TW200835784A - A process for heating a hydrocarbon stream entering a reaction zone with a heater convection section - Google Patents

Abstract

An exemplary process can include passing a hydrocarbon stream through a reforming unit (100). The reforming unit (100) may include a heater (210), which in turn generally includes a convection section (230) and a radiant section (250), and a plurality of reforming reaction zones. Generally, the hydrocarbon stream is heated in the convection section (230) for reacting in one of the reforming reaction zones (412) to which the hydrocarbon stream is sent and the hydrocarbon stream is heated in the radiant section (250) of the heater for reacting in the other reforming reaction zone (418) to which the hydrocarbon stream is sent.

Description

200835784 IX. DESCRIPTION OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The field of the invention is the heating of a hydrocarbon stream entering a reaction zone. [Prior Art] The exothermic or endothermic hydrocarbon conversion process can be used in the petroleum refining or petrochemical manufacturing industry. An exemplary smoke conversion process for improving the burnt quality of tobacco raw materials is catalytic recombination, wherein the main product of the recombination is automotive gasoline or petrochemical aromatics. Catalytic recombination techniques are well known to us and a brief implementation is provided below. In general, in catalytic recombination, the feedstock is combined with a recycle stream comprising hydrogen to form a feed stream, commonly referred to as a combined feed stream, and the combined feed stream is contacted with the catalyst in the reaction zone. A common raw material for catalytic recombination is called naphtha and has 82.石油 (180〇F) initial boiling point and 2〇; rc (4〇〇τ) final boiling petroleum fraction. Catalytic recombination processes are particularly useful for treating straight run naphtha consisting of relatively high concentrations of naphthenes and substantially linear alkanes' which are readily aromatized via dehydrogenation and/or cyclization reactions. Recombination can be defined as dehydrogenation of cyclohexane and dehydrogenation isomerization of alkylcyclopentane to obtain dehydrogenation of aromatics and alkanes to obtain dehydrocyclization of olefins, alkanes and dilute hydrocarbons. Isomerization of a group, a normal alkane, or isomerization of an alkylcycloalkane to obtain a total effect of cyclohexane, isomerization of a substituted aromatic, and chlorination of an alkane. Further information on methods of recombination can be found in, for example, U.S. Patent No. 4,119,526 (Peters et al.); 4,409, 〇95 (peters); and 4,44,626 (winter et al.). The catalytic recombination reaction is usually carried out in the presence of catalyst particles, which include - or a plurality of Dichu (leg c 8 · iG) metal (eg, turn, 铱, record, put) and dentate and A combination of porous supports such as refractory inorganic oxides.

In a common form, the recombination process can use catalyst particles in several reaction zones interconnected in a stream configuration. There may be many reaction zones, but usually the number of reaction zones is 3, 4 or 5. Because recombination reactions typically occur at elevated temperatures and are generally endothermic, each reaction zone is typically associated with one or more heating zones that heat the reactants to the desired reaction temperature. A common method for flowing through the column heating and reaction zones in the 3 reactor catalytic reforming process due to these considerations is as follows. The naphtha-containing feedstock can be combined with a hydrogen-containing recycle gas to form a combined feed stream of a tangible over-combined feed heat exchanger. In the combined feed heat exchange, the combined feed can be heated by exchanging heat with the effluent of the third reactor. However, the heating of the combined feed stream occurring in the combined feed heat exchanger is generally insufficient to heat the combined feed stream to the desired inlet temperature of the first reactor. Thus, the combined feed stream typically requires compensating heating after exiting the combined feed heat exchanger and before entering the first reactor. This compensating heating occurs in a heater, commonly referred to as a feed heater, which heats the combined feed stream to the desired inlet temperature of the first reactor. The combined feed can then be passed to the first reactor and through the first reactor. Due to the endothermic recombination reaction occurring in the first reactor, the temperature of the effluent of the first reactor typically drops to not only lower than the temperature of the combined feed in the first reactor, but more importantly lower than the second reaction. The required inlet temperature for the unit. Thus, the effluent of the first reactor can pass through another heater, 126304.doc 200835784. The heater is commonly referred to as a first intermediate heater and it can heat the first reactor effluent to the second reactor Required inlet temperature. After exiting the first intermediate heater, the first reactor effluent typically enters the second reactor. As in the first reactor, the endothermic reaction causes the temperature to drop again on the reactor. Typically, however, because the reaction occurring in the second reactor typically produces less endotherm than the reaction occurring in the first reactor, the temperature drop on the second reactor is typically lower than the first reaction at 10 The temperature on the device drops. Although the temperature drop is slightly less in the second reactor, the effluent from the second reactor is still at a lower temperature than the desired inlet temperature of the third reactor. Thus, the effluent from the second reactor can pass through another heater, commonly referred to as a second intermediate heater, and can then pass to the third reactor. In the second reactor, the endothermic reaction causes the temperature to drop again, since the temperature drop on the second reactor is generally lower than the temperature drop on the first reactor, the temperature drop is usually lower than in the first reactor. The temperature of the second reactor is lowered. The effluent of the third reactor can be passed to the previously mentioned, and the stone feed father can be exchanged, wherein the effluent of the third reactor can be cooled by exchanging heat with the combined feed stream. • In general, it is also known that recombination units can operate at different feed inlet temperatures for each of the reactors. In general, the unit has a column of 3 pairs, 4 pairs or 5 pairs of heaters and a reactor containing a catalyst bed (preferably a fixed or moving bed), but many different possible combinations of different inlet temperatures are formed (this , often referred to as the temperature distribution of the unit. Perhaps the best choice for the 3 reactor unit is that if the inlet temperatures of all three reactors are the same, then the temperature distribution is 126304.doc 200835784 is often referred to as flat. Otherwise, the reactors can be operated with a non-flat or skewed reactor inlet temperature profile. For example, if the inlet temperature of the first reactor is lower than the inlet temperature of the second reactor, and the inlet temperature of the second reactor is lower than the inlet temperature of the third reactor, the reactor inlet temperature is usually The distribution is called a step-up distribution. If the first inlet temperature is greater than the second inlet temperature & the second inlet temperature is greater than the third inlet temperature, then the distribution is generally referred to as a descending distribution. If the second inlet temperature is greater than the first and third inlet temperatures' then the distribution may be referred to as a hill shape. If the second inlet temperature is lower than the second and second inlet temperatures, the distribution may be referred to as a valley shape. The most common reason for operating the inlet temperature profile of a non-flat (i.e., skewed) reactor is to distribute the desired heat load among the heaters in the heater_reactor column. Ideally, all heaters individually transfer heat at approximately the same percentage of their individual design load. The heater load is referred to as "equalization" when each heater is operated with a design load of the same fraction of the design load of the other heaters in operation of any other heater in the column. When heated, it should not be operated above its design load, ie the percentage should normally be less than or equal to (10)%. If some operational variables (such as raw material quality or throughput) are significantly different from their design values or if the flow rate is uneven or mechanically asked; IP Mo & q ^ n ^ „ 鸠V-induced reaction state effect is significantly reduced to its expected performance The following 'then flat distribution may cause the operating load of the heater in this column to be unbalanced. 3 In the commercial company's reorganization method, try to use the skew reactor population temperature to balance the heater load's $ming>, +, and two conditions. Ming is described in the article by Rlchard Lee, whose title 126304.doc -11 - 200835784 is "Reforming Processes, Maximizing Profitability", edited by John J. McKetta and by Marcel Dekker, Inc., New York at 199 Λ Beginning on page 15 of Encyclopedia of Chemical Processing and Da/gn, Volume 47. In the example of Lee et al., a valley-like distribution of reactor inlet temperatures is recommended, with inlets of reactors 1 and 2 in parallel. The temperature is the same and greater than the inlet temperature of the reactor 3, the inlet temperature of the reactor 3 is lower than the inlet temperature of the reactor 4. The inlet temperature of the reactor 4 can be the same as the inlet temperature of the reactors 1 and 2 or The inlet temperature of reactors 1 and 2. The maximum difference between the inlet temperature of reactors 1, 2 and 4 and the inlet temperature of reactor 3 is 14 ° C (26 ° F). The article by Lee et al. It is expected that when performing an equal (ie, flat) reactor inlet temperature profile versus performing a staggered (ie, skewed) reactor inlet temperature profile, the difference between the gasoline-based products (C5 + yield) does not exceed the feed. 0.5%. The reprocessing furnace may comprise a plurality of units, wherein the feed to the reactor may be heated in the radiant zone of the unit, and the steam is typically produced in the convection zone of the heater. In general, the investment cost of the heater typically exceeds the unit. 20% of the cost. Because the feed can be heated in the radiant zone of the heater, a significant amount of combustion fuel (eg, 30% fuel) may actually be used to generate steam rather than heat processing the feed. Multiple heat entering the process reduces the cost of the heater and fuel.

