JP4504025B2 - Combined hydroprocessing step and structure for the same - Google Patents

Description

  The field of the invention is petrochemistry, particularly hydroprocessing of various hydrocarbon feedstocks.

  Hydroprocessing is commonly used in many modern refineries where hydrogen is contacted with a hydrocarbon feedstock in the presence of a catalyst to remove impurities including oxygen, nitrogen and sulfur and saturate the hydrocarbon. Is a type of hydrogenation process commonly used. A frequently used form of hydroprocessing is hydrodesulfurization, which is mainly used to reduce sulfur content from the refinery intermediate stream. Hydrodesulfurization is commonly used in combination with processes including catalytic reformers, fluidized bed catalytic crackers, and hydrocracker raw material pretreatments, and also includes naphtha, diesel, jet, heating oil and residue. It can be used independently as a product quality improvement step for olefin saturates, and polycyclic aromatics. Hydrocracking is commonly used in many modern refineries where hydrogen is contacted with a hydrocarbon feedstock in the presence of a catalyst to produce a light product (ie, the average molecular weight is reduced). Another type of hydrogenation process. Many hydroprocessing configurations and processes known in the prior art improve product quality while reducing energy consumption and capital costs resulting in integration of hydroprocessing and hydrocracking reactors in various processes There is a constant effort to do that.

  For example, in one integrated concept, a two-stage hydrocracking process is described in which new feedstock is combined with waste from the hydrocracking stage and the combined stream is then introduced into the hydrotreating stage. A hydrotreater is coupled to the hydrocracker as disclosed in US Pat. No. 3,328,290 to Hengstebeck. The high boiling fraction is then separated from the hydrotreater waste, fractionated to produce a light product and a heavy bottom stream, and then recycled to the hydrocracking stage with a hydrogen-containing gas.

  Another example, US Pat. No. 6,235,190 by Bertram, describes an integrated hydroprocessing and hydrocracking process in which two hydroprocessing catalysts having different activities are improved. Acted in series to provide the quality of the treated product, the waste from the hydrotreating reactor converts the hydrotreated waste to a light product with reduced aromatic hydrocarbon content In order to be subjected to a hydrocracking process. In further illustration, to produce a naphtha product, a distillate that boils beyond the boiling range of naphtha, and a lubricant product, as described in US Pat. No. 6,261,441 by Gentry et al. A combined hydrotreating / hydrocracking process is described in which the hydrocracking stage is followed by a hydrodewaxing stage with single feed and bottoms fraction recycle.

  Hydrocracking to produce a variety of products, as described in US Pat. No. 6,328,879 to Kalnes, in another system, where the product has a lower boiling range than the feedstock. In a catalytic hydrocracking using a zone, a hydrotreating zone, and a high pressure product stripper, two independent feedstocks are hydrocracked.

  Alternatively, more than one hydrotreating reactor and / or catalyst bed is used for catalytic hydrogen as described in Parker US Pat. No. 3,537,981 or Cooper US Pat. No. 6,103,105. May be used for Parker's process uses a first hydrotreating reactor coupled to a separator in series with a second hydrotreating reactor, while Cooper et al. Uses two series connected hydrogens without the use of a separator. A catalyst bed is used. However, both the Cooper and Parker hydroprocessing configurations are generally limited to only a single feedstock.

  Thus, many integrated processes provide at least some advantages over other known configurations and methods, but all or almost all of the known configurations and methods are hydrocracking. Or a process where hydroprocessing of a single boiling range (e.g., naphtha, diesel, light oil, residual oil) feedstock is considered. As a result, all or almost all of the known hydroprocessing steps require individual plants where one or more feedstocks are used. Accordingly, there remains a need to provide improved configurations and methods for hydroprocessing petrochemical products.

  The present invention relates to a configuration and method for a hydroprocessing plant, and particularly for an integrated hydroprocessing plant in which at least two feedstocks having different boiling ranges (eg light oil and diesel oil) are hydrogenated. It relates to a configuration and method. Moreover, the aspect assumed especially includes the control method of the structure assumed.

