KR101473135B1 - Process and apparatus for venting a catalyst cooler - Google Patents

Abstract

The method and apparatus herein provide a catalytic chiller with an exhaust port that communicates the fluidized gas to the lower chamber of the regenerator. At this time, the air used as the fluidizing gas can be consumed in the regenerator without promoting afterburn in the upper chamber.

Description

TECHNICAL FIELD [0001] The present invention relates to a method and apparatus for evacuating a catalyst cooler,

Priority claim of early international application

This application claims priority to U.S. Application No. 13 / 036,603 and U.S. Application No. 13 / 036,660, filed February 28, 2011, both of which are incorporated herein by reference.

Technical field

The field of the present invention is to regenerate the catalyst in a Fluid Catalytic Cracking (FCC) unit.

Fluid phase catalytic cracking (FCC) is a hydrocarbon conversion process accomplished by contacting a hydrocarbon in a fluidization reaction zone with a catalyst composed of finely divided particulate material. In contrast to hydrocracking, the reaction in catalytic cracking takes place in the absence of significant hydrogen or hydrogen consumption. When the decomposition reaction proceeds, a considerable amount of material containing a large amount of carbon, referred to as coke, is deposited on the catalyst. The high temperature regeneration process within the regenerator zone burns the coke from the catalyst. Wherein the coke-containing catalyst, referred to as the coked catalyst, is continuously removed from the reaction zone or is replaced by a coke-free catalyst from the regeneration zone. The fluidization of the catalyst particles by the various gas streams allows the catalyst to be transported between the reaction zone and the regeneration zone.

Conventional regenerators typically include a vessel having a coking catalyst inlet, a regenerating catalyst outlet and a combustion gas distributor for supplying air or other oxygen containing gas to the catalyst bed in the vessel. Before the gas exits the regenerator vessel, the cyclone separator separates the catalyst incorporated in the flue gas.

At present, many types of catalyst regenerators are used. Conventional bubbling bed regenerators typically have only one chamber in which air is bubbled through a dense catalyst bed. A coking catalyst is added, and the regenerated catalyst is taken out from the same dense catalyst bed. A relatively small amount of catalyst is incorporated into the combustion gas exiting the dense bed.

Two types of regenerators have two chambers. The two-stage bubbling bed has two chambers. A coking catalyst is added to the dense bed in the first upper chamber and is partially regenerated by air. The partially regenerated catalyst is transferred to a dense bed in the second lower chamber, and is completely regenerated by air. The completely regenerated catalyst is taken out from the second lower chamber.

Full catalyst regeneration can be performed in a dilute phase fast fluidized combustion regenerator. A coking catalyst is added to the lower chamber and fully regenerates the catalyst while being transported upward by air under fast fluidizing flow conditions. The regenerating catalyst is separated from the flue gas by the main separator when the regenerating catalyst and the flue gas enter the upper chamber portion from which they are separated from each other. Only a small proportion of the air added to the regenerative vessel is added to the upper chamber. US 4,197,189 and US 4,336,160 teach the riser combustion zone that the fast fluidizing flow conditions are maintained to cause complete combustion and there is no need for further combustion in the catalyst bed collected from the top of the riser.

The after burn is a phenomenon that occurs when the hot flue gas separated from the regenerated catalyst contains carbon monoxide, which is burned with carbon dioxide. The afterburning may be a risk factor in the upper separation chamber containing the hot flue gas separated from the catalyst, thereby providing a catalyst lean phase. In this catalytic lean phase, an insufficient catalyst acts as a heat sink to absorb the heat of combustion, thereby causing the surrounding equipment to be subjected to a potentially damaging high temperature and possibly creating an atmosphere that promotes the production of nitrogen oxides.

The catalyst cooler was used to cool the regenerated catalyst and to allow the regenerator and the reactor to operate under independent conditions. In the catalyst cooler, the hot regenerated catalyst is cooled by indirect heat exchange with water vaporized with steam. The steam is removed from the catalyst cooler for other uses, while the low temperature catalyst is returned to the regenerator. The air used to fluidize the catalyst in the catalyst cooler can be vented to the regenerator.

