JP2006515798A - Conversion method for fixed bed catalytic reformer - Google Patents

Abstract

A method for converting a fixed bed catalytic reformer to a moving bed apparatus is disclosed. Converting the fixed bed reactor to a moving bed reactor having facilities for continuously or intermittently supplying catalyst, and continuous or intermittent addition of fresh or regenerated catalyst to the catalyst inlet of the moving bed reactor, and Allows continuous or intermittent removal of spent catalyst from the catalyst outlet of the moving bed reactor. Waste catalyst withdrawn from the reactor is supplied with a non-integrated regenerator (off-site regenerator, centrally located on-site regenerator that serves several reformers, or a second moving bed device). Can be a shared regenerator). The moving bed reactor, catalyst supply equipment and catalyst recovery equipment should be operable between themselves and existing equipment from fixed bed equipment (piping, compression, reformer feed handling and heating, etc.) Connected. The converted equipment is operated at a reactor pressure effective to improve the quality and yield of the reformate and to exceed the reformate product from the fixed bed equipment prior to conversion.

Description

  The present invention generally relates to catalytic reformers. More particularly, the present invention relates to an improved process for converting or converting a high pressure fixed bed catalytic reformer to a catalytic reformer equipped with a continuous moving bed reactor.

  Catalytic reforming is an established refinery process. It is used to improve the octane quality of hydrocarbon feedstock. In general, reforming refers to the molecular action of a hydrocarbon feedstock produced by a substantial number of reactions or the overall action of a hydrocarbon reaction. Typical reforming reactions include cyclohexane dehydrogenation, alkylcyclopentane dehydroisomerization, paraffin and olefin dehydrocyclization, substituted aromatic isomerization, and paraffin hydrocracking. A typical reforming catalyst is a multifunctional catalyst having a hydrogenation-dehydrogenation component dispersed in a porous inorganic oxide support. The carrier may also generally contain acidic functional groups necessary for the modification reaction.

  The reforming reaction is endothermic and exothermic. The endothermic reaction is generally dominant at the initial stage of reforming. The exothermic reaction is dominant in later reaction stages. The reformer generally supplies additional heat to the reaction stream as it passes from one reactor to the next to compensate for the heat absorbed by the overall endothermic characteristics of the process. A plurality of reactors connected in series with a furnace tube to Traditionally, the reforming process has been operated as a semi-regenerative or circulating process using a fixed bed reactor or as a continuous process using a moving bed reactor. Proposals have also been made to combine fixed bed and moving bed reactors with regeneration modes appropriate to the reactor type used in the hybrid configuration, which allows fixed bed reactors to be regenerated, usually a fixed bed type. The semi-regenerative regeneration is held, and the moving bed reactor in the apparatus holds a dedicated moving bed regenerator. This hybrid type apparatus is disclosed in, for example, Patent Document 1, Patent Document 2, Patent Document 3, Patent Document 4, Patent Document 5, Patent Document 6, Patent Document 7, and Patent Document 8. The apparatus described in US Pat. No. 6,057,096 uses two rows of fixed bed reactors, each row having a final moving bed reactor at its end, the moving bed reactor being a moving bed reactor. Share the regenerator. The apparatus shown in US Pat. No. 6,047,096 uses two rows of fixed bed apparatus that feed a shared moving bed reactor (with its own, fully integrated regenerator). A similar hybrid reformer using a combination of fixed bed and moving bed reactors is described in [1]. Patent Document 9 describes a moving bed reformer in which two stacked moving bed reactors share a common regenerator. Recently, UOP has its CycleX® to increase hydrogen production from a fixed bed reformer by adding a circulating catalytic reactor as the final reactor in the reactor row. Announced the process. The reactor is provided with its own heater and regenerator as an extension rather than a replacement of existing assets (see Non-Patent Document 2).