  In one embodiment of the present inventive subject matter, an envisaged plant includes an interbed separator that contains a first feed (eg, hydrotreated gas oil) and a second feed (eg, diesel oil). The first raw material includes preheating and vaporizing at least a portion of the second raw material, thereby producing a preheated and at least partially vaporized second raw material, wherein at least one of the first raw materials A portion is provided by the first hydroprocessing reactor, and at least a portion of the preheated and at least partially vaporized second feed is fed to the second hydroprocessing reactor that produces the product. Is done.

In particular, the envisaged interbed separator comprises at least a partial vapor-liquid equilibrium stage, preferably at least two vapor-liquid equilibrium stages, and may have a tray column or pack column configuration. It is further preferred that the envisaged interbed separator may contain a hydrogen rich stream, which may be recirculated in the plant and / or a makeup hydrogen stream. Assumed interbed separators generally operate at pressures similar to operating reactor pressures of about 3.45 MPa ( 500 psi ) to about 16.55 MPa ( 2400 psi ) .

  In particularly preferred embodiments of the present inventive subject matter, at least a portion of the second feedstock is effective to control light-end recovery of the hydrotreated first feedstock in the interbed separator. At a rate to the second hydrotreatment reactor. The remaining portion of the second feed may then be used to adjust the temperature in the second hydrotreating reactor.

In another aspect of the present inventive subject matter, the first and second hydrotreating reactors are conditions under which hydrotreating reactor feedstocks will exhibit less than 10% conversion, and more preferably less than 8% conversion. Work under. Thus the second hydrotreating reactor envisaged are preferably operated at a pressure of between about 4.83 MPa (700 psi) to about 16.55MPa (2400psi).

  Furthermore, it is envisaged that the arrangement according to the present inventive subject matter may be realized in a new plant. However, the interbed separator and the second hydroprocessing reactor may also be integrated into an existing hydroprocessing plant as an improvement.

  In a further aspect of the present inventive subject matter, a hydrotreating method provides a first hydrotreating reactor, a second hydrotreating reactor, and an interbed separator that contains first and second feedstocks. Includes one step. In another step, the interbed separator is fluidly coupled to the first and second hydroprocessing reactors. In yet a further step, the hydrotreated first raw material is used to preheat and vaporize at least a portion of the second raw material, thereby preheated and at least partially vaporized first. In a separate step, at least a portion of the second raw material that has been preheated and at least partially vaporized is mixed with another portion of the second raw material to produce a second hydrogen Supplied to the chemical treatment reactor.

Various known configurations and processes for desulfurization and / or denitrification are performed in the presence of a catalyst that forms H ₂ S and / or NH ₃ from sulfur-containing and / or nitrogen-containing compounds in the feedstock. A process using a hydroprocessing reactor in which a hydrocarbon-based raw material reacts with hydrogen is utilized. Prior art FIG. 1 shows an exemplary configuration 100 for such a plant. In this figure, a single feedstock (eg, diesel) 110 passes through a heater 120 and then is supplied to a hydroprocessing reactor 130. Hydrogen (either separately via line 141) or combined with the feedstock (via line 142) is added to the hydroprocessing reactor catalyst and the hydrotreated product 112 is ( After the cooling step in cooler 180) In separation device 150, gaseous portion 112A containing primarily hydrogen, hydrogen sulfide, and light non-condensed hydrocarbons, hydrotreated diesel, some natural naphtha, and the remaining sour gas The liquid portion 112B containing the liquid is separated. Hydrogen from the gaseous portion is generally purified in an adsorber 152 having an amine-containing solvent and recycled through the compressor 160 into the hydrogen reactor (up). Hydrotreated product 112C can then be recovered from column 170 along with representative products such as natural naphtha 112D and sour gas 112E. While such a configuration works relatively well for single type feedstocks (eg vacuum gas oil, diesel oil, diesel, naphtha, etc.), known plants with multiple feedstocks (eg diesel oil and diesel) In general, it requires a number of separate hydroprocessing configurations that add significantly to the construction and implementation of such plants.

  In prior art efforts to improve the configuration and method for hydrotreating hydrocarbonaceous feedstocks, a large number of feedstocks (ie feedstocks with different boiling ranges such as light oil and diesel) are combined into a unified configuration. In that configuration, the interbed separator is fluidly coupled to the first and second hydroprocessing reactors and also (eg, a cooler or heat exchanger, liquid / gas That a single hydrogen recycle loop (including separator, amine stripper, and compressor) can be used in two (or more) hydroprocessing reactors, each processing different feedstocks. The inventors have found.

