperature of the catalyst during reduction and ensure the activity recovery effect.

[0031] Furthermore, the temperature of hydrogen used for reduction is increased from 140-150° C. to 180-200° C. If the reduction temperature is too low, the metal platinum on the catalyst is unevenly dispersed and the catalyst activity recovery effect is poor; if the reduction temperature is too high, the catalyst is at risk of sintering.

[0032] The beneficial effects of the present invention are as follows: by using the stock catalyst in the separation hopper at the top of the regenerator as a buffer, valve replacement can be achieved without stopping the operation at the minimum circulation rate, avoiding the impact of rapid temperature rise and fall on the regeneration inner network, and solving the technical problem of damage to the regeneration inner network caused by frequent shutdown of the regeneration device. After the implementation of the method of the present invention, obvious economic benefits have been achieved.

[0033] For example, according to past experience, the inner net will break once every three years, and the catalyst loss caused by each inner net breakage is about 5 tons, the catalyst price is about 1.2 million yuan / ton, and the dust replacement catalyst processing fee is about 300,000 yuan / ton. About 40% of the coarse dust in the damaged catalyst can be recovered, and about 60% is worn into fine powder and carried downstream with oil and gas and cannot be recovered. After the implementation of this technology, it can effectively avoid the damage of the regeneration inner net, and save catalyst costs every year: (5×0.6×120+5×0.4×30) / 3=1.4 million yuan / year.

[0034] The manufacturing cost of the regeneration inner net is about 1.5 million yuan, the maintenance cost of the regeneration system is about 400,000 yuan, and the cost of catalyst unloading and screening is about 200,000 yuan. After the implementation of this technology, the damage of the regeneration inner net can be effectively avoided, and the replacement and maintenance cost of the inner net can be saved every year: (1.5 million + 40 million + 20 million) / 3 = 700,000 yuan / year.

[0035] During the shutdown and maintenance period when the regeneration internal network was damaged, the catalytic reforming unit had to operate at a reduced load, and the insufficient processing capacity during this period resulted in the loss of product value. The full load of the reforming unit is 268m 3 / h, and should be reduced to 200m during maintenance 3 / h, processing capacity reduced by 68m 3 / h. After the implementation of this technology, the value leakage caused by insufficient processing capacity can be reduced by approximately 328.09 yuan each year.

[0036] To sum up the above, the total economic benefits that can be obtained are: 140+70+328.09=538.09 million yuan / year. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 It is a process flow diagram of a catalytic reforming unit.

[0038] Figure 2 It is a structural diagram of the regenerator.

[0039] Figure 3 This is a trend diagram of bed temperature variation during valve replacement in the regeneration unit of Example 1 without stopping operation.

[0040] Figure 4 This is a diagram showing the bed temperature variation trend during valve replacement without stopping the regeneration unit of Example 2.

[0041] Figure 5 This is a trend diagram of bed temperature variation during valve replacement without stopping the regeneration unit of Example 3.

[0042] Figure 6 This is a trend chart of bed temperature variation during the regeneration unit shutdown and valve replacement period of Example 1. DETAILED DESCRIPTION

[0043] The present invention is further described below in conjunction with specific examples to facilitate understanding of the present invention, but the present invention is not limited thereto.

[0044] Example 1

[0045] On January 24, 2022, the 26# programmable valve in the regeneration unit leaked internally and the valve needed to be replaced.

[0046] (1) The catalyst inventory is calculated to be 1.98 tons based on the catalyst layer height detected by the radioactive source level detector and the size of the lower head of the catalyst dust separation hopper;

[0047] (2) At 12:30, the catalyst flow rate was reduced from 100% to 60%, that is, from 907 kg / h to 544.2 kg / h, so that the regeneration device could maintain safe operation for 1.98 / 0.544 = 3.65 hours when the catalyst stopped circulating;

[0048] (3) Reduce the burning air volume from 350Nm 3 / h is reduced to about 220Nm 3 / h, reducing the oxygen molar content in the charring zone from 1.12% to 0.72%, and reducing the chloride flow rate from 1.15kg / h to 0.75kg / h;

[0049] (4) At 14:25, the catalyst circulation was stopped, and the catalyst in the catalyst dust separation hopper was temporarily stored in the catalyst buffer hopper after completing the three regeneration steps of charring, oxychlorination, and drying in the regenerator; the operation of the 2# lock hopper program was manually stopped, and the operation of the 1# lock hopper program was manually stopped;

[0050] (5) Close the manual valve at the bottom outlet of the reactor;

[0051] (6) Replace the valve;

[0052] (7) At 17:13, the valve was replaced, the manual valve at the bottom outlet of the reactor was opened, the No. 1 lock hopper operation program was started, and the No. 2 lock hopper operation program was started; the catalyst circulation was resumed, and the catalyst flow rate was started to increase;

[0053] (8) By 21:21, the catalyst flow rate returned to the original value of 907 kg / h within 4 hours, that is, the catalyst flow rate increased by 90.7 kg / h per hour; while increasing the catalyst flow rate, the oxygen molar content in the charring zone was increased at a rate of 0.1% / h to return to the original value of 1.12%; the chloride flow rate was increased at a rate of 0.1 kg / h to return to the original value of 1.15 kg / h.