  In semi-regenerative reforming, deactivation of the catalyst caused by coke deposition until the entire system is finally shut down for catalyst regeneration and reactivation that is carried out while the catalyst remains in the reactor. In order to compensate, the entire reforming process apparatus is operated by gradually and gradually increasing the temperature. In cyclic reforming, the reactors are individually separated by various piping configurations. The catalyst is regenerated and then reactivated while the other reactors in the series remain online. In a “rocking reactor”, the reactor is temporarily replaced and removed from the series for catalyst regeneration and reactivation, and then the reactor is returned to the series. In continuous reforming, the reactor is a moving bed reactor with continuous and intermittent catalyst additions and withdrawals, where the catalyst moves progressively through the reactor and is then regenerated and reactivated. It passes through the regeneration zone for conversion and is then returned to the reactor again. In the regenerator, at least a portion of the deposited coke is burned off, and the regenerated catalyst is recycled to the reactor and continues to circulate. Commercial continuous reformers may have reactors arranged in a parallel or stacked configuration. In its continuous mode of operation with its frequent regeneration, coke build-up on the catalyst can be tolerated, so continuous devices can be operated at pressures lower than those normally used in semi-regenerative and circulating devices. It is important, or at least desirable, to extend the catalyst life between subsequent regenerations.

  In Europe and the United States, environmental concerns have driven the removal of lead from gasoline pools and the introduction of premium grade high-octane unleaded gasoline. In response, oil refiners have changed the way that refinery equipment operates to meet the demands for high octane unleaded gasoline contamination. The majority of refinery gasoline pools are produced by catalytic reformers and, for this reason, improved reforming methods and apparatus for producing lead-free fuel oil products having sufficient octane numbers is required. Reformation can also be an attractive source of hydrogen in refineries, especially when fuel oil sulfur levels must be reduced to meet government regulations.

US Pat. No. 5,190,638 US Pat. No. 5,190,639 US Pat. No. 5,196,110 US Pat. No. 5,211,838 US Pat. No. 5,221,463 US Pat. No. 5,354,451 US Pat. No. 5,368,720 US Pat. No. 5,417,843 US Pat. No. 4,498,973 NPRA paper number AM-96-50 “IFP Solutions for Revamping Catalytic Reforming Units” (1996 NPRA Annual Meeting, March 17-19, 1996) NPRA paper AM-03-93

  A semi-regenerative reformer can be converted to a continuous moving bed system to take advantage of the high octane reformed oil and improved hydrogen yields associated with continuous operation, but this has been considered The conversion is a replacement of the entire device, requiring the replacement of virtually all existing vessels and most of the auxiliary equipment, as well as the installation of an integrated catalyst regenerator, which is the most expensive in this conversion. It is one of those things. The cost of the regenerator can be as much as about 80 percent of the total cost required for conversion. Accordingly, there is still a need for an improved and less expensive method for converting a fixed bed reformer unit to a moving bed reformer.

  The present invention generally relates to techniques for converting a fixed bed catalytic reformer to a moving bed catalytic reformer. The conversion costs associated with this conversion technology are, in part, significantly lower than existing conversions because this technology uses existing equipment and does not require a dedicated on-site continuous catalyst regeneration facility. . Another advantage of the present invention is that a significant number of existing moving bed catalytic reformers share a single catalyst regeneration facility and further reduce the investment required to convert several fixed bed units. Is possible.

  According to the present invention, a technique for converting a fixed bed catalytic reforming apparatus having at least one fixed bed catalytic reforming reactor into a moving bed apparatus is used as a moving bed catalytic reforming reactor. , Allowing fresh or regenerated catalyst to be added continuously or intermittently to the catalyst inlet of the reactor, and waste catalyst to be removed continuously or intermittently from the catalyst outlet of the reactor. The apparatus is provided with a catalyst supply facility for continuously or intermittently charging fresh or regenerated catalyst into the moving bed reactor in continuous or intermittent operating modes. In addition, a waste catalyst recovery facility is added to collect the waste catalyst, temporarily store it, and transfer it to the catalyst regeneration facility. The moving bed reactor, catalyst supply equipment and catalyst recovery equipment are operably connected between themselves and to existing equipment (piping, accessory equipment) of fixed bed equipment that does not require replacement.

  The moving bed reactor is operated at a pressure effective to improve the quality and yield of the reformate compared to the quality and yield of the fixed bed equipment prior to conversion. Compared to the quality and yield of the reformate obtained from the fixed bed equipment prior to the conversion, the moving bed reforming reactor of the converted equipment substantially improves the quality and yield of the reformate. It is an advantage of the present invention that it can operate at an effective pressure sufficiently low. However, during normal operation, this pressure is maintained at a high enough value to allow the use of some of the existing fixed bed catalytic reformer equipment such as compressors, heat exchangers, and furnace tubes. . Using a fully integrated continuous reactor-pressure higher than typical for a regenerator thereby allows the catalyst flow rate for regeneration (compared to that of an integrated device) This is desirable in that the burden of handling the catalyst is reduced.