U.S. Patent No. 6,1,6,696 to David Fecteau and Kenneth Peters discloses the possibility of removing the heater in the recombination unit. The feed is heated and vaporized in a combined feed exchanger and fed directly into the first reactor at a relatively low temperature. The combined feed exchanger outlet temperature can be below 482 ° C (900 T:). If the total load is 126304.doc -12· 200835784 > ^ load is quirky and the first - heater load is compared with other heaters: and no: balance, the relative low temperature at the exit of the combined feed exchanger may be followed by Higher reaction temperature requirements for the reactor. And typically, it would be necessary to increase the feed temperature above the temperature of the combined feed exchanger outlet to keep the subsequent reactor population temperature low without increasing catalyst loading. It may also be desirable to skew the inlet temperature of the reactor to equalize the thermal load requirements of each heater unit.

Information Disclosure The recombination method of two moving bed reaction zones is preferably not heated between the combined feed exchanger and the (iv) reaction zone. U.S. Patent No. 6,H)M96 is hereby incorporated by reference in its entirety. SUMMARY OF THE INVENTION As used above, U.S. Patent No. 6,1,6,696 discloses a use. An exemplary method can include passing a hydrocarbon stream through a recombination unit. The recombination unit can include a heater and a plurality of recombination reaction zones, including a pair of flow zones and a radiation zone. Generally, the hydrocarbon stream is heated in the convection = to react in one of the recombination reaction zones to which the hydrocarbon stream is passed and to heat the hydrocarbon stream in the radiant zone of the heater so that The reaction is carried out in another recombination reaction zone where the hydrocarbon stream is passed. Another exemplary recombination method can include delivering a stream comprising hydrocarbons via a recombination unit. The recombination unit can include at least one heater and a plurality of recombination reaction zones. In general, the at least one heater includes a pair of flow zones and a radiation zone, wherein at least 9% of the heat transferred from the at least one heater to the hydrocarbon stream entering one of the recombination reaction zones is from At least one 126304.doc -13- 200835784 one or more convection zones of the heater. An exemplary refinery or petrochemical manufacturing facility can include a recombination unit. Typically, the recombination unit includes at least one heater including a pair of flow zones and a radiation zone. The convection section may include at least one convection tube having an inlet and an outlet, and the radiant section includes a burner and at least one radiant tube having an inlet and an outlet. The recombination unit may further comprise a plurality of recombination reaction zones in tandem form, wherein each reaction zone has an inlet and an outlet. In general, the first reaction zone inlet is for receiving a hydrocarbon stream from the outlet of the convection tube and the second reaction zone inlet is for receiving a hydrocarbon stream from the outlet of the radiant tube. Yet another exemplary method can include passing a hydrocarbon stream through a recombination unit. The recombining unit can include a heater and a plurality of recombination reactors, which in turn can include a pair of flow zones and a radiation zone. In general, the hydrocarbon stream is heated only in the convection zone of the heater prior to entering one of the recombination reactors such as helium without heating in the radiant zone. Another exemplary method can include operating a heater including a pair of flow zones and a radiant zone; operating a plurality of reaction zones in series; passing a hydrocarbon stream through at least one convection tube directly into the inlet of one of the zones And passing the hydrocarbon stream through at least one radiant tube directly into the inlet of another zone. The convection zone can include at least one convection tube having an inlet and an outlet and the radiant zone can include at least one radiant tube having an inlet and an outlet. In addition, each reaction zone may have an inlet. It is desirable to use one or more convection zones of the heater to heat the feed to one of the reactors and set the inlet temperature of the reactor, possibly replacing the heater zone with a convection zone or a radiant zone of the furnace. This reduces investment costs and catalyst costs while reducing fuel and exhaust streams, thereby reducing emissions from the unit (e.g., C〇2, SOx, NOx). Moreover, the convective zone and the skewed temperature distribution allow the heat load to be transferred from the front end to the end. Therefore, the size of the furnace can be standardized to reduce capital costs. In addition, this configuration can achieve an increase in yield, such as an increase of 0.1%. Moreover, embodiments herein can provide a ratio of heater radiation zone to reaction zone of less than 1:1, such as 34 or 2:3. [Embodiment] As used herein, the term "hydrocarbon stream" may include various hydrocarbon molecules (such as linear, branched or cyclic alkanes, alkenes, diolefins, and alkynes) and (as appropriate) other materials (such as gases). A stream of (e.g., hydrogen) or impurities (such as heavy metals). ‘but as long as after the reaction

The number of non-carbon atoms in the hydrocarbon molecule. The plume can be subjected to a reaction (eg, a recombination reaction), but a small amount of smoke present in the stream can still be referred to as a hydrocarbon stream.

W milk T exits from the heater to reach the reaction zone.

Convective heat is received by, for example, 35-126304.doc -15- 200835784 65% (for blocked tubes) or 45_65% (for the blocked tube), which is usually released by the heater and is mainly burned by the fire and dance. The area of the heater for the relatively clean heat of the tube. 3) As used herein, the term "convection area" generally refers to the gas that is burned by the heater primarily by convection and light heat transfer. Released: 10-45% of the heater area. Typically, the heat of ^(10) is lost via the discharge port, so typically no more than 93% of the radiation and convection zones released by the fuel are released. …,in

As used herein, the term "transportation with respect to fluids" may mean that it will be produced.