  Thus, in a particularly preferred embodiment of the present inventive subject matter, the plant can include an interbed separator that contains a first feed and a second feed, wherein the first feed is at least one of the second feed. Preheating and vaporizing the part, thereby producing a pre-heated and at least partially vaporized second feed, wherein at least a portion of the first feed is provided by the first hydrotreating reactor; At least a portion of the pre-heated and at least partially vaporized second feed is supplied to a second hydroprocessing reactor that produces a product.

  FIG. 2 shows an exemplary configuration of a hydroprocessing plant 200 in which two different hydrocarbonaceous feedstocks are hydroprocessed using an integrated configuration with a single hydrogen recycle loop. . In FIG. 2, light oil 210A (first hydrocarbon feedstock) is heated in heater 220 and then produces hydrotreated product 212 (which is the first feedstock for the interbed separator). Therefore, it is introduced into the hydrotreating reactor 230A. The hydrotreated product 212 is then fed to an interbed separator (hot separator) 240. It should be appreciated that the hydrotreated product 212 may pass through an apparatus (eg, a heat exchanger, etc.) before entering the interbed separation apparatus. The interbed separator 240 is also preferably a second feedstock for the interbed separator that may be preheated, preferably at least partially (ie at least 10 to 50%, more typically from 50). It also contains diesel feed 210B, which is liquid phase (80%, most commonly 80 to 100%). Steam feed 290, typically hydrogen (or hydrogen-containing), may be further fed to an interbed separator where the steam feed is partially recycled within the plant. Alternatively, the steam feed (or hydrogen-containing feed) may be at least partially make-up hydrogen.

  Within the separator, the second feed is at least partially vaporized (or further vaporized) and heated by direct contact with the hydrotreated product 212. In addition, the interbed separator 240 separates the feed into products, in which the highly volatile components exit the separator along with the vaporized second feed 201 'and are also volatile. The lower component exits with a slightly cooled hydrotreated cracker product 212 '. The interbed separator comprises at least a partial vapor-liquid equilibrium stage, or more preferably at least two or more vapor-liquid equilibrium stages, and may have a tray column or pack column configuration. The liquid hydroprocessed product 212 'then separates the liquid hydroprocessed product 212' into processed products including, but not limited to, light oil, natural naphtha, and sour gas. To the column 270A. The vaporized second feed 210 'is then mixed with additional diesel feed via line 210B' and can be accommodated in the second hydroprocessing reactor 230B that can or cannot accommodate the additional feed stream. Introduced (as a combined second raw material). It should be appreciated that some of the light boiling range components will be recovered from the first product 212 'and further hydrotreated in the second reactor.

The so-treated second feed 210 "(usually hydrotreated diesel) is then cooled in cooler 280 and in separator 250, the liquid portion and (mainly H ₂ S, hydrogen, And gaseous fractions (including light non-condensed hydrocarbons), which can be purified via an adsorber 252 that may use prior art solvents. Compresses this hydrogen-containing recycle gas stream to a suitable pressure for reintroduction into the system (eg, in the first reactor and / or to the first feed or feed). The liquid portion of the two hydrotreated feeds 210 "then contains the hydrotreated product, low sulfur diesel, natural naphtha, and sour gas. It is not limited to, separates the treated product, it is fed to the column 270B.

Also, as used herein, the term “interbed separator” means that the interbed separator is at least partially hydrotreated (can be previously hydrotreated or not hydrotreated). Can also refer to a separation device that is fluidly coupled to at least two hydroprocessing reactors to contain a first feed and a second feed, wherein the first and second feeds have different boiling ranges (eg, Light oil and diesel oil). In general, the contemplated interbed separator operates at high temperatures (ie, 148.9 ° C to 398.9 ° C ( 300 to 750 ° F ) ), and the interbed separator is a steam or hydrogen containing feed. It is particularly envisaged that may be further accommodated.