  The effective operating pressure of the converted reformer can generally be substantially lower than the reactor pressure during operation of the fixed bed apparatus. Typically, the effective operating pressure of the converted reformer is about 15 to about 70%, preferably about 20 to about 60%, more preferably greater than the reactor pressure during operation of the fixed bed unit prior to conversion. Can be about 25 to about 50% lower.

  In the present invention, an off-site catalyst regeneration facility can be used. Alternatively, the present invention can use a shared on-site continuous catalyst regeneration facility, i.e., a continuous catalyst regenerator shared between two or more reactors. Also, a discontinuous on-site regeneration facility can be used for one or more catalytic reformers.

  Depending on the site economics and other factors, it may be preferable to use off-site catalyst regeneration equipment. Alternatively, an on-site continuous regeneration facility may be placed near a plurality of converted reformers. The catalyst from the reformer's continuous reactor can be transported to a regeneration facility and, after regeneration, returned to the reformer for reuse in the reactor. The transfer from the reactor to the regenerator can be carried out continuously by means of a suitable transfer device, for example a conveyor, or depending on the field requirements, the proximity of the regenerator and other factors, for example a truck. Or it can also carry out intermittently with a rail vehicle. Another variation is to use an on-site discontinuous regeneration facility, such as a recirculating regenerator that can be used to regenerate the catalyst from multiple moving bed reformers.

  The present invention provides a substantially low cost option for refiners to significantly improve the performance and operating factor of existing fixed bed reformers. The discontinuous (or fixed bed) catalytic reformer may be a semi-regenerative catalytic reformer, a swinging reactor (also called a regenerative reformer) catalytic reformer, or a hybrid system. Yes, all this is known.

  The non-continuous catalytic reformer may be a semi-regenerative device. Semi-regenerative devices typically include one or more fixed bed reactors operated in series with an interbed heater that maintains operating severity by raising the reaction temperature when the catalyst is deactivated. . The semi-regenerative device is eventually shut down for catalyst regeneration and reactivation.

Typical semi-regenerative reformer operating conditions are:
Pressure: 1035-3800 kPag (about 150-550 psig)
Temperature: 425-565 ° C (approximately 800-1050 ° F)
Space velocity: 0.5-3.0WHW
It is.

  The high pressure semi-regenerative catalytic reformer is a reactor of the converted equipment to ensure substantial improvement in reformate quality and yield (compared to the semi-regenerative equipment prior to conversion). Can be effectively converted to operate at lower effective reactor pressures, but this conversion can be handled once the conversion has been made (handling, discharge, transfer, regeneration) of the catalyst. It does not cause the above-mentioned problems that cannot be overcome. In particular, the process of the present invention enables the production of a reformed oil having an octane number of preferably 90-105, more preferably 95-103, most preferably 98-102. In addition to the improved reformate quality and yields obtained, the effective reactor pressure used in the present invention is compatible with existing equipment such as compressors, heat exchangers, furnace tubes, piping, drums, and pumps. Enable use.

  This effective pressure is generally lower than the reactor pressure of a typical semi-regenerative unit, but it also relates to a typical continuous reactor (in this case related to catalyst speed caused by handling considerations). Higher) without any similar constraints. The pressure can range from 345 to 2760 kPag (50 to 400 psig), preferably from 690 to 2620 kPag (100 to 380 psig), more preferably from about 1035 to 2415 kPag (150 to about 350 psig).

  The converted equipment will be operated at an effective reactor pressure, which provides a substantially improved reformate quality and yield compared to existing fixed bed reformers. provide. The degree of reactor pressure reduction may be limited to the extent that many of the existing compression, furnace, piping, and other devices can be reused with the new moving bed reactor, if desired. Limiting the degree of pressure drop also reduces the required catalyst circulation rate (between the reactor and the regeneration facility). This is particularly attractive in systems where spent catalyst is sent offsite for regeneration. In general, a reactor pressure drop of about 25 to about 50% can be achieved without the need to replace most existing equipment. However, even greater pressure drops can be used if it may be attractive to replace many of the existing equipment under certain site-specific conditions.