The background to the present invention is a catalyst cooler having an exhaust outlet communicating with the upper chamber of the regenerator vessel. The air that is fluidized in the catalyst cooler and exhausted to the upper chamber can provide an oxidant for the afterburning.

A method of efficiently utilizing air for fluidizing a high-temperature catalyst in a catalyst cooler for a regenerator is sought.

In a method embodiment, the present invention includes a catalyst regeneration method for regenerating a catalyst, comprising burning the coke from the catalyst in a combustor chamber of the regenerator vessel. The flue gas is separated from the catalyst in the separation vessel. The hot catalyst is transferred from the regenerator vessel to the catalyst cooler via the hot catalyst inlet. The high temperature catalyst from the regenerator vessel is cooled in the catalyst cooler. The catalyst is fluidized by air in the catalyst cooler. The low temperature catalyst is taken out of the catalyst cooler. Air is vented from the catalyst cooler to the regenerator vessel. The improvement of the present invention involves exhausting air from the catalyst cooler to the combustor chamber.

In another method embodiment, the invention includes a catalyst regeneration method for regenerating a catalyst, comprising burning the coke from the catalyst in a combustor chamber of the regenerator vessel. The regenerated catalyst is separated from the flue gas in the separation chamber of the regenerator vessel. The hot catalyst is transferred from the separation chamber via the hot catalyst inlet to the catalyst cooler. The catalyst from the regenerator vessel is cooled in the catalyst cooler. The catalyst in the catalyst cooler is fluidized by air. The low temperature catalyst is taken out of the catalyst cooler. The low temperature catalyst is delivered to the combustor chamber. Air is vented from the catalyst cooler to the regenerator vessel separately from the low temperature catalyst. The improvement of the present invention involves exhausting air from the catalyst cooler to the combustor chamber.

In another method embodiment, the present invention comprises a catalyst regeneration method for regenerating a catalyst, comprising transferring the coking catalyst and the combustion gas to a regenerator vessel. The coke is burned from the coking catalyst in the combustor chamber of the regenerator vessel. The catalyst is separated from the flue gas in the separation chamber. The hot catalyst is transferred from the regenerator vessel to the catalyst cooler via the hot catalyst inlet. The high temperature catalyst from the regenerator vessel is cooled in the catalyst cooler. The catalyst is fluidized by air in the catalyst cooler. The low temperature catalyst is taken out of the catalyst cooler. Air is vented from the catalyst cooler to the regenerator vessel separately from the low temperature catalyst and the high temperature catalyst inlet. The low temperature catalyst taken out of the catalyst cooler is transferred from the riser to the combustor chamber. The improvement of the present invention involves exhausting air from the exhaust to the combustor chamber.

In an apparatus embodiment, the invention includes a catalyst regenerator comprising an inlet for a catalyst and a combustion gas, and a regenerator vessel having a regeneration catalyst outlet, a cooler catalyst outlet, a flue gas outlet, an upper chamber and a lower chamber. A catalytic chiller is also included, wherein the catalytic chiller has a high temperature catalyst inlet in communication with the chiller catalyst outlet of the regenerator vessel. The catalyst cooler has a plurality of heat exchange tubes in the catalyst cooler for delivering the gas distributor, the exhaust, the cooler catalyst outlet and the heat exchange fluid. The exhaust pipe communicates the exhaust port with the regenerator vessel. The improvement of the present invention is that the exhaust pipe communicates the exhaust port with the lower chamber of the regenerator vessel.

In another device embodiment, the present invention includes a catalyst regenerator comprising a catalyst and an inlet for a combustion gas, a regenerated catalyst outlet, a cooler catalyst outlet, a flue gas outlet, a regenerator vessel having an upper chamber and a lower chamber. A catalytic chiller is also included, wherein the catalytic chiller has a high temperature catalyst inlet in communication with the chiller catalyst outlet of the regenerator vessel. The catalyst cooler has a gas distributor, an exhaust port spaced above the hot catalyst inlet, a cooler catalyst outlet, and a plurality of heat exchange tubes in the catalyst cooler for transferring the heat exchange fluid. The exhaust pipe communicates the exhaust port with the regenerator vessel. The improvement of the present invention is that the exhaust pipe communicates the exhaust port with the upper chamber of the regenerative vessel.