[0054] from Figure 3 It can be seen that during the valve replacement without stopping work, the peak temperature of the regeneration unit burnout slowly decreased from the highest value to the lowest value, and the peak temperature gradually decreased from 580°C to 530°C, which took about 4 hours and the cooling rate was about 10°C / h. The cooling rate was gentle, which was less than the temperature increase and decrease index of <50°C / h in the technical regulations.

[0055] Example 2

[0056] On February 13, 2023, the packing of the 27# programmable valve in the regeneration unit leaked and the valve needed to be replaced.

[0057] (1) The catalyst inventory is calculated to be 1.98 tons based on the catalyst layer height detected by the radioactive source level detector and the size of the lower head of the catalyst dust separation hopper;

[0058] (2) At 13:52, the catalyst flow rate was reduced from 100% to 70%, that is, from 907 kg / h to 634.9 kg / h, so that the regeneration device could maintain safe operation for 1.98 / 0.63 = 3.1 hours when the catalyst stopped circulating;

[0059] (3) Reduce the burning air volume from 360Nm 3 / h reduced to about 250Nm 3 / h, the oxygen molar content in the charring zone is reduced from 1.10% to 0.80%, and the chloride flow rate is reduced from 1.13kg / h to 0.8kg / h;

[0060] (4) At 14:43, the catalyst circulation was stopped, and the catalyst in the catalyst dust separation hopper was temporarily stored in the catalyst buffer hopper after completing the three regeneration steps of charring, oxychlorination, and drying in the regenerator; the operation of the 2# lock hopper program was manually stopped, and the operation of the 1# lock hopper program was manually stopped;

[0061] (5) Close the manual valve at the bottom outlet of the reactor;

[0062] (6) Replace the valve;

[0063] (7) 16:55 After the valve replacement is completed, the manual valve at the bottom outlet of the reactor is opened, the No. 1 lock hopper operation program is started, and the No. 2 lock hopper operation program is started; the catalyst circulation is resumed, and the catalyst flow rate is started to be increased.

[0064] (8) By 19:46, the catalyst flow rate returned to the original value of 907 kg / h within 3 hours, that is, the catalyst flow rate increased by 90.7 kg / h per hour; while increasing the catalyst flow rate, the oxygen molar content in the charring zone was increased at a rate of 0.1% / h to return to the original value of 1.10%; the chloride flow rate was increased at a rate of 0.1 kg / h to return to the original value of 1.13 kg / h.

[0065] from Figure 4 It can be seen that during the valve replacement without stopping work, the peak temperature of the regeneration unit slowly decreased from the highest value to the lowest value, and the peak temperature gradually decreased from 578°C to 532°C, which took about 4 hours, and the cooling rate was about 11.5°C / h; the cooling rate was gentle, which was less than the temperature increase and decrease index of <50°C / h in the technical regulations.

[0066] Example 3

[0067] On April 25, 2023, the 4# programmable valve of the regeneration unit got stuck during operation and the valve needed to be replaced.

[0068] (1) The catalyst inventory is calculated to be 1.98 tons based on the catalyst layer height detected by the radioactive source level detector and the size of the lower head of the catalyst dust separation hopper;

[0069] (2) 8:16, the catalyst flow rate was reduced from 100% to 60%, that is, from 907 kg / h to 544.2 kg / h, so that the regeneration device could maintain safe operation for 1.98 / 0.544 = 3.65 hours when the catalyst stopped circulating;

[0070] (3) Reduce the burning air volume from 360Nm 3 / h is reduced to about 225Nm 3 / h, the oxygen molar content in the charring zone is reduced from 1.11% to 0.73%, and the chloride flow rate is reduced from 1.13kg / h to 0.73kg / h;

[0071] (4) At 10:50, the catalyst circulation is stopped, and the catalyst in the catalyst dust separation hopper is temporarily stored in the catalyst buffer hopper after completing the three regeneration steps of charring, oxychlorination, and drying in the regenerator; the operation of the 2# lock hopper program is manually stopped, and the operation of the 1# lock hopper program is manually stopped;

[0072] (5) Close the manual valve at the bottom outlet of the reactor;

[0073] (6) Replace the valve;

[0074] (7) At 13:20, the valve was replaced, the manual valve at the bottom outlet of the reactor was opened, the No. 1 lock hopper operation program was started, and the No. 2 lock hopper operation program was started; the catalyst circulation was resumed, and the catalyst flow rate began to be increased.