  FIG. 3 shows a particularly preferred configuration of the flow around the interbed separator 340 and the second reactor, in which the portion 310B ′ of the second feed 310B and the additional third feed 395C. Bypasses the interbed separator to produce a hydrotreated product 310 "(through the combined stream 310 ') and is fed to the second reactor (second feedstock). ) The speed of the substantially liquid phase stream 310B "is determined to allow the desired light-end recovery of the first hydrotreated feed 312 '. The term “light end recovery” as used herein refers to the recovery of components within a component mixture, where the boiling point of the component is the upper third of the boiling range of the mixture, and more generally. The boiling point of the upper quarter (or higher). The remaining portion of the second feedstock 310B 'may be further preheated in a heat exchanger or heater 310C before being directed to the second reactor. It should be appreciated that the third feedstock can be any hydrocarbon-based feedstock and may include naphtha, jet, diesel, or light oil boiling range materials. It should also be appreciated that additional (fourth, fifth, etc.) feed streams can be fed to the second reactor, bypassing the interbed separator. In this representative configuration, the third raw material 395C is circulating oil from the FCC unit. In this preferred configuration, the second reactor operates at a stable feed rate while allowing good operational flexibility in the operation of the interbed separator and good light end recovery control. It should also be appreciated that the reactor 330B may operate in a two phase (vapor / liquid) or preferably trickle fluid region.

  In order to maintain a specific inlet temperature to the second reactor 330B, the feed temperature of the heated stream 310B ′ and / or 395C ′ (uses the internal stream in the plant, or a stripping or fraction portion And can be regulated via an integrated heat source or an external heat source. Directing the feed portion to a second hydroprocessing reactor solves the difficulties associated with thermal balance (eg, hydrogen stream 390 is avoided (eg, as hot hydrogen stripping gas) to avoid thermal imbalances. This ability to adjust the feed temperature of the feed section that bypasses the interbed separator is particularly advantageous. The amount of the second feed that bypasses the interbed separator (eg, by direct feed downstream of the interbed separator hydrotreater) is also relative to the first and second reactor feeds. It will also depend on the volumetric velocity. As the volumetric rate of the second reactor feed increases in proportion to the first reactor feed, the percentage of the second reactor feed that bypasses the interbed separator will generally increase.

Still further, a portion of the second feed (or alternatively the third feed) that bypasses the interbed separator (eg, via a feed directly to the second hydrotreater) is preheated. It should be appreciated that the temperature may be controlled. As a result, the temperature control of the portion of the second feedstock controls the inlet temperature of the second hydrotreating reactor over a relatively wide range (eg, +/− 23.9 ° C. ( 75 ° F. ) ). It should be appreciated that may be used for this purpose. Thus, the portion of the second feed that bypasses the interbed separator is typically about 20 vol% (or less) to about 80 vol% (or more) of the total volumetric rate of the second feed. Within range. Most commonly, however, the amount of the portion of the second feed that bypasses the interbed separator will be about 35 to 65 vol%. Preferably, the additional feed (3rd, 4th, etc.) is at (temperature and pressure) conditions (when initially fed to the recirculation loop or when measured at reactor inlet temperature and pressure) If there is make-up gas or recycle gas, it will be at least partially liquid phase (below its dew point) before its addition. Thus, in some of the envisaged configurations, and particularly in configurations where a portion of the second or third feedstock is in liquid phase and fed to the second hydrotreating reactor, the second hydrogenation It should be appreciated that the processing reactor operates in a two-phase or preferably trickle fluid region.

  In a preferred embodiment of the present inventive subject matter, it is more particularly recognized that both hydroprocessing reactors operate under conditions effective to reduce the concentration of sulfur-containing and / or nitrogen-containing compounds in the feed. I want. As a result, it should be appreciated that in a preferred configuration, both feeds are not substantially converted to low boiling products (ie, less than 10%, more typically less than 8%). In a particularly preferred embodiment, the second feedstock comprises diesel, which is less than 50 ppm, more preferably less than 25 ppm, and most preferably less than 10 ppm after hydroprocessing and column separation. Containing.