  The fixed bed reformer is a moving bed reforming reactor that can continuously add freshly regenerated catalyst to the reactor inlet and continuously remove waste catalyst from the reactor outlet. It is preferable to convert. This can be accomplished by providing a suitable storage facility for the regenerated catalyst or by using a regenerator shared by two or more reactor rows. In the latter case, for example, the catalyst from the converted apparatus is integrated in the regenerator row with the (second) reactor row, but not with the first reactor row, ie The regenerator for the converted device is regenerated by the regenerator of the second reformer which is not a dedicated regenerator. The shared regenerator is fully integrated into one reactor row, but can be configured to have the capacity to regenerate catalyst from two or more reactors. Non-integrated reactors may be on-site (same refinery plant) or at a remote site. In this way, the substantial capital cost of the regenerator is correspondingly reduced due to the economies of scale associated with the regenerator.

  Converting a fixed bed (semi-regenerative or recirculating) reformer to operation with a moving bed reactor can involve at least one fixed bed reactor, preferably all of the fixed bed reactors in the device, Exchange or conversion to a moving bed reactor may be included. The catalyst equipment of the converted apparatus and the continuous moving bed reactor are connected to an existing plant apparatus so that they can be operated as required. The moving bed reactors can be arranged in a parallel or stacked configuration, depending on site requirements. This conversion is indeed a continuous reactor and selected (ie off-site, non-integrated on-site, or partially integrated) in addition to catalyst charging and recovery (removal) equipment. It is necessary to add a transfer facility related to the boundary with the regenerator (which is a regenerator that is shared).

  Waste catalyst recovered from the reformer can be collected and transferred to an off-site regeneration facility. The catalyst is preferably recovered in a continuous manner. The spent catalyst leaving the last reactor will be collected in a spent catalyst storage vessel and then transferred in smaller batches to a drum or special container suitable for transport to an off-site regeneration facility.

  The catalyst can be collected in a storage device (drum, container, container) and transferred to a regeneration facility. The equipment for collecting the waste catalyst and the equipment for transferring it may be different. For example, they can be as simple as a dump nozzle at the bottom of the last reactor (the contents are emptied through a conventional 200 liter (55 US gallon) drum). . Alternatively, they can include specially designed trucks, rail vehicles or shipping containers that can maintain an inert atmosphere during loading, shipping and removal.

  The catalyst regeneration facility can be off-site or, preferably, centrally located on-site if on-site conditions permit. In most cases, it is preferred that the regenerator is independent and only indirectly associated with a particular reformer, although a shared regenerator configuration may be possible, and in some circumstances it may be There are even desirable cases. In this way, an independent regeneration facility can be operated independently of any particular reformer and can regenerate the catalyst from one or more reformers. Thereby, in addition to the increase in operational flexibility regarding the reformer and the regeneration facility, it is possible to reduce the investment amount (apparatus standard) and improve the reformed oil product. According to this embodiment, the centrally located catalyst regeneration facility continuously or intermittently receives waste catalyst from a plurality of moving bed reformers, and the regenerated catalyst is fed to the reactors of these devices. Supply continuously or intermittently.

  Any typical reforming catalyst can be used, including a catalyst comprising one or more Group VIII noble metals on a refractory support. This catalyst comprises a hydrogenation-dehydrogenation function (hydrogen transfer) and an acid function. Examples include catalysts comprising platinum, tin, rhenium, iridium, tin or combinations of these metals. Suitable supports include substantially spherical alumina support particles. Suitable catalysts include platinum, platinum and tin, or platinum and rhenium on substantially spherical alumina support particles. Spherical particles are preferred because they pass through moving bed reactors and other equipment with minimal catalyst attrition.

  Any type of regeneration facility can be used. One suitable regeneration facility may include a continuous moving bed regeneration tower (typical for a commercially available continuous reforming process) and may include a batch regeneration process unit. An example of a batch regeneration process is the Hot Flue Gas Regeneration Circuit, which is characteristic of cyclic power homing (POWERFORMING®). Another example is a shut-off semi-regenerative device used exclusively for catalyst regeneration.