In another device embodiment, the present invention provides a catalyst comprising a catalyst in a combustor chamber and an inlet for the combustion gas, a regenerator vessel with a regenerator catalyst outlet in a separation chamber and a flue gas outlet, and a cooler catalyst outlet in a separation chamber Lt; / RTI > A catalytic chiller is also included, wherein the catalytic chiller has a high temperature catalyst inlet in communication with the chiller catalyst outlet of the regenerator vessel. The catalyst cooler has a plurality of heat exchange tubes in the catalyst cooler for delivering the exhaust, the cooler catalyst outlet, and the heat exchange fluid. The exhaust pipe communicates the exhaust port with the regenerator vessel. The improvement of the present invention is that the exhaust pipe communicates with the combustor chamber.

1 is a schematic diagram of an FCC unit of the present invention.

The inventors have found that exhausting air from the catalyst cooler to the lower chamber instead of the upper chamber of the regenerator minimizes the afterburning which may result in exhausting the catalyst cooler to the upper regenerator. By exhausting the air to the lower chamber, it becomes possible to consume air to burn the coke on the spent catalyst.

As shown in FIG. 1, the FCC unit 8 can be used in an FCC process. The hydrocarbon feedstock can be injected by the distributor 10 into the riser 20, which contacts the catalyst in the riser. Generally, the feedstock can be decomposed in the riser 20 in the presence of the catalyst to form a cracked product stream.

Conventional FCC feedstock is a suitable feed to riser 20. The most common conventional feedstock described above is "Vacuum Gas Oil " (VGO), which typically has a boiling range of 343 to 552 DEG C (650 DEG F to 1025 DEG F.) And is prepared by vacuum fractionation. In the present invention, heavier hydrocarbon feedstocks may also be used. Conventional FCC feedstock is vaporized and injected into the riser by distributor 10.

As shown in Fig. 1, the regenerated catalyst is transferred from the regenerator stand pipe 18 to the riser 20. In an embodiment, a lift gas, which may include an inert gas, such as steam, may be dispensed by the lift gas distributor 6 to lift the catalyst upward from the lower section 14 of the riser 20 have. The feed injected from the distributor 10 contacts the lifted fluidizing catalyst and moves upward in the riser 20 as the hydrocarbon feed decomposes into smaller hydrocarbon cracked products. The decomposition product and the spent catalyst enter the reactor vessel 70 and then exit from the top of the riser 20 through the riser outlet 72 and are passed through the cracked product vapor stream and a substantial amount of coke, Quot; catalyst " A stirring arm arrangement 74 provided at the end of the riser 20 can further improve the initial catalyst and cracked hydrocarbon separation by imparting a tangential velocity to the effluent catalyst and the cracked product vapor stream mixture. The stirring arm arrangement 74 is located in the upper portion of the separation chamber 76 and the stripping zone 78 is located in the lower portion of the separation chamber 76. The catalyst separated by the stirring arm arrangement 74 falls into the stripping zone 78.

The cracked product vapor stream comprising naphtha, light olefins, and some catalysts and cracked hydrocarbons may exit the separation chamber 76 through a gas conduit 80 in communication with the cyclone 82. Cyclone 82 can remove residual catalyst particles from the product vapor stream and reduce the particle concentration to very low levels. The product vapor stream may exit the upper portion of the reactor vessel 70 through the product outlet 84. The catalyst separated by the cyclone 82 returns to the reactor vessel 70 via a dip leg into dense bed 86 and the catalyst in the bed passes through the chamber opening 88 and into the stripping zone 78. [ . The stripping zone 78 removes hydrocarbons absorbed and entrained from the catalyst by countercurrent contact with an inert gas, such as steam, over an optional baffle 90. Steam can enter the stripping zone 78 via the distributor 92. The spent catalyst conduit 94 is regulated by a control valve to transfer the coked catalyst to the catalyst regenerator 30.