The body is moved to another location by means of sending or compressing or by using gravity. W. . As used herein, the term "heater" may include a furnace 'feed heating or a mid-door heater. The heater may include at least one burner and may include at least one radiant zone, at least one convection zone, or a combination of at least one radiant zone and at least one convection zone. DETAILED DESCRIPTION OF THE INVENTION As generally described, the embodiments disclosed herein are applicable to a variety of reaction systems having a plurality of reactors, such as various hydrocarbon conversion processes, including their exothermic and endothermic processes. For example, embodiments of the present invention are applicable to a heat release process using multiple reaction zones where a temperature rise profile would be required. The money embodiment disclosed herein is preferably applicable to an endothermic recombination method. The hydrocarbon feedstock typically fed to the recombination process includes naphthenes and alkanes having boiling points in the gasoline range. In most cases, the sputum can also be found in the 'known but the better feed is the naphtha composed mainly of naphthenes and alkanes. The best types include straight-run gasoline, natural gasoline, synthetic gasoline and 126304.doc •16- 200835784

analog. As an alternative embodiment, feeding pyrolysis gasoline or catalytically cracked gasoline or partially recombined naphtha is often advantageous. 1 A mixture of straight and pyrolysis gasoline naphtha can be used to gain an advantage. The gasoline-based naphtha feed may be a full (four) gasoline with a 4G·hunting (sakisaki) and a (four) point in the range of 16〇_(320-428T) or a selected crane. The museum can usually be a high-fossil point that is often called heavy naphtha. For example, the point is 100-200 ° C (212-392 ^ 1 ^ naphtha. In some cases, 'feeding A pure di- or hydrocarbon mixture recovered from a self-extracting unit of a person to be converted into an aromatics (for example, from a raffinate of aromatic extraction or a linear alkane) = = advantageous. In some other cases, the raw material may also contain Light hydrocarbons having 丨5 carbon atoms, but because these light hydrocarbons are not easily reconstituted into aromatic hydrocarbons, the light hydrocarbons that enter with the feedstock are minimized. One can be disclosed herein. Exemplary feedstocks which produce such conversions generally comprise a stream which may be a naphtha comprising components expressed in weight percent based on the total weight of rhodium in the stream and disclosed in Table 1: Table 1 Q or lower carbon array parts: no more than 0.5% no more than 4% ^6 no more than 30% C7 10-50% Cg 20-50% c9 not exceeding 25% Ci〇 no more than 15% Cu or higher carbon array no more than 2% 126304.doc 200835784 In general, the combined feed stream or hydrocarbon feedstock (if hydrogen is not supplied with the hydrocarbon feedstock) is typically 65- Enter the heat exchanger at a temperature of 177 ° C (150-3 50 ° F) and more typically 93-121 ° C (200-250 ° F). Since hydrogen is usually supplied with hydrocarbon feedstock, it can be used in this paper. This heat exchanger is referred to as a combined feed heat exchanger, even if hydrogen is not supplied with the hydrocarbon feedstock. In general, the combined feed heat exchanger transfers heat from the final recycle reactor discharge stream to the combination. A feed stream to heat the combined feed stream. Preferably, the combined feed heat exchanger is an indirect (rather than a direct) heat exchanger to prevent valuable recombination products and combined feeds in the final reactor effluent Mixing and thus recycling to the recombination reactor, at which point the quality of the recombination may be degraded. Although the combined feed stream and the final reactor effluent stream in the combined feed heat exchanger may be in the same direction, reverse Flow, mixed flow or cross flow, but flow pattern Preferably, the countercurrent flow means that the combined feed stream contacts one end of the heat exchange surface of the combined feed heat exchanger (ie, the cold end) at its coldest temperature, and the final reactor discharge stream is also at its maximum Contacting the cold end of the heat exchange surface at cold temperatures. Thus, the final reactor effluent stream exchanges heat with the combined feed stream which is also at the coldest temperature in the heat exchanger at its coldest temperature in the heat exchanger. At the other end of the combined feed heat exchanger surface (ie, the hot end), the final reactor effluent stream and the combined feed stream contact the hot end of the heat exchange surface at its hottest temperature in the heat exchanger and Thereby exchange heat. Between the cold end and the hot end of the heat exchange surface, the final reactor effluent stream and the combined feed stream flow in substantially opposite directions such that generally at any point along the heat transfer surface, the temperature of the final reactor effluent stream High, combined with the final 126304.doc -18 - 200835784 Reactor vent stream exchange heat The higher the temperature of the feed stream. For further information on flow patterns in heat exchangers, see, for example, Perry's Chemical Engineers' Handbook, edited by Robert H. Perry et al., McGraw-Hill Book Company, New York, 1984, No. 10, sixth edition Pp. 24-10-31, and the references are incorporated herein. In general, the combined feed heat exchanger is typically below 56 ° C (10 ° F), preferably below 33 ° C (60 ° F) and more preferably below 28 ° C (50 ° F) The hot end is close to the value operation. As used herein, the term "hot end approach value" is defined as a heat exchanger based on the exchange of heat between the last reactor effluent stream and the cooler combined feed stream, where T1 is the last reactor effluent stream. The inlet temperature, T2 is the outlet temperature of the final reactor effluent stream, t1 is the inlet temperature of the combined feed stream and t2 is the outlet temperature of the combined feed stream. As used herein, for the countercurrent heat exchanger, "heat The end proximity value is defined as the difference between T1 and t2. In general, the smaller the hot end approach value, the higher the degree of heat exchange between the final reactor effluent and the combined feed stream. Although a shell and tube heat exchanger can be used, another possibility is a plate type heat exchanger. Panel exchangers are well known and commercially available in a number of different and unique forms, such as spiral, plate and frame, welded plate fin and plate fin tube. Plate exchangers are generally described in Perry's Chemical Engineers' Handbook, edited by R. H. Perry et al., and published by McGraw Hill Book Company, New York, 1984, pages 11-21 to 11-23, sixth edition. . In one embodiment, the combined feed stream can exit the combined feed heat exchanger at 399-516 ° C (750-960 ° F) to enter at least one heater (or 126304.doc -19- 200835784

Brother-heater) - or multiple convection zones. Typically, the feed stream enters the convection zone at the top portion of the convection zone where the exhaust gas is at its coldest temperature and is centered at the lower portion of the convection zone where the exhaust gas is at its hottest temperature. Alternatively, the feed stream may exit the convection zone at a lower portion of the convection zone where the exhaust gas is at its hottest temperature and exit at a higher portion of the convection zone where the exhaust gas is at its coldest temperature. Or the 'feed stream' can enter and exit at the top or bottom of the convection zone. The temperature of the combined feed stream leaving the convection zone (also the inlet temperature of the first reaction zone) is typically 482-54n: (_.1()2"f, preferably 518_538. 〇 (965·1000 °F) 益处 The benefit of the embodiment of the invention is the flexibility to control the temperature at the outlet of the convection zone. Conversely, control of product quality can be achieved by adjusting the temperature of the remaining reaction zone population. In the U case where independent temperature control of the first reaction zone is required, the control of the convection zone processing outlet temperature can be achieved by combining the feed exchanger with a hot side or a cold side bypass design. The final reactor effluent stream or a portion of the combined feed stream can bypass the combined feed exchanger. Alternatively, control can be achieved by using a small hot side bypass on the combined feed heat exchanger to slightly regulate excess air into the heater by combining with the fine control. The invention is particularly applicable to catalytic recombination of hydrocarbons in a reforming reaction system having at least two catalytic reaction zones, wherein at least a portion of the reactant stream and at least a portion of the catalyst particles are continuously passed through the reaction zone. Reaction systems with multiple zones typically take one of two forms: side-by-side or stacked. In the side-by-side configuration, a plurality of independent reaction vessels (each including a reaction zone) may be placed along the sides of each other. In a stacked configuration, a common reaction vessel may have 126304.doc -20-200835784 containing multiple reaction zones that are placed on top of each other independently, although the reaction zone may include many configurations of hydrocarbon streams (such as upward flow and cross flow) , but the most frequent downward flow,