  Thus, the envisaged configuration may be used for the production of two products having different boiling ranges and different product specifications. For example, the existing diesel oil hydroprocessing plant upstream of the FCC unit has been modified with a relatively low capital investment to include a second reactor (or reactor part) for producing high quality, low sulfur diesel fuel. Good. In this configuration, additional heat is required for existing heaters, heat exchanger trains, and coolers because it leaves the system via products from the interbed separator used as stripper preheat. It should be particularly recognized that the increase in capacity is moderate to slight.

  Still further, the concept of bypassing a portion of the second feed around the interbed separator (eg, by feeding it downstream of the hydrobed of the interbed separator) is an alternative integrated An alternative configuration that may be used in the configuration and method, and that is specifically envisioned, is a configuration in which a first hydrocracking reactor is coupled in series to a second hydrotreating reactor (see herein for reference). (See US Pat. No. 6,328,879 to Kalnes, incorporated).

  Still further, the concept of bypassing a portion of the second feed around the interbed separator may be extended to alternative integrated configurations and methods, and particularly contemplated alternative configurations are It should be appreciated that one hydrotreating reactor includes a configuration coupled in series to a second hydrocracking reactor.

  Among other advantages, adding the liquid portion of the third feed to the second reactor without passing through the interbed separator can reduce the high boiling range fraction of the third feed in the separator. Without loss, it will allow processing of high boiling range materials (ie, similar to the first feedstock). Moreover, the potential for difficulties associated with heat balance can be reduced if not completely avoided.

It should be particularly recognized that the terms “hydrocracking” and “hydrotreating” do not refer to the same type of hydrotreating that occurs in the reactor. As used herein, the term “hydrocracking reactor” as used herein refers to a reactor in which a hydrocarbon-containing feedstock is converted to a light product (ie, the average molecular weight is reduced). As used herein, the terms “converted” or “converted” mean that a certain percentage of new feedstock will change to middle distillates, gasoline, and light products (eg, “Hydrocracking Science And Technology”). by J. Scherzer and A. J. Gruia; see Marcel Decker, Inc.). Thus, a contemplated hydrocracking reactor will have a conversion of at least 15%, more typically at least 30%, and most typically at least 50%. In contrast, the term “hydrotreating reactor” refers to (a) conditions that result in less than 15% conversion, and more typically less than 10%, and (b) sulfur in hydrocarbon-containing feedstocks. And a reactor in which a hydrocarbon-containing feedstock reacts with hydrogen in the presence of a catalyst under conditions that result in the formation of H ₂ S and / or NH ₃ from the nitrogen-containing compound.

  With respect to the first, second, and third hydrocarbon-based feedstocks (210A, 210B, and 395C), various hydrocarbon-based feedstocks are considered suitable and particularly contemplated for use herein. In an embodiment, the first hydrocarbonaceous feedstock comprises light oil or any petroleum fraction having a higher boiling range than diesel, and the second hydrocarbonaceous feedstock is from diesel or the first feedstock. It should be recognized that any fraction having a lower boiling range is included. Furthermore, in a particularly envisaged embodiment, the third hydrocarbon feedstock may comprise any feedstock regardless of the boiling range. Suitable hydrocarbon-based feedstocks include crude oil or heavy oil, heavy diesel oil, straight run diesel oil, deasphalted oil, kerosene, jet fuel, circulating oil from upstream FCC (fluid catalytic cracking) reactors, etc. Including purified petroleum fractions. Without limiting the subject of the present invention, suitable first and second hydrocarbonaceous feedstocks generally have different boiling ranges, and the first hydrocarbonaceous feedstock is generally , Having a boiling range that is higher than the second boiling range (at least 5 ° C., more usually at least 10 ° C., and most typically at least 25 ° C., as measured from the intermediate volume boiling point in the boiling range). Suitable first and second ingredients will generally have at least one different physicochemical parameter (eg, molecular composition, boiling range, etc.). The design speed of adding the first feedstock to the second feedstock added to the third feedstock (plus the fourth, fifth feedstock, etc.) is generally The total feed will be greater than the total feed to the second reactor. The total feed rate to the second reactor is typically about 25 liquid vol% (or less) to about 90 liquid vol of the total feed rate to the first reactor as measured at standard conditions. % (Or more). In the most preferred design, the total rate to the second reactor will be between about 40 liquid vol% and about 80 liquid vol%.