In addition, the spent catalyst recycle conduit (not shown) may transport some spent catalyst back to the riser 20 under the feed distributor configuration 10 without undergoing regeneration.

As shown in FIG. 1, the catalyst regenerator 30 receives a coking catalyst through the inlet 32 and typically combusts the coke from the surface of the catalyst particles by contact with an oxygen-containing gas. The oxygen-containing combustion gas enters the bottom of the regenerator 30 through the inlet 34 to the combustion gas distributor 36. The catalyst incorporated with the flue gas passes upward through the regenerator 30. The flue gas exits the regenerator through the flue gas outlet (38).

The catalyst regenerator 30 includes a regenerator vessel 40 that includes a lower chamber 42 and an upper chamber 44. The catalyst regenerator may be a two stage regenerator in which air is delivered to the upper first stage chamber 44 and the lower second stage chamber 42. In the two-stage regenerator, 20 to 40% by weight of air is transferred to the lower chamber. Oxygen depleted air from the lower chamber and the remainder of the total air delivered to the catalyst regenerator are transferred to the upper chamber. The spent catalyst is first transferred to the upper first stage chamber 44. Thereafter, the partially regenerated catalyst is guided downward into the second-stage chamber 42 to make contact with fresh air and to complete the regeneration process.

The catalyst regenerator 30 may also include a combustor regenerator as shown in FIG. In the combustor regenerator, the spent catalyst enters the lower chamber 42, which is referred to as the combustion chamber, in which the coke is burned from the catalyst and the catalyst and flue gas are separated from the lower chamber 42 And is transferred to the upper chamber 44. A main separator, such as a tee disengager 50, initially separates the catalyst from the flue gas. Before the flue gas exits the vessel through the flue gas outlet 38, a regenerator cyclone 52, 54 or other means separates the entrained catalyst particles from the flue gas rising. The combustion of coke from the catalyst particles raises the temperature of the catalyst. The separated catalyst is collected in dense bed 56 which is fluidized by air from distributor 58. The separated catalyst may escape from the regenerator vessel to the regenerator standpipe 18 via the regenerator catalyst outlet 16. The catalyst can be regulated by the control valve and guided to the lower section 14 of the riser 20 via the regenerator stand pipe 18.

The regenerated catalyst exiting the regenerator standpipe 18 will typically have a temperature in the range of 649 ° C to 760 ° C (1200 ° F to 1400 ° F). If air is used as the oxygen-containing gas, the ratio of dry air to regenerator may be 8 to 15 kg / kg coke. The hydrogen in the coke may be 4 to 8 wt%, and the sulfur in the coke may be 0.6 to 3.0 wt%.

At least one catalyst cooler (100) is provided for cooling the regenerated catalyst. In the combustor regenerator 30 the catalyst is transferred from the upper chamber 44 via the cooler catalyst outlet 102 to the catalyst cooler 100 via the hot catalyst conduit 104 and the hot catalyst inlet 106. A cooler catalyst outlet 102 is provided in the upper chamber so that the hot catalyst is withdrawn from the upper chamber 44 for delivery to the hot catalyst inlet 106. Although only one catalyst cooler is shown in FIG. 1, two or more catalyst coolers can be used.

The catalyst cooler 100 shown in Fig. 1 is a flow-through type cooler. A catalyst heat exchange tube 120 is located in the catalyst cooler 100 to cool the catalyst before the catalyst is taken out of the catalyst cooler 100 through the cooler catalyst outlet 102 to the low temperature catalyst pipe 108. By using the heat exchange tube 120, it is possible to recover and remove heat from the catalyst caused by the combustion of the coke in the regenerator vessel 40. Preferably, 50 to 250 heat exchange tubes (120), and more preferably 75 to 200 heat exchange tubes (120), are located in the catalyst cooler (100). Heat is typically removed from the catalyst to produce steam that can be used elsewhere in the refinery. The catalytic control valve 112 regulates the amount of catalyst exiting the cooler catalyst outlet 110 through the low temperature catalyst pipe 108 and thereby entering the catalyst cooler 100 from the regenerator vessel 40, Thereby controlling the temperature in the regenerator vessel 40.