The screen may have a nominal inner (four) facet that is lower than the cross section of the outer screen, the outer

The outer screen and the inner screen may be cylindrical, but they may take on any suitable shape, such as a triangle, square, rectangle or diamond, depending on a number of design, manufacturing, and technical considerations. For example, a common outer screen is not a continuous cylindrical screen, but instead a configuration of a separate elliptical tubular screen (referred to as a scallop) that can be placed around the inner wall of the reaction vessel. The inner screen is typically a perforated center tube that is covered by a screen around the outer circumference. An exemplary reaction vessel having a stacked reaction zone and which can be used to practice the invention is shown in U.S. Patent Nos. 3,706,536 (Greenwood et al.) and 5,130,1,6 (Koves et al.), the teaching of which is incorporated by reference. The way of the whole 126304.doc -21· 200835784 is incorporated herein. Transfer of gravity flow catalyst particles from one reaction zone to another via a catalyst transfer conduit can be accomplished, introducing fresh or regenerated catalyst particles and recovering spent catalyst particles containing coke. In general, such recombination reactions are typically made up of one or more vm (IUPAC 8_1®) noble metals (eg, platinum, rhodium, ruthenium, and palladium) and a combination of a halogen and a porous support such as a refractory inorganic oxide. It is achieved in the presence of catalyst particles. For example, U.S. Patent No. 2,479,11 (Haensel) teaches an alumina-platinum-halogen recombination catalyst. Although the catalyst may contain a Group VI metal of -2·〇5-2·0 wt·%, a relatively inexpensive catalyst such as a metal containing ruthenium 〇5-〇·5 wt-% of Group VIII may be used. Catalyst. Preferably, the noble metal is platinum. In addition, the catalyst may contain indium and/or a lanthanide metal such as a decoration. The catalyst particles may also contain one or more Group IVA (IUPAC 14) metals of 〇〇5-〇·5 ( For example, tin, antimony, and lead, as described in U.S. Patent No. 4,929,333 (Moser et al.), U.S. Patent No. 5,128, the entire disclosure of The halogen is usually chlorine and the alumina is usually a carrier. Preferred alumina materials are ruthenium, eta and iridium alumina, of which gamma and eta alumina are generally preferred. A property related to the performance of the catalyst is the surface area of the support. Preferably, the support has a surface area of 100 500 m/g. The activity of the catalyst having a surface area below no m2/g tends to be more susceptible to adverse effects of the catalyst coke than catalysts having a higher surface area. In general, despite these Particles can be as large as 6.35 mm (1/4吋) or as small as ι·〇6 mm (1/24吋), but it is usually spherical and has a diameter of 1.6 to 3.1 mm (1/16_1/8吋). However, in a specific recombination reactor In this case, it is necessary to use catalyzed particles of 126304.doc -22-200835784 which are in a relatively narrow size range. The preferred catalyst particle diameter is 1 · 6 mm (1 / 16 leaves). The recombinant method can be carried out using a fixed catalyst bed or a moving bed reaction. The vessel and the moving bed regenerate H. In general, the regenerated catalyst particles are fed into a reaction vessel that typically includes a plurality of reaction zones and the particles are flowed through the reaction vessel by gravity. The catalyst can be withdrawn from the bottom of the reaction vessel and Delivery to a regeneration vessel. In a regeneration vessel, a multi-step regeneration process is typically used to regenerate the catalyst to restore its ability to promote recombination reactions. U.S. Patent No. 3,652,231 (Gr generation nwood et al.), No. 3,647,680 (Greenwood et al.) And 3,692,496 (Greenwood et al.) describe a catalyst regeneration vessel suitable for use in a recombinant process. The catalyst can be passed through gravity through each regeneration step and subsequently from a regeneration vessel. Retrieved and delivered to the reaction vessel. Typically, s ' & is used to supplement the fresh catalyst to the process and is used to reclaim the spent catalyst in the process. The movement of the catalyst via the reaction and regeneration vessel is generally referred to as continuous However, in practice it is semi-continuous. Semi-continuous movement means to transfer a relatively small amount of catalyst at a time close to the interval. For example, one batch can be withdrawn from the bottom of the reaction vessel every twenty minutes and The recovery can take up to 5 minutes, ie the catalyst can flow for 5 minutes. If the catalyst inventory in the vessel is relatively large compared to the batch size, the catalyst bed in the vessel can be considered to be continuously moving. A moving bed system can have the advantage of continuous manufacturing while removing or replacing the catalyst. Typically, the rate at which the catalyst moves through the catalyst bed can range from as little as 45.5 kg per hour to 2,727 kg per hour or more, or the reaction zone of the present invention can be recombined Operating under conditions, including 126304.doc •23- 200835784, often at atmospheric pressure 0-6895 kPa(g) (〇psi(g)-l〇00 psi(g)), especially at 276- Good results were obtained for the relatively low pressure range of 1379 kPa(g) (40-200 psi(g)). The total liquid hourly space velocity (LHSV) is usually 〇1_1 〇hd, preferably 1-5 hours·and more preferably m〇hr-1, based on the total catalyst volume in all reaction zones. The body is σ, ^ gas supply to supply the amount of hydrogen per uomo of the raw material into the recombination zone. Hydrogen is preferably supplied to supply less than 3.5 moles of hydrogen per mole of hydrocarbon feed to the reforming zone. If hydrogen is provided, it can be provided upstream of the combined feed exchanger, downstream of the combined feed exchanger, or upstream and downstream of the combined feed exchanger. Alternatively, hydrogen may be supplied to the recombination zone along with the hydrocarbon feedstock. Even if hydrogen is not supplied to the first reaction zone together with the hydrocarbon feedstock, the cycloalkane recombination reaction occurring in the first reaction zone can also produce hydrogen as a by-product. The by-product or hydrogen produced in situ is admixed with the first reaction zone effluent leaving the first reaction zone and subsequently becomes available to the second reaction zone and other downstream reaction zones. The hydrogen produced in this situ in the first reaction zone effluent typically reaches from 0.5 to 2 moles of hydrogen per mole of hydrocarbon feed. As mentioned previously, the endothermic cycloalkane recombination reaction can occur in the first reaction zone, and thus the outlet temperature of the first reaction zone is typically lower than the inlet temperature of the first reaction zone and is typically 316-454 ° C (600 -850T). The first reaction zone typically accounts for 5% _50 〇 / 〇 and more typically 10% - 30% of the total catalyst volume in all reaction zones. Therefore, the liquid hourly space velocity (LHSV) in the first reaction zone is usually from 0.2 to 200 hours 1, preferably from 2 to 100 hours - 1 and more preferably from 5 to 40, based on the volume of the catalyst in the first reaction zone. Hour -1. Catalyst 126304.doc -24- 200835784 particles are withdrawn from the first reaction zone and passed to the second reaction zone. The particles typically have a coke content of less than 2 wt% based on the weight of the catalyst. The first reaction zone effluent stream can be heated in a heater of the type well known to those skilled in the art of reorganization, such as gas, fuel or gas and fuel hybrid heaters. The heater heats the first reaction zone effluent stream by radiation and/or convective heat transfer. Preferably, the first reaction zone effluent is heated in the radiant zone (preferably only in the radiant zone and not in the convective zone). The hydrocarbon stream can enter and exit the top or lower portion of the radiant zone via a mouth or inverted U-shaped tube. Alternatively, the hydrocarbon stream may enter the lowest temperature of the radiant zone and exit at the bottom of the radiant zone where the temperature is the hottest, or conversely, enter at the bottom and exit at the top. Preferably, for the heater and any subsequent heaters, the hydrocarbon stream enters the top of the radiant zone and exits the bottom. Commercially available combustion heaters suitable for recombination processes typically have individual radiant heat transfer zones (for individual heaters) and a common convective heat transfer zone that can be heated by exhaust gases from the radiant zone. Thus the heater can be considered a second heater, wherein the or the convection zone acts as the first heater. The first reaction zone effluent stream exits the second heater at a temperature typically between 482 and 560 ° C (90 (M040 T). The heater outlet temperature is typically greater than the inlet temperature of the second reaction zone by no more than 5 in consideration of heat loss. It is preferably not more than 1 ° C (2 ° F). Therefore, the inlet temperature of the second reaction zone is usually 482-560 ° C (900-1040 T), preferably 527-549 ° C. (980_1020°F) and