Suitable regeneration procedures can include hydrocarbon purge, coke combustion, oxychlorination, oxide purge and reduction procedures. However, it can also include presulfidation as part of the regeneration procedure, depending on the type of catalyst. When it is preferable to complete the reduction and (if necessary) presulfidation after the regenerated catalyst has been returned from the off-site regeneration facility and immediately before feeding the regenerated catalyst to the top reactor top There is. Oxychlorination treatment can vary significantly. At a minimum, it involves the addition of chloride, including substances such as Cl ₂ , HCI or pumpable organic chloride, to replace chloride lost during coke combustion after coke combustion. There is a case. However, it may also involve the continuous addition of chloride material during coke combustion. It may also include a chloride equilibration step after the platinum metal has been completely redispersed following excessive chlorination after coke combustion. The actual regeneration procedure may include any combination of these chlorination techniques.

  FIG. 1 is provided only as an illustration and shows a continuous catalytic moving bed reforming process apparatus 10. This apparatus is constructed by removing a fixed bed reactor case from an existing high pressure semi-regenerative reformer and installing a moving bed case arranged in a parallel configuration. When inevitably determined by on-site demands, such as limited area, the lift pot and transfer line shown in FIG. 1 is connected to a gravity trickle from one reactor in the row to the next. Can be conveniently used in a stacked reactor configuration in which the catalyst transfer device is necessarily reduced. In FIG. 1, thick lines indicate new devices and piping, and thin lines indicate existing devices and piping.

For the conversion, the semi-regenerative reactor (not shown) is replaced with a new moving bed reactor 27, 57, 65, respectively, the platform 18 for charging fresh / regenerated catalyst, and line 11 It includes installing a fresh catalyst storage drum 20 through which fresh / regenerated catalyst is fed (the feed is controlled by valve 13). Other newly added items include inter-catalyst transfer devices including waste catalyst storage drums 71 and 73, collection devices 24, 54 and 64, lift pots 31, 61 and 69 and transfer lines 53, 58 and 59, A waste catalyst charging platform 24, a dust filter 26, an N ₂ cooler 28, an N ₂ circulator 30, a supplemental nitrogen supply port 32, and an H ₂ preheater 34 are included. Similar equipment for removing the spent catalyst from the last reactor is shown, including a separation hopper 71, a lock hopper 73, and a charging platform 74. Other additional items are discussed again below. The following existing equipment items are retained and reused in the converted equipment: charging furnace 36, reheat furnaces 38, 40, feed / effluent heat exchanger 42 and corresponding lines, effluent. A cooler 44 and corresponding lines, a product separator 46, a recycle compressor 48, and a chloride processor 50;

In operation, the converted device is operated as follows.
Fresh catalyst or regenerated catalyst from off-site regeneration facilities is placed on the charging platform 18 and added to the regenerated catalyst storage drum 20. The catalyst then enters lock hopper 17 (purged with nitrogen from line 15 to remove residual air). The catalyst is then transferred to the lift joint 19 where the catalyst is transferred to the top of the first reactor 27 via the transfer line 52 by hydrogen gas supplied via line 19 and valve 21. Lifted to reduction / purge / separation chamber 12. The gas is removed from the hopper 12 in the elution pipe 12 and passes to the dust filter (new) 26 via the pipe line 43. The reduced catalyst is added to the first reactor 27 via the catalyst flow line 37. The catalyst moves under the reactor 27 by gravity, and then the catalyst exits via the conduit 41 and enters the catalyst collector 24 to which the hydrogen rich gas is supplied via the conduit 39. The catalyst from the catalyst collector 24 then enters the lift coupling 31 where the catalyst is lifted to the separation hopper 55 with a H ₂ rich stream. Lift gas flows through the valve / inlet 33. The catalyst enters the second separation hopper 44 at the top of the second reactor 57 and then enters the reactor 57 where the catalyst moves down to the outlet, where the catalyst collector 54 is followed by the lift coupling. Move into 61. The catalyst from the lift coupling 61 is then lifted by the hydrogen rich gas to the separation hopper 16 at the top of the third or last reactor 65, from which the catalyst is then passed to the third or last reactor. Move to 65 entrances. The catalyst flows down through the reactor 65 to the collector 64 and then to the lift coupling 69. The catalyst from the lift joint 69 is lifted to the separation / storage drum 71 with hydrogen-rich gas, where the gas is separated from the catalyst and sent to the dust removal filter 26 via the wind duct 22. The spent catalyst is then transferred to the lock hopper 73 where it is purged with nitrogen and finally loaded into a transport vessel on the spent catalyst loading platform 24.