Suitable interbed separators include in particular high temperature separators, such high temperature separators further configured to contain at least a portion of the second feedstock and / or a steam feedstock that generally contains hydrogen. The steam raw material may or may not be optional. In a particularly preferred alternative embodiment of the inventive subject matter, the hydrogen concentration of the hydrogen-containing feedstock may vary substantially, and in some configurations, the hydrogen concentration is about 50 vol% and 95 vol% (or more). While it may be between, it is envisaged that the concentration of hydrogen may be low (eg, between 1 vol% and 50 vol%) or substantially zero. In such cases where the hydrogen-containing feed is substantially free of hydrogen (ie, less than 1 vol%), it is preferred that the stream contain primarily light-end material (ie, material that leaves the separator as a gaseous component). . It is also recognized that the steam feed is supplied from that source without additional preheating. Generally, the steam source will be from a makeup gas compressor or from a recirculation gas compressor. The temperature of the steam to the interbed separator is 26.7 ° C to 176.7 ° C ( 80 ° F to 350 ° F ) , more typically 51.7 ° C to 148.9 ° C ( 125 It can be in the range from ° F to 300 ° F ) and most commonly in the range from 65.6 ° C to 135 ° C ( 150 ° F to 275 ° F ) . Additional steam preheating is possible and is only advantageous to some extent that it can improve plant thermal efficiency, but may add additional capital costs.

A suitable interbed separator preferably operates at or near the pressure in the first hydrotreating reactor and at or above the pressure of the second hydrotreating reactor. It should be particularly recognized that Accordingly, a suitable interbed separator will generally operate between about 3.45 to 16.55 MPa ( 500 to 2400 psi ) . However, where appropriate, the pressure may be lower than 4.83 MPa (700 psi), low pressure is particularly contemplated, generally between 4.83 2.76 MPa (400 psi to 700), also it It should be recognized that: Similarly, if hydrotreating conditions allow, the interbed separator may operate at a pressure of 16.55 MPa ( 2400 psi ) or higher, and a suitable high pressure is 16.55 to 27.58 MPa ( 2400 to 4000 psi ). Pressure during and above. Due to the relatively high partial pressure of hydrogen in the separator (hydrogen may be hydrogen recycled in the plant), the effective hydrocarbon vapor partial pressure is less than 1.38 MPa ( 200 psi ) , more commonly Is assumed to be in the range between about 0.55 MPa and 1.24 MPa ( 80 psi to 180 psi ) , and most commonly in the range between about 0.21 MPa and 1.03 MPa ( 30 psi to 150 psi ). The

  In a particularly envisaged aspect of the present inventive subject matter, the interbed separator is such that the temperature of the hydrogenated product from the first hydrotreating reactor vaporizes at least a portion of the second feedstock. Is assumed to work. Thus, in a particularly preferred configuration, at least a portion of the hydrogenated product is gaseous or vapor phase and at least a portion of the second feedstock (eg, at least 50%, more generally at least at least 75%, even more typically at least 85%, and most commonly at least 80% or 100%) will be vaporized by the heat of the first feedstock. Accordingly, it should be appreciated that the energy required to operate the second hydrotreating reactor will be provided primarily by the heat and pressure of the first hydrotreating reactor.

For a particular temperature, the first reactor preferably operates at about 343.3 ° C. ( 650 ° F. ) and the interbed separator operates from about 332.2 ° C. to about 315.6 ° C. (about 630 ° C.). It is envisioned that the second reactor will preferably operate at a temperature of between about 315.6 ° C. ( 600 ° F. ) , preferably operating at a temperature between 0 ° F. and about 600 ° F. . However, it should be recognized that the pressure and temperature may vary accordingly depending on the particular feedstock of the first and second reactors. Regarding temperature adjustment of the second hydrotreater, the temperature of the second hydrotreating reactor is adjusted by supplying at least a portion of the second feedstock, or additional feedstock to the second reactor. Please recognize that it is good.