Most preferably 532 to 543 ° C (99 (M 〇 HTF). The inlet temperature of the second reaction zone is usually at least 33 greater than the inlet temperature of the first reaction zone. 〇 (60 ° F) and comparable to the inlet temperature of the first reaction zone The height is at least 56 ° C (l ° ° F) or even at least 83 ° C 126304.doc -25- 200835784 (15 0 F). The inlet temperature of the reaction zone is usually greater than the inlet temperature of the first reaction zone 33- 83 ° C (60-150 ° F) and preferably 56-67 ° C (10 (M 20 ° F). Recombinant C5 + fraction of the desired recombinant octane is usually 85_107 net research octane number (C5 +RONC) and preferably 98-107 C5+RONC. The second reaction zone typically accounts for 10〇/0_6〇〇/0 and more typically 15%-40% of the total catalyst volume in all reaction zones. The liquid hourly space velocity (LHSV) in the second reaction zone is usually 〇17_100 hr-1, preferably 1.7-50 hrs, and more preferably 3.8-26.7 hr-1, based on the catalyst volume in the second reaction zone. The second reaction effluent may pass through the light-emitting zone of the third heater and may pass to the third reaction zone after heating. However, one or more other heaters and/or other heaters may be omitted after the second reaction zone. Reactor The second reaction zone can be the last reaction zone in the column. The third reaction zone typically comprises 25% - 75% and more typically 25% - 50% of the total catalyst volume in all reaction zones. Similarly, the third reaction zone The effluent can pass to the radiant zone of the fourth heater and pass there to the fourth reactor. The fourth reaction zone typically accounts for 30%-80% and more typically 30% of the total catalyst volume in all reaction zones. 50%. The inlet temperature of the third, fourth and subsequent reaction zones is usually within Π (2〇卞) of the inlet temperature of the second reaction zone because it occurs in the second and subsequent (ie third and fourth) reactions. The recombination reactions in the zone often produce less endotherm than the recombination reactions that occur in the first reaction zone, so the temperature drop that occurs in the subsequent reaction zone is generally lower than the temperature drop that occurs in the first reaction zone. The exit temperature of the final reaction zone may be 11 ° C (20 T) or less below the inlet temperature of the final reaction zone, but of course it may be desirable to have an inlet temperature that is higher than the final reaction zone. 126304.doc -26· 200835784 Mentioned by transferring heat in a combined feed heat exchanger The combined feed stream is cooled to cool the final reaction zone effluent stream. After exiting the combined feed heat exchanger, the cooled final reactor effluent is passed to the product recovery zone. The appropriate product recovery zone is known to those skilled in the art of recombination. For example, 'these product recovery equipment typically includes a gas-liquid separator for separating hydrogen from the final reactor effluent stream and (: 1-〇3 hydrocarbon gas and for separating the CU from the remainder of the recombination) - A column of at least a portion of the C5 light smoke. Further, the recombinant can be separated by separating the light recombinant fraction and the heavy recombinant by distillation. In an alternate embodiment, as discussed below, the combined feed stream of the first reactor is heated in the jurisdiction of the first heater and the third or penultimate reaction zone effluent can be entered in the fourth or last The reaction zone is preceded by one or more convection zones of at least one heater. The operating conditions will be similar to the embodiments discussed above. It will also be appreciated that any reaction zone in series may have its feed heated by one or more convection zones without being heated by the radiant zone of the heater. DETAILED DESCRIPTION OF THE DRAWINGS The figures illustrate embodiments of the invention. The figures are presented for purposes of illustration and are not intended to limit the scope of the invention as set forth in the appended claims. The drawings show only the equipment and tubes, lines necessary to understand the present invention, and do not show equipment (such as pumps, compressors, heat) that are not necessary, necessary, and well known to those skilled in the art of hydrocarbon processing. Exchanger and valve). Referring to Figure 1, an embodiment of a refining apparatus 10 is schematically illustrated. The refinery apparatus 10 can include a recombination unit 1 that can in turn include a combined feed heat exchanger or heat exchanger 200, at least one heater 210 (ideally plural A heater 215) and a recombination reactor 400, which in the exemplary embodiment are stacked. In general, recombination reactor 400 includes a plurality of recombination reaction zones 41 in series, such as first reaction zone 412, second reaction zone 418, third reaction zone 424, and fourth reaction zone 430. The first reaction zone 412 can have an inlet 414 and an outlet 416. The second reaction zone 418 can have an inlet 420 and an outlet 422. The third reaction zone 424 can have an inlet 426 and an outlet 428 and a fourth reaction zone 430. There may be an inlet 432 and an outlet 434. While reaction zones 412, 418, 424, and 430 can be included in a single recombination reactor, it should be understood that recombination reactor 400 can include any number of reaction zones or zones can be included in a separate reactor. Moreover, in the present exemplary embodiment, the recombination reactor 400 can be a moving bed reactor in which fresh or regenerated catalyst particles can be introduced via line 402 via an inlet nozzle 404 and spent catalyst can be passed through a line 408 through an outlet nozzle. 406 exit. The plurality of heaters 215 may include a first heater 22A, a second heater 270, and a third heater 320. In general, the first heater 22 includes a pair of flow regions 230 and a light shot region 250, the second heater 270 includes a pair of flow regions 280 and a radiation region 300, and the third heater 32 includes a pair of flow regions 33. And a radiation zone 350. Each of the convection zones 230, 280, and 330 typically includes at least one convection tube 234, 284, and 334, respectively, and each of the radiant zones 250, 3, and 35, respectively, typically includes at least one burner 252 and at least one radiant tube 254, at least one The burner 302 and the at least one radiant tube 3〇4 and at least one 126304.doc -28·200835784 burner 352 and at least one radiant tube 354. Each of the convection tubes 234, 284, and 334 may include an inlet 240 and an outlet 244, an inlet 290 and an outlet 294, and an inlet 340 and an outlet 344, and each of the radiant tubes 254, 3〇4, and 354 may include An inlet 260 and an outlet 264, an inlet 31 and an outlet 3 14 and an inlet 360 and an outlet 364. Moreover, although only one of the zones 230, 250, 280, 300, 330, and 350 and one of the heaters 250, 300, and 350 in the recombination unit 100 are discussed, it should be understood that each zone may typically include a plurality of tubes and Each heater can include several burners. During operation, hydrocarbon stream 150 can enter heat exchanger 2, which uses a hydrocarbon stream effluent 16 from reaction zone 430 to heat the hydrocarbon stream 15 〇. In general, the plume 150 may be referred to as a naphtha feed 1 54 prior to undergoing a recombination reaction. The naphtha feed 1 54 can then enter one or more convection zones 330, 280, and 230 to heat the feed 154 of the first reaction zone 412. Desirably, the naphtha feed 154 continuously passes through the convection zones 330, 280, 230 and exits the convection zone 230 directly into the first reaction zone 412 via the inlet 414. Prior to entering the first reaction zone 412, the convection zones 230, 280, and 330 typically transfer at least 90% of the heat from the at least one heater 210 to the naphtha feed 154. Desirably, at least 95%, 99%, or even 100% of the heat transferred from the at least one heater 210 to the naphtha feed 154 is from the convection zones 230, 280, and 330. After the hydrocarbon stream 150 is subjected to a conversion reaction, the hydrocarbon stream 15 exits the first reaction zone 412 via the outlet 416 and enters the light shot zone 250 via the inlet 260. The hydrocarbon stream 150 can be heated in the Korean zone 250 of the heater 220. Hydrocarbon stream 15〇 can then exit via outlet 264 to enter second reaction zone 418. Thus, the hydrocarbon stream 150 can be passed through the convection zone 230 of the heating 126304.doc -29-200835784 220 before entering the first reaction zone 412 and the hydrocarbon stream 15 〇 subsequently flows through the heater zone 22 of the heater 22 The exemplary embodiment corresponds to the second reaction zone 418. Hydrocarbon stream 150 then enters second reaction zone 418 via inlet 42 and exits via outlet 422 to enter second heater 27A. Ideally, hydrocarbon stream 150 enters inlet 31 of radiant zone 300 for heating for the next reaction zone 424. Hydrocarbon stream 150 can then exit via outlet 314 and enter third reaction zone 424 via inlet 426. After it is completed, 150 can exit via outlet 428 and enter the radiant zone 35 of second heater 320 via inlet 36 〇 for heating for fourth reaction zone 430. Hydrocarbon stream 150 can exit heater 32 via outlet 364 to enter fourth reaction zone 430 via inlet 432. The hydrocarbon stream 15 can then exit as a hydrocarbon stream effluent 160 via outlet 434 to heat the naphtha feed in heat exchanger 2 154 °. Other embodiments of the invention are illustrated in Figures 2-3. As shown in Fig. 2, a reassembly unit 110 can include a heat exchanger 2A and at least one heater 210, and (ideally) a plurality of heaters 215, as described above. The recombination unit 11 can also include a plurality of recombination reactions of 440. The plurality of recombination reactors 440 may preferably include a first recombination reactor 45 having an inlet 454 and an outlet 458, a second recombination reactor 46 having an inlet 464 and an outlet 468, and an inlet. 474 and a third recombination reactor 47 of an outlet 478 and a fourth recombination reactor 48 having an inlet 484 and an outlet 488. Although each reactor may contain more than one reaction zone, each of the plurality of reactors 44, 460, 470, and 480 typically have a single reaction zone. Hydrocarbon stream 150 (preferably naphtha feed 154) may be preheated in a parent exchanger 200 heated with a hydrocarbon stream discharge ι6 〇 126304.doc -30 - 200835784. The naphtha feed 154 can then be heated in the convection zones 230, 280 and 330 of the plurality of heaters 2, 5, similar to the use of the convection zones 230, 280 and 330 with respect to the flow reversal sequence. Desirably, after the naphtha feed 154 exits the convection zone 330 of the heater 320, the naphtha feed 154 enters the recombination reactor 450 via inlet 454 for conversion. Hydrocarbon stream 150 can then exit reforming reactor 450 via outlet 458 and enter radiant zone 250 of heater 220 via inlet 260. Following heating, hydrocarbon stream 150 can exit heater 220 via outlet 264 and enter second reformer reactor 460 via inlet 464. After it is completed, hydrocarbon stream 150 can undergo further conversion before exiting recombination reactor 460 via outlet 468. Next, hydrocarbon stream 150 can be heated via inlet 3 10 into heater 270 and then exited via outlet 314 to undergo further reaction. After exiting heater 270, hydrocarbon stream 150 can enter third recombination reactor 470 via inlet 474 to be further recombined prior to exit via outlet 478. Hydrocarbon stream 150 can then enter inlet radiant zone 350 of heater 320 via inlet 360 to transfer heat to hydrocarbon stream 150. After it is completed, hydrocarbon stream 150 can exit via outlet 364 to enter fourth recombination reactor 480 via inlet 484 to react hydrocarbon stream 150 before hydrocarbon stream 150 can exit outlet 488. The hydrocarbon stream 150 can then be a hydrocarbon stream effluent 160 for heating the naphtha feed 154 in the heat exchanger 200. In another embodiment, referring to FIG. 3, a recombination unit 120 can include a heat exchanger. 200. At least one heater 210 and a plurality of recombination reactors 440, as described for recombination unit 110. The flow of hydrocarbon stream 150 is similar except that hydrocarbon stream 150 entering the final reactor 126304.doc-31-200835784 480 is heated by convection zones 230, 280 and 330 rather than by radiant zone 350 of third heater 320. Specifically, after heating in the heat exchanger 2, the hydrocarbon stream 150 entering the first reactor 45 0 can be heated by the radiation zone 25 of the first heater 22. After completion, the hydrocarbon stream 150 can be passed to the second heavy-group reactor 460 and the third recombination after being heated in the radiation zone 300 of the second heater 27 and the light-emitting zone 350 of the second heater 320, respectively. Reactor 470. Next, the hydrocarbon stream 15 can be withdrawn from the second reactor 470 to enter the convection zones 230, 280 and 330 of the heaters 220, 270 and 320, respectively, before entering the fourth or final recombination reactor 480. The hydrocarbon stream effluent 160 from the fourth reactor 480 can then heat the naphtha feed 154 in the heat exchanger 200. In the embodiments described above, it is desirable to have a ratio of the heater radiation zone to the reaction zone or reactor below 1:1. Preferably, the ratio is determined to be 1:2, 2:3, 3:4 or 4:5 depending on the number of reaction zones. Although the flow pattern is not continuously passed through the convection zone in Figure ι.3, it should be understood that the flow can pass through the parallel convection zone _ and combine before entering, for example, the first or last reaction zone in series. Moreover, although any temperature profile can be used for the above embodiments, it is " using a step-up reactor inlet temperature profile. In general, although it is not desirable to have any constraints, the step-up temperature distribution can reduce the difference in the load of the plurality of Han shots. This reduced difference can improve - or standardize the radiation zones in multiple heaters, thereby reducing manufacturing, installation or refurbishment costs. Although the above embodiment illustrates a heater having its own convection zone, it should be understood that the above-described recombination unit may include one or more heaters or furnaces having i (four) zones (having a common convection zone). Specifically, see Figure 4, 126304.doc •32- 200835784