[0075] (8) By 17:03, the catalyst flow rate returned to the original value of 907 kg / h within 4 hours, that is, the catalyst flow rate increased by 90.7 kg / h per hour; while increasing the catalyst flow rate, the oxygen molar content in the charring zone was increased at a rate of 0.1% / h to return to the original value of 1.11%; the chloride flow rate was increased at a rate of 0.1 kg / h to return to the original value of 1.13 kg / h.

[0076] from Figure 5 It can be seen that during the valve replacement without stopping work, the peak temperature of the regeneration unit slowly decreased from the highest value to the lowest value, and the peak temperature gradually decreased from 575°C to 506°C, which took about 3 hours and the cooling rate was about 23°C / h. The cooling rate was gentle, which was less than the temperature increase and decrease index of <50°C / h in the technical regulations.

[0077] Comparative Example 1

[0078] On January 1, 2021, the 29# programmable valve of the regeneration unit malfunctioned and became stuck, the regeneration unit stopped, the air was evacuated, and the circulation stopped.

[0079] from Figure 6 It can be seen that the peak temperature of the charring dropped rapidly from 9:23 to 9:38, and the peak temperature dropped rapidly from 572°C to 478°C, with a cooling rate of about 376°C / h, far exceeding the temperature rise and fall index of <50°C / h in the technical regulations.

[0080] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention. These improvements and modifications are also within the protection scope of the present invention.

Claims

1. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation, characterized in that: The catalyst flow rate is reduced so that the catalyst in the catalyst dust separation hopper is temporarily stored in the catalyst buffer hopper after completing the three regeneration steps of charring, oxychlorination and drying in the regenerator; the valve is replaced while the catalyst is temporarily stored in the catalyst buffer hopper. After the valve replacement is completed, the circulation of the catalyst is restored and the catalyst flow rate is increased to return to its original value.

2. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 1, characterized in that: The specific steps include: (1) Calculate the catalyst inventory in the catalyst dust separation hopper at the top of the regenerator; (2) adjusting the catalyst flow rate according to the catalyst inventory so that the regeneration device can maintain operation for more than 3 hours during the period when the catalyst circulation is stopped; (3) adjusting the oxygen molar content in the charring zone and the chloride flow rate in the oxychlorination zone according to the adjusted catalyst flow rate; (4) Stop the catalyst circulation, manually stop the No. 2 lock hopper program, and manually stop the No. 1 lock hopper program; (5) Close the manual valve at the bottom outlet of the reactor; (6) Replace the valve; (7) After the valve replacement is completed, open the manual valve at the bottom outlet of the reactor, start the No. 1 lock hopper operation program, start the No. 2 lock hopper operation program, and resume the circulation of the catalyst; (8) Gradually increase the catalyst flow rate until it returns to the original value, and at the same time increase the oxygen molar content in the charring zone and the chloride flow rate in the oxychlorination zone until they return to the original value.

3. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: Step (4) comprises: (4.1) After the 2# lock hopper completes the catalyst lifting task, manually stop the 2# lock hopper program; (4.2) After the 1# lock hopper completes the catalyst lifting task, manually stop the 1# lock hopper program.

4. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: In step (1), the catalyst inventory is calculated based on the catalyst layer height detected by the radioactive source level detector and the size of the lower head of the catalyst dust separation hopper.

5. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: In step (2), the catalyst flow rate is reduced from an original value of 850-1000 kg / h to 500-600 kg / h.

6. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 5, characterized in that: In step (3), the oxygen molar content is reduced from the original value of 1.1-1.2% to 0.7-1.0%, and the chloride flow rate is reduced from the original value of 1.1-1.3 kg / h to 0.6-0.8 kg / h.

7. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: In step (8), the catalyst flow rate is increased at a constant rate of 10% of the original value.

8. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: In step (8), the rate of increase of the oxygen molar content is 0.1% / h, and the rate of increase of the chloride flow rate is 0.1 kg / h.

9. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 2, characterized in that: In step (8), while increasing the catalyst flow rate, the temperature of the hydrogen used for reduction in the reactor is increased, and when the catalyst flow rate returns to a normal flow rate, the temperature of the hydrogen is reduced to a normal value.

10. A method for replacing a program-controlled valve in a regeneration unit of a catalytic reforming device without stopping the operation according to claim 9, characterized in that: The reducing hydrogen temperature is increased from 140-150°C to 180-200°C.

Images