The regenerated catalyst entering the catalyst cooler 100 through the hot catalyst inlet 106 is in contact with the catalyst heat exchange tube 120. The catalyst moves down through the catalyst cooler 100 to the lower portion of the cooler and exits through the cooler catalyst outlet 110 below the high temperature catalyst inlet 106.

The catalyst cooler 100 typically has a "low temperature wall ". The term "low temperature wall " means that the metal shell 128 of the cooler 100 is coated with an internal heat-resistant refractory lining. However, in one embodiment, metal enclosure 128 may be free of adiabatic refractory lining, in which case it is considered to have a "hot wall ". Additionally, a portion of the cooler 100 may be further lined with a wear resistant coating. The metal shell 128 of the cooler 100 may be formed of stainless steel.

The catalyst cooler 100 includes an inlet manifold 114 and an outlet manifold 130. The lower tube sheet 118 can be bolted between the flange at the upper end of the lower head 122 in the cooler 100 and the lower flange at the lower end of the outlet manifold 130. [ The upper tube sheet 132 may be bolted between a flange at the upper end of the outlet manifold 130 and a lower end of the enclosure 128 defining the cooler 100. A grate 140 extends horizontally in the catalyst cooler 100 to reinforce the vertically aligned heat exchange tubes 120 in the catalyst cooler 100. The grate 140 may form an opening through which the heat exchange tubes extend. Each catalyst cooler 100 may have at least two layers of grate 140. The bristles are fixed to the heat exchange tubes 120 and to each other by vertical support rods, which may be formed of the same material as the heat exchange tubes 120. The grate 140 and the heat exchange tube 120 may be thermally expanded together without being joined if desired.

In an embodiment, the boiler feed water is a heat exchange fluid, but other types of heat exchange fluids are also contemplated, including water containing additives that affect the boiling point of the fluid. The boiler feed water enters the inlet manifold 114 through the cooling medium nozzles 116 at or near the bottom of the catalyst cooler 100. In an embodiment, the inlet manifold 114 is formed between the lower tube sheet 118 and the bottom head 122 of the cooler. Preferably, the catalyst heat exchange tubes 120 have inlets and outlets at or near the bottom of the cooler 100. Preferably, the catalytic heat exchange tubes 120 are bayonet style tubes, each comprising an inner tube 124 and an outer tube 126. The inner tube 124 extends through this length into the majority of the length of the outer tube 126. The inner tube 124 of the heat exchange tube 120 is secured to the lower tube sheet 118 and extends through the lower tube sheet 118 and protrudes from the lower tube sheet 118. The inlet of the inner tube 124 is in fluid communication with the inlet manifold 114. The boiler feed water entering the inlet manifold 114 is directed upwardly to the inner tube 124 of the heat exchange tube 120. The boiler feedwater moves upward along the length of the inner tube 124 and exits the outlet of the inner tube 124. The boiler feedwater then reverses direction and flows downward to the outer tube 126 surrounding the inner tube 124. The catalyst contacts the outer surface of the outer tube 126 of the catalyst heat exchange tube 120.

Heat from the catalyst is indirectly exchanged with the boiler feedwater in the outer tube 126. Indirect heat exchange raises the temperature of the boiler feedwater in the outer tube 126 and converts at least a portion of the boiler feedwater to steam. This contact with the outer tube 126 lowers the temperature of the catalyst falling in the catalyst cooler 100. The steam from the outer tube 126 and the heated boiler feed water flow out of the outlet of the outer tube 126 and out of the outlet manifold 120 formed in the catalytic cooler 100 between the upper tube sheet 132 and the lower tube sheet 118 130). The outer tube 126 is secured to the upper tube sheet 132, extends through the upper tube sheet, and protrudes from the upper tube sheet. The outlet of the outer tube 126 is in fluid communication with the outlet manifold 130. The fluid in the outlet manifold 130 is then transferred from the catalyst cooler 100 through the nozzle 136, possibly to the circulation drum, where the steam and heated boiler feed liquid are separated. The low temperature catalyst then flows out of the catalyst cooler 100 to the low temperature catalyst pipe 108 through the cooler catalyst outlet 110 and the low temperature catalyst pipe passes the catalyst cooler through the catalyst recirculation valve 112 to the regenerator vessel 40, . In one aspect, the low temperature catalyst pipe 108 is in communication with the riser 150. A fluidizing gas is supplied to the riser 150 to lift and transport the catalyst from the riser 150 to the regenerator vessel 40 and preferably to the lower chamber 42 of the regenerator 30. The catalyst distributor 152 may distribute the catalyst to the regenerator vessel 40 through the openings.