The heater 500 can include a common convection zone 51 and a plurality of radiant zones 53A, such as a first radiant zone 540, a second radiant zone 55A, and a third radiant zone 560. The common convection zone 51〇 typically includes a number of convective officers 512 in a parallel configuration. In general, each convection tube 512 is slightly u-shaped and oriented with its sides. A number of tubes 512 can be aligned back and forth in a stacked form. Other configurations of tube 512 can also be used, such as those discussed above. The exhaust gas raised by the radiation zones 54G, 55G, and 56G can enter the convection zone 51 and exit the stack 520. Although indicated only in the first radiant zone 540, typically each radiant zone 540, 550, and 56A can include a plurality of radiant 544 in a parallel configuration. In general, each radiant tube 544 is slightly u-shaped and a plurality of 544 are vertically oriented in a stack form and aligned back and forth. Other configurations may also be used for tube 544, such as those discussed above. The radiant zones "Ο, 550 and 56G may be separated by fire walls 57 and 572 and respectively include a plurality of burners 542, 552 and 562. Using a heater, the hydrocarbon stream ... may enter the first reaction, for example, in the recombination unit (10) The zone 412 enters the common convection zone 51. The hydrocarbon stream can then be heated in the radiant zones 540, 550 and 560 after entering the reaction zone 418 and 43 分别, respectively, without further detailed description. The present invention may be made to the extent possible by the above description. The foregoing preferred embodiments are to be considered as merely illustrative and not limiting in any way. The method of the present invention is intended to be described in detail. The description of the embodiments of the present invention is not limited to the scope of the patent application of the present invention. 126304.doc -33·200835784 T: The specific details of the example These examples are based on engineering calculations and practical experience with respect to similar methods. Comparative Example 1 and Example 1 describe the heater load of the 4 reactor helium heater method and the 4 reactor/3 heater method, respectively.