  The reformer charge enters the apparatus at inlet 85, obtains hydrogen-rich recycle gas from line 83, and via line 82, effluent heat exchanger 42, then the preheating furnace (both first Is held by the device). The charge moves from the preheating furnace tube into the first reactor 27 and comes into contact with the catalyst. After passing through the first reactor 27, the charge is now routed to the second reactor 57 via the reheat furnace 38 (also held item) and finally to the reheat furnace. Move to the third reactor 65 via 40 (held). The reformate effluent from the third reactor is taken via line 89 into charge heat exchanger 42 and recycle hydrogen heat exchanger 34 to effluent cooler 44 and then to pipe. Via line 88, the existing product separator 46 is reached where the liquid and gas are separated. The hydrogen rich gas is recompressed by the compressor 48 supplied via the line 77 and returned to the apparatus via the line 83 as a recirculated gas, or via the existing chloride processor 50. Sent outside the refinery equipment. Unstabilized reformed oil is recovered via line 75.

  The purge nitrogen is introduced via the replenishment inlet 32, moves to the nitrogen loop via the knockout drum 45, then moves to the lift joint 17 via the line 51, and also via the line 15. Nitrogen is also introduced into the lock hopper 23. The gas from the reactor moves to the nitrogen cooler 28 via the dust filter 26 and then returns to the nitrogen loop via the knockout drum 45.

FIG. 1 does not show an actual off-site or centrally located on-site regeneration facility. Several different designs can be used with these regeneration facilities. The preferred design can vary based on actual project details. The off-site playback system options are
1) Equipment available immediately from commercial catalyst regeneration companies,
2) Continuous moving bed regeneration technology,
3) a commercially available recirculating regeneration facility, including high temperature flue gas technology (Hot Fluid Gas Technology) provided by EXXONMOBIL POWERFORMING Technology, or
4) may include existing dormant semi-regenerative catalytic reformers of various configurations dedicated to completion of catalyst regeneration.

A variation of this method is:
1) send all spent catalyst removed from the outlet of the last reactor to a third party catalyst supplier who can regenerate the catalyst at a fee,
2) For an existing semi-regenerative reformer, as part of a conversion project, an oversized regeneration facility (the size of this facility is the catalyst from other equipment that may also be converted) Can also be used to recycle
3) to build a very large regeneration facility in a central location and to regenerate the catalyst from other semi-regenerative reformers in the area to be converted,
4) Use or dormant existing dormant semi-regenerative reformers to regenerate spent catalyst from other active semi-regenerative reformers in the area to be converted And 5) At one or more locations that are already using continuous contact regeneration technology, the on-site equipment at the site is in the other equipment (they are currently regenerating) Expansion of existing regeneration equipment may be included so that the catalyst from (in addition to the catalyst from its own integrated device) can also be regenerated.

  Table 1 shows the results of the feasibility study for evaluating the device of FIG.

Despite the increase in feed rate from 4,770 to 5,406 m ³ / day (30 to 34 kbd), the reactor pressure drops by about 25 percent from 3344 to 2482 kPag (from 485 to 360 psig). This reduction in reactor pressure allows the refiner to maintain a relatively constant C ₅ + reformate yield despite increasing severity from 95 to 100 RON. Hydrogen production is also from 77 to 130 n. L. L. Increase to about ^-1 (from 435 to 733 scf / B) by about 70%.

  A catalyst regeneration facility can be used to regenerate spent catalyst from two or more reformers, thus achieving economies of scale, and (2) an existing continuous catalyst regeneration facility that has a dedicated continuous catalyst regeneration facility Somewhat moderate pressure drop and yield improvement can be achieved with much lower project investment compared to conversion.

It is a figure which shows the continuous moving bed reforming process constructed | assembled from the existing high pressure fixed bed reforming apparatus. Thick lines indicate new equipment and piping, and thin lines indicate existing equipment and piping.