The fluidizing gas is also directed downward in the catalyst cooler 100 by a distributor 138 with nozzles. Preferably, the distributor 138 is located above the heat exchanger tube 120, so that the nozzle directs the fluidizing gas downwards in the catalyst cooler 100. Gas, such as air, is used to fluidize the catalyst particles entering the catalyst cooler 100 through the hot catalyst inlet 106. The flow rate of the fluidizing gas must be high enough to achieve fluidization of the catalyst. The fluidizing gas used in the catalyst cooler 100 enhances the heat transfer between the catalyst and the heat exchange tube 120 by creating turbulence that enhances the heat transfer coefficient between the catalyst and the heat exchange tube 120. Two schemes for controlling the temperature of the circulated catalyst are controlled by the catalytic recirculation valve 112 to control the amount of catalyst flowing through the catalyst cooler 100 or to the amount of fluidization that is distributed to the catalyst cooler 100 via the distributor 138 To change the gas velocity.

At the top of the catalyst cooler 100 is provided an exhaust port 144 through which the fluidized gas exits the catalyst cooler. The exhaust pipe 146 communicates the exhaust port 144 with the regenerator vessel 40 through the exhaust gas inlet 154. In one aspect, the exhaust duct 146 communicates with the lower chamber 42 of the regenerator vessel 40. The air is exhausted to the lower chamber 42 separately from the low temperature catalyst exiting the low temperature catalyst pipe 108 and the high temperature catalyst entering through the high temperature catalyst inlet 106. As a result, the air exiting the catalyst cooler is transferred to the lower chamber 42 of the regenerator, and the air in this lower chamber can be consumed in the combustion of the coke from the internally consumed catalyst. Exhausting the fluidized air to the lower chamber 42 is improved compared to venting air to the upper chamber 44 because air does not promote afterburning in the upper chamber 44, ) In the combustion of coke. Exhaust air in the exhaust pipe 146 is directed downward after being exhausted from the exhaust port 144 and before entering the lower chamber 42 of the regenerator vessel 40. In one embodiment, the exhaust pipe directs the fluidized gas upwardly from the catalyst cooler 100, then laterally, and then downwardly, and then laterally into the lower chamber 42 of the regenerator vessel 40 . As a result, the exhaust gas inlet is disposed at a lower level than the exhaust port 144.

A separator 148 may be disposed between the high temperature catalyst inlet and the exhaust 144 in the upper portion of the gas distributor 138 in the catalyst cooler 100. The separation portion 148 provides a space in which the catalyst can be separated from the fluidizing gas before exiting the exhaust port 144. Heat exchange tube 120 is disposed below separator 148. In one aspect, the vent 144 is spaced above the catalyst inlet 106 to provide a separator 148.

The heat exchange tube may be formed of a chromium-molybdenum-iron alloy because the alloy is resistant to corrosion due to trace amounts of chloride in the boiler feed water when the boiler feed water is used as the heat exchange liquid to be.

The zeolite molecular sieve used in conventional FCC processes has a large average pore size and is suitable for the present invention. The molecular sieve having a large pore size has more than ten atomic rings, typically large pores with an opening larger than 0.7 nm in effective diameter formed by the 12-atom ring. Suitable large pore molecular sieves include synthetic zeolites such as X-type zeolite and Y-type zeolite, mordenite and faujasite. Y-type zeolite with a low rare earth content is preferred. The lower rare earth content represents less than or equal to 1.0 wt% rare earth oxide relative to the zeolite portion of the catalyst. A catalyst additive may be added to the catalyst component during the process. To increase the production of light olefins, molecular sieves of intermediate pore size such as MFI with openings of 0.7 nm or less can be mixed with large pore molecular sieves. In some cases only midsuper pore size molecular sieves can be used if the feed to the riser is an FCC product portion such as a naphtha stream.