In the comparative example!, the inlet temperatures of the reactors were equal and the combustion heaters used and having multiple radiant heater units heat the feed and reactor effluent. i is based on the load distribution between the convection zone and the radiant zone and the charge that can be used for process heating in the convection zone to estimate the maximum process load in the turbulent zone. The following process load or heat absorption requirements for each heater unit are given when the reactor inlet temperatures are equal and 548 〇 c (1019 T). Only Example 1 uses a convection zone instead of the _ radiant heater unit. This is achieved by lowering the heater outlet temperature (in this case the reactor port temperature). In this example, only the portion of the convection zone shared by the radiant heater unit is used to heat the feed to the first reactor (as shown in Table 2), while the remainder is used to generate steam. (4) Holding the second radiant heater unit outlet temperature is lower in order to reduce the load demand in the second heater unit. These methods are moving bed processes utilizing continuous regeneration, each of which regrades the feedstock at the same feed rate. In all methods, lhsv, hydrogen to smoke molar ratio, reactor pressure, catalyst, c5+R〇nc, catalyst distribution, and catalyst circulation rate were all the same. In Table 2 below, the data of Comparative Example 1 was compared with the data from Example 1. Table 2 126304.doc -34· 200835784 (Q, in kilojoules per second and millions of btu per hour) Comparative Example 1 Example 1 Δ Burning Q, kilojoules per second (mm btu/hour) __ 77,199 (263.63) 64,185 (219.19) -17% Radiation zone Q, kJ/s (mm btu/hour) __ 45,588 (155.68) 37,213 (127.08) -18% Processing convection Q, kJ/s (mm btu/hour) ____ 0 7,581 (25.89) Heater inlet temperature No. 1. C (°F) ____ 478 (893) 477 (891) Heater No. 1 Q, kJ/s (mm btu/hour) 10?29〇 (35.15) Heater 1 inlet temperature, °C (°F) ___ 548 (1,019) 529 (985) Heater No. 2 Q, kilojoules per second (mm btu/hour) 15,890 (54.27) 15,560 (53.12) Reactor 2 inlet temperature. c (°F) 548 (!?019) 542 (1,008) Heater No. 3 Q, kJ/s (mm btu/hour) 10,560 (36.06) 12,370 (42.23) Reactor 3 inlet temperature. C (°F) 548 (1,019) 554 (1,030) Heater No. 4 Q, kJ/s (mm btu/hour) 7,816 (26.69) 9?289 (31.72) Reactor 4 inlet temperature, ° C (°F) 548 (1,019) 554 (1,030) Reactor 4 outlet temperature,. c (°F) ^ 510 (950) 509 (948) Total processing Q, kJ/s (mm btu/hour) 44,557 (152.16) 44,803 (153.0) HP steam convection Q, kJ/s (mm btu/hour) 24,840 (84.82) 12,690 (43.33) T flue exit,. C (°F) 162 (324) 194 (381) Total Fuel Efficiency, % 91.2 89.7 All temperatures are design temperatures, which are typically 16°C (28°F) greater than the actual predicted operating temperature. This deviation allows for a small margin of error for the predicted decrease in catalyst activity. An example according to the invention has an average thermal load of 12,400 kJ/s (42.36 mm btu/hr) in the radiation zone with an unbiased standard deviation of 3,133 kJ/s (10.70 mm btu/hour) and 4 radiations. Comparative Example 1 of unit heating feed had an average heat load of 11,14 〇 kJ/sec (38.04 mm btu/hr) and an unbiased standard deviation of 3,400 kJ/sec (ιι·61 mm btu/hr). Further, the load range in Example 1 was 6,267 kJ/s (21.40 mm btu/hour) and the load range in Comparative Example 1 was 8, 〇76 kJ/sec (27.58 mm btu/hour). The total fuel combustion requirement of Comparative Example 1 was 77,199 126304.doc -35·200835784 kJ/sec (263.63 mm btu/hr) at 58% radiation efficiency and 28% heat was recovered by the process in the convection zone. f. The available load in the convection zone can be estimated for process heating. If the first radiant heater unit is removed, the available convection zone load is: (54·27+36·06+26·69)/0·58*(1·0_58)*〇·28=23·7 leg btu/ Hours or 6,940 kJ/s. If the fourth radiant heater unit is removed, the available convection zone load is: (35.15 + 54.27 + 36.06) / 0.5811 - 0.58) 18 ^ 4 faces btu / hour or 7, in general, the equivalent reaction in this comparative example The inlet temperature of the inlet is not designed to give sufficient convection load to replace one of the heater units with the same amount of catalyst load in the reactor. However, without increasing the catalyst loading in the reactor, it is possible to remove the heater unit by reducing the efficiency of the radiant zone and increasing the bridge wall temperature or skewing the reactor inlet temperature. In general, reducing the efficiency of the radiant zone and the temperature of the bridge wall are not effective. For this reason, it is generally more fuel efficient and cost effective to skew the reactor inlet temperature to change the heat absorption requirements of each heater unit. As discussed above, Example 1 replaced the first radiant heater unit with a pair of flow zones. The reactor inlet temperature was deflected to 529/542/554/554 °C (985/1008/1030/1030 °F). This helps to balance the remaining radiant area loads of the different heater units. In Example 1, the available load in the convection zone was estimated for feed heating. (53·12+42·23+31·72)/0·58*(1-0·58)*0_28=25·8 mmbtu/hour or 7,560 kJ/sec. Therefore, it is possible to slightly reduce the radiation zone efficiency to below 58% or otherwise slightly lower the reactor inlet temperature to remove the first radiant heater unit. Therefore, by removing the first radiant heater unit, the expected fuel combustion is reduced from 126304.doc -36 - 200835784 77, 199 kJ / sec (263 · 63 匪 Mu / hr) to 64, (8) kJ, seconds (21 ^9_btu/hour), which can result in significant savings in equipment investment and fuel. This reduction in heater load range enables standardization of the heater size, thereby reducing the cost of purchasing and/or installing the apparatus in the recombination unit. The convection zone can be used to heat the reactor (preferably The feed of the first or last reactor in series. This can be achieved in the above examples by appropriately adjusting the inlet temperature of the first reactor. Another possibility is that the convection zone used for process heating can be used to reduce the efficiency of the radiant zone and use a lower bridge wall temperature, although in some cases this possibility is generally considered to be less than ideal. Another possibility is to add sufficient catalyst to the reaction zone in order to reduce the load demand so that it is possible to replace one or more radiation zones with at least one convection zone. Without further elaboration, it will be apparent to those skilled in the art that the invention can All injuries and percentages are by weight unless otherwise stated. The entire disclosures of all of the cited applications, patents and publications are hereby incorporated herein by reference. The various features and modifications of the present invention are susceptible to various modifications and alternatives to those skilled in the art. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic illustration of an exemplary refining apparatus including a recombination unit of the present invention. 126304.doc -37- 200835784 Figure 2 is a schematic illustration of another exemplary recombination unit of the present invention. Figure 3 is a schematic illustration of yet another exemplary recombination unit of the present invention. Figure 4 is a schematic double cross-sectional view of an exemplary heater having a common convection zone and a plurality of radiant zones of the present invention. [Main component symbol description]