Claims (17)

A method for converting a fixed bed catalytic reformer to a moving bed reactor operation comprising:
In a fixed bed catalytic reformer having at least one fixed bed catalytic reforming reactor, the at least one fixed bed reforming reactor is continuously connected to the catalyst inlet of the moving bed reactor of newly regenerated catalyst or Converting to a moving bed catalytic reforming reactor that allows for intermittent addition and continuous or intermittent removal of spent catalyst from the catalyst outlet of the moving bed reactor;
In order to continuously or intermittently charge fresh or regenerated catalyst into the continuous moving bed reactor via the catalyst inlet of the moving bed reactor, continuously or intermittently at the catalyst inlet. Adding equipment to supply the catalyst;
A waste catalyst recovery facility for collecting the waste catalyst from the catalyst outlet of the moving bed reactor and transferring the waste catalyst to a reforming catalyst regeneration facility that is not integrated with the reactor from which the catalyst is removed. Adding step;
Operating the moving bed reactor at a pressure effective to improve the quality and yield of the reformate compared to the quality and yield of the reformate product from the fixed bed unit prior to conversion. The step of:
A conversion method comprising the steps of continuously or intermittently removing the waste catalyst from the moving bed reactor; and transferring the waste catalyst to the non-integrated regeneration facility.   The regeneration facility is an on-site regeneration facility shared by a plurality of reformers, and the shared on-site regeneration facility continuously or intermittently receives the waste catalyst from the plurality of reformers, and The conversion method according to claim 1, wherein the catalyst is regenerated, and the regenerated catalyst is continuously or intermittently supplied to the plurality of reformers.   2. The conversion method according to claim 1, wherein the regeneration facility is an off-site regeneration facility adapted to regenerate a waste catalyst from a plurality of reformers.   The regeneration facility is a moving bed regenerator integrated with a second moving bed reformer, and the regeneration facility receives the catalyst from the moving bed reactor of the converted device after conversion. The conversion method according to claim 1, wherein the conversion method has the capability of enabling The fixed bed reformer includes a plurality of fixed bed reactors in a row, wherein the plurality of fixed bed reactors includes reformer feeds from one reactor to the next reactor in the row. Connected in series with the flow,
Each of the plurality of fixed bed reactors is converted to a moving bed reactor, the moving bed reactor forming a row, and the reformer charge from one reactor in the row to the next reactor. The conversion method according to claim 1, wherein the conversion method is connected in series with the flow of the reforming catalyst and the flow of the reforming catalyst.   6. The method of claim 5, wherein the catalyst flow in the reactor row is co-current with the reformer charge flow in the reactor row.   The conversion method according to claim 1, wherein the moving bed reactor is operated at a pressure lower than the pressure of the fixed bed reactor before the conversion after the conversion.   The fixed bed reactor is operated at a pressure of 1035 to 3800 kPag before conversion, the moving bed reactor is in the range of 345 to 2760 kPag after conversion and less than the pressure of the fixed bed reactor before conversion. The conversion method according to claim 7, wherein the conversion method is operated under pressure.   The conversion method according to claim 8, wherein the moving bed reactor is operated at a pressure of 690 to 2620 kPag after the conversion.   The conversion method according to claim 9, wherein the moving bed reactor is operated at a pressure of 1035 to 2415 kPag after the conversion.   8. The moving bed reactor is operated at a pressure equal to 20-60% lower than the pressure of 1035-3800 kPag where the fixed bed reactor was operated before the conversion after the conversion. Conversion method described in 1.   12. The moving bed reactor is operated at a pressure equal to 25-50% lower pressure after conversion than the pressure of 1035-3800 kPag where the fixed bed reactor was operated before conversion. Conversion method described in 1.   The method of claim 1, wherein the fresh or regenerated catalyst comprises one or more Group VIII noble metals on a refractory support.   The conversion method according to claim 1, wherein the fresh or regenerated catalyst includes a hydrogenation-dehydrogenation function and an acid function.   The method of claim 1, wherein the fresh or regenerated catalyst comprises platinum, tin, rhenium or combinations thereof on substantially spherical alumina support particles.   The method of claim 1, wherein the fresh or regenerated catalyst comprises platinum, platinum and tin, or platinum and rhenium on substantially spherical alumina support particles. The catalyst supply facility is operably connected to the moving bed catalytic reforming reactor,
The catalyst recovery facility is operably connected to the moving bed catalytic reforming reactor and the catalyst supply facility,
The catalyst recovery equipment and the moving bed catalytic reforming reactor can be operated in existing fixed bed equipment equipment including a reformed feed heater and reformed oil product recovery equipment maintained from the fixed bed equipment. The conversion method according to claim 1, further comprising:

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