  Moreover, it should be appreciated that the product from the first reactor (ie, the first feed) preheats and vaporizes at least a portion of the second feed. As a result, the steam thus generated contains one or both feedstocks (generally in the same boiling range), and the steam thus generated is in the envisaged configuration (one or more catalysts). It is envisioned to be fed to a second reactor (which may include a bed). The remainder of the liquid from the first feed of the interbed separator, which is cooled somewhat from the vaporization of the second feed, is fed directly to the first feed product stripper without additional stripper preheating. It is also possible that The intermediate pressure to the stripper in the feed stream (the pressure set between the operating pressure of the interbed separator and the stripper pressure) flash drum provides a means to safely reduce the pressure, and from the stripper feed It is also envisioned that it may be included to recover dissolved hydrogen. The remaining liquid from the first feed of the interbed separator may pass through a device (eg, heat exchanger, pump, etc.) other than the intermediate pressure flash drum on its way to the first feed product stripper. It is also envisaged.

  Due to the integration of the two hydroprocessing reactors into the assumed configuration, the costs for the assumed plant construction and operation will be significantly reduced. For example, it is envisaged that the cost for a hydrogen recycle compressor in the contemplated configuration is substantially lower than the cost for two independent recycle compressors. Moreover, a common set of fraction columns (referred to herein as gas plants) designed to separate light hydrocarbon fractions can be used downstream of the product stripper column, It is envisioned that it will be installed at substantially less expense than two independent gas plants. In yet another aspect of the present inventive subject matter, the energy required to operate the second hydroprocessing reactor will be provided primarily by the heat and pressure of the first hydroprocessing reactor. I want you to recognize that. As a result, it is envisaged that the second heater for the second reactor may be omitted.

  In addition, the product of the second hydroprocessing reactor (here low boiling point material) absorbs light hydrocarbon compounds that cannot be condensed (ie at least partly) under typical hydroprocessing operating conditions (temperature and pressure). Recognize that it is well suited for removal. By removing these non-hydrogen compounds from the recycle gas, the hydrogen-rich recycle gas to the first reactor section is purified. Compounds that will be removed from the recycle gas (absorbed by the product from the second reactor) include methane, ethane, propane, and butane. Purification of the hydrogen-rich recycle gas advantageously removes inactive light-end compounds and also increases the hydrogen partial pressure, thereby reducing the size of the equipment (eg reactor) and the required hydroprocessing catalyst Will.

  In yet a further aspect, by fluidly coupling the first reactor to the second reactor, the second reactor is a general independent design designed only to process a light second feedstock. It will be appreciated that it operates at significantly higher pressures, thereby significantly reducing the amount of catalyst required for the second reactor. This reduction in the amount of catalyst in the second reactor largely offsets the additional costs associated with the design of the second reactor at high pressure.

  The size and capacity of the envisaged hydroprocessing reactor will generally depend at least in part on the particular feedstock and on the overall throughput of the hydroprocessing plant. Thus, all known hydroprocessing reactors are envisioned to be suitable for use herein. Thus, the characteristics of the catalyst may vary significantly. However, preferred hydroprocessing catalysts may include catalysts comprising cobalt, molybdenum, and / or nickel dispersed on a support (eg, alumina extrusion).

  Suitable configurations may include additional hydroprocessing reactors (i.e., third reactor, fourth reactor, etc.) and separation devices, containing the products of existing or aforementioned reactors, and of additional reactors It will also be appreciated that each of the additional reactors is fluidly coupled to an existing or previously described reactor via a separator that removes at least one component of the additional feedstock. It is envisioned that all known commercially available components may be used with respect to the components in the envisaged configuration (eg, piping, hydroprocessing reactor, compressor, heat exchanger, etc.). . Moreover, the envisaged configuration may also be realized in a new plant, but it is particularly preferred that the separator and the second hydroprocessing reactor are integrated as an improvement to an existing hydroprocessing plant. .