10 Refining equipment 100 Recombining unit 110 Recombining unit 120 Recombining unit 150 Hydrocarbon stream 154 Naphtha feed 160 Hydrocarbon stream effluent 200 Heat exchanger 210 Heater 215 Heater 220 Heater 230 Convection zone 234 Convection tube 240 Inlet 244 Outlet 250 Fortunately, S-field 252 burner 254 radiant tube 260 inlet 126304.doc -38 - 200835784

264 out σ 270 second heater 280 convection zone 284 convection tube 290 inlet 294 out σ 300 幸昌射区 302 burner 304 radiant tube 310 inlet 314 outlet 320 third heater 330 convection zone 334 convection pipe 340 inlet 344 out π 350 Fortunately, the blasting area 352 burner 354 radiant tube 360 inlet 364 out σ 400 recombination reactor 402 line 404 inlet nozzle 126304.doc -39- 200835784

406 outlet nozzle 408 line 410 recombination reaction zone 412 first reaction zone 414 inlet 416 out a 418 second reaction zone 420 inlet 422 outlet 424 third reaction zone 426 inlet 428 outlet 430 fourth reaction zone 432 inlet 434 outlet 440 recombination reactor 450 First reactor 454 inlet 458 out α 460 second recombination reactor 464 inlet 468 outlet 470 third recombination reactor 474 inlet 126304.doc -40 200835784

478 out π 480 fourth recombination reactor 484 inlet 488 outlet 500 heater 510 common convection zone 512 convection tube 514 parallel configuration 520 discharge port 530 radiation zone 540 first radiation zone 542 burner 544 radiant tube 546 parallel configuration 550 Second radiation zone 552 burner 560 third radiation zone 562 burner 570 fire wall 572 fire wall 126304.doc -41 -

Claims (1)

200835784 X. Patent application scope: 1 · A method comprising: (4) transferring a hydrocarbon stream through a recombination unit, wherein the recombination unit comprises: (1) a heater comprising a pair of flow regions and a radiation region, and (η a plurality of recombination reaction zones, wherein the hydrocarbon stream is heated in the convection zone for reaction in one of the recombination reaction zones to which the hydrocarbon stream is passed, and the radiation of the hydrocarbon stream in the heater The zone is heated to react in another recombination reaction zone to which the hydrocarbon stream is passed. 2. The method of claim 1, wherein the heater of the recombination unit further comprises a burner. 3. The method of claim 1, wherein the transporting the hydrocarbon stream through the recombination unit further comprises: 3 heaters; and 4 recombination reactors, wherein each recombination reactor comprises one of the plurality of recombination reaction zones And further comprising: passing the hydrocarbon stream through at least one convection zone of the heater prior to entering one of the recombination reactors; and passing the hydrocarbon stream through each of the other recombination reactors, wherein The hydrocarbon stream is heated in a radiant zone of one of the heaters corresponding to one of the other recombination reactors. 4. The method of claim 3, wherein the transferring the hydrocarbon stream further comprises the recombination reactors connected in series, and the first or last recombination reactor receives the hydrocarbon stream passing through at least one convection zone of a heater such as a side . 126304.doc 200835784 5. The method of claim 4, wherein the transporting the hydrocarbon stream further comprises a respective enthalpy = a-radiation zone and a convection zone or a common-common convection zone, and wherein: The reaction stream is passed through the convection zone or the common convection zone of each heater prior to receiving the hydrocarbon stream. 6' The method of claim 4, wherein the transferring the hydrocarbon stream further comprises: capturing the hydrocarbon: passing through a heat exchanger to receive the final recombination reactor from the series prior to passing through the at least one convection zone Hydrocarbon flow: The heat of the material. 7. The method of claimant wherein transferring the hydrocarbon stream further comprises the convection zone comprising a plurality of convection tubes in a parallel configuration and the radiant zone comprising a plurality of radiant tubes in a parallel configuration. 8. The method of item i, wherein at least 9% of the heat from the heater is transferred to the recombination reaction zone is from the convection zone of the heater. 9. A device comprising at least one of a refining device and a petrochemical manufacturing device, comprising: a component (a recombination unit comprising: (1) at least one heater, the heater comprising a pair of flow zones And a radiant zone, the convection zone comprising at least one pair having a population and an outlet, the radiant zone comprising a burner and at least one radiant tube having an inlet and an outlet; and (...the plurality of series recombination a reaction zone, wherein each reaction zone has an inlet and an outlet, wherein a first reaction zone inlet is used to receive the hydrocarbon stream from the outlet of the convection tube, and a second reaction zone inlet is received by 126304.doc 200835784 The hydrocarbon stream from the outlet of the radiant tube. The apparatus of claim 9, wherein the recombining unit further comprises: 3 heaters; and 4 series recombination reactors, wherein each recombination reactor comprises the plurality of recombination reactors One of the reaction zones is a recombination reaction zone. 126304.doc