The riser 20 can operate at a catalyst to oil ratio of 4 to 12, preferably 4 to 10. [ The inert gas to the riser 20 may be from 1 to 15 wt%, preferably from 4 to 12 wt%, of the hydrocarbon feed. Prior to contacting the catalyst, the hydrocarbon feed may have a temperature in the range of 149 ° C to 427 ° C (300 ° F to 800 ° F), preferably in the range of 204 ° C to 288 ° C (400 ° F to 550 ° F). The riser 20 is capable of operating in a temperature range of 427 ° C to 649 ° C (800 ° F to 1200 ° F), preferably 482 ° to 593 ° C (900 ° F to 1100 ° F). The pressure in the riser 20 may be from 69 to 241 kPa (gauge) (10 to 35 psig), preferably 103 kPa (gauge) (15 psig).

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of the present invention, including the best mode known to the inventor for practicing the present invention, are described herein. The presented embodiments are to be understood as illustrative only and are not to be construed as limiting the scope of the invention.

Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent. The foregoing preferred specific embodiments are accordingly to be considered exemplary only and are not intended to limit the remainder of this disclosure in any way.

In the foregoing, all temperatures are expressed in degrees Celsius, unless otherwise indicated, and all parts and percentages are by weight.

From the foregoing description, those skilled in the art will readily be able to acquire essential features of the present invention, and various modifications and alterations of the present invention can be made without departing from the spirit and scope of the present invention.

Claims (10)

As a catalyst regenerator,
A regenerator vessel having an inlet for catalyst and combustion gas, a regeneration catalyst outlet, a cooler catalyst outlet and a flue gas outlet;
A catalyst cooler having a gas distributor, an exhaust, a cooler catalyst outlet, and a plurality of heat exchange tubes in the catalyst cooler for delivering heat exchange fluid; and a catalyst cooler having a high temperature catalyst inlet communicating with the cooler catalyst outlet of the regenerator vessel. And
An exhaust pipe communicating the exhaust port with the regenerator vessel,
≪ / RTI > The catalyst regenerator according to claim 1, further comprising a header portion between the high temperature catalyst inlet and the exhaust port in the catalyst cooler. 3. The catalyst regenerator of claim 2, wherein the heat exchange tube is below the header portion. 2. The catalyst regenerator of claim 1, wherein the regenerator vessel has a combustor chamber and a separation chamber, and the cooler catalyst outlet is provided in the separation chamber. 5. The catalyst regenerator according to claim 4, wherein the exhaust pipe extends into the separation chamber. 5. The catalyst regenerator of claim 4, wherein the exhaust duct extends into the combustor chamber. A catalyst regeneration method for regenerating a catalyst,
Burning the coke from the catalyst in the regenerator vessel;
Transferring the high temperature catalyst from the regenerator vessel to the catalyst cooler through the high temperature catalyst inlet;
Cooling the high temperature catalyst from the regenerator vessel in the catalyst cooler;
Fluidizing the catalyst using air in the catalyst cooler;
Withdrawing the low temperature catalyst from the catalyst cooler; And
Separately from the low temperature catalyst and the high temperature catalyst inlet, venting air from the catalyst cooler to the regenerator vessel
≪ / RTI > 8. The apparatus of claim 7, wherein the regenerative vessel has a combustor chamber and a separation chamber, wherein the high temperature catalyst is withdrawn from the separation chamber for transfer to the high temperature catalyst inlet and air is exhausted to the separation chamber. Way. 8. The catalyst of claim 7, wherein the regenerator vessel has a combustor chamber and a separation chamber, wherein the high temperature catalyst is withdrawn from the separation chamber for transfer to the hot catalyst inlet and air is exhausted to the combustor chamber. Playback method. 10. The method of claim 9, wherein the evacuated air is directed upward and then downwardly prior to entering the combustor chamber after being exhausted from the vent.

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