  Accordingly, a method for operating a plant may include steps in which a first hydrotreating reactor, a second hydrotreating reactor, and an interbed separator that accommodates the first feedstock and the second feedstock are provided. . In a further step, the interbed separator is fluidly coupled to the first and second hydroprocessing reactors. In yet a further step, the first hydrotreated feed is used to preheat and vaporize at least a portion of the second feed, thereby preheated and at least partially vaporized second. 2 and, in another step, at least a portion of the preheated and at least partially vaporized second raw material is mixed with the remaining second raw material to produce a second hydrotreatment Supplied into the reactor. The same considerations apply as described above for the first and second hydrotreating reactors, interbed separators, feedstocks and feedstocks, hydrotreated products, and hydrotreated products. The

  Accordingly, specific configurations and methods for improved hydroprocessing are disclosed. However, it will be apparent to those skilled in the art that many more modifications besides those already described are possible without departing from the spirit of the invention. The subject matter of the invention is therefore not to be restricted except in the spirit of the claims. Moreover, in interpreting both the specification and the claims, all terms should be interpreted in the broadest possible manner consistent with the context. In particular, the terms “comprising” and “including” mean that a referenced element, component, or step is present or utilized with another element, component, or step not expressly referenced, Or to be construed as a reference to an element, component or step in a non-exclusive manner indicating that they are combined.

1 is a schematic diagram of an exemplary configuration of a prior art hydroprocessing plant. FIG. 1 is a schematic diagram of an exemplary configuration of a hydroprocessing plant according to the present inventive subject matter. FIG. FIG. 2 is a schematic detailed view of the flow for an interbed separator according to the present inventive subject matter.

Claims (24)

A system for integrated hydroprocessing of a first hydrocarbonaceous feedstock and a second hydrocarbonaceous feedstock having different boiling ranges,
Comprising interline bed separation apparatus which is configured to receive the first hydrocarbon feedstock is water hydride process, and the second hydrocarbon feedstock,
The hydrotreated first hydrocarbon-based raw material has a temperature effective for preheating and vaporizing at least part of the second hydrocarbon-based raw material in the interbed separator. Thereby producing a second hydrocarbon-based feedstock that is preheated and at least partially vaporized,
The first hydrocarbon-based raw material has a higher boiling range than the second hydrocarbon-based raw material,
A first hydrotreating reactor configured to receive the first hydrocarbon-based feed and to supply the hydrotreated first hydrocarbon-based feed to the interbed separator; A second hydrotreating reactor configured to receive at least a portion of the preheated and at least partially vaporized second hydrocarbonaceous feedstock and produce a liquid product;
The system is further configured such that the hydroprocessed first hydrocarbon feedstock, which is the liquid product and liquid discharged from the interbed apparatus, is separately recovered from the system.   The system of claim 1, wherein the interbed separator includes at least a partial vapor-liquid equilibration stage.   The system of claim 1, wherein the interbed separator comprises at least two vapor-liquid equilibration stages.   The system of claim 1, wherein the interbed separator is a tray column or a pack column.   The system of claim 1, wherein the first feedstock comprises hydrotreated gas oil or circulating oil from a fluid catalytic cracking reactor.   The system of claim 1, wherein the second feedstock comprises diesel oil or circulating oil from a fluid catalytic cracking reactor.   The system of claim 1, wherein the interbed separator further contains a hydrogen-containing stream.   The system of claim 7, wherein the hydrogen-containing stream is recycled in the plant.   The system of claim 7, wherein at least a portion of the hydrogen-containing stream is a make-up hydrogen stream.   The system of claim 1, wherein the interbed separator is operable at a pressure between 3.45 MPa and 16.55 MPa.   The system of claim 10, wherein the second hydrotreating reactor is operable at a pressure between 4.83 MPa and 13.79 MPa.   The system of claim 1, wherein at least a portion of the second feedstock is supplied to the second hydroprocessing reactor.   The system of claim 1, wherein the third feed is fed to a second hydroprocessing reactor.   The system of claim 12, wherein a portion of the second feedstock has a temperature effective to adjust the temperature of the second hydrotreating reactor.   The system of claim 12, wherein a portion of the second feedstock controls the recovery of light boiling range materials from the hydrotreated first feedstock of the interbed separator.   The system of claim 1, wherein the interbed separator and the second reactor are integrated into an existing hydroprocessing plant as an improvement.   The first hydrotreating reactor receives a first total feed volume, the second hydrotreating reactor receives a second total feed volume, and the second total feed volume is a first total feed volume. The system according to claim 1, wherein the system is between 25 vol% and 90 vol%.   The first hydrotreating reactor receives a first total feed volume, the second hydrotreating reactor receives a second total feed volume, and the second total feed volume is a first total feed volume. The system according to claim 1, wherein the system is between 40 vol% and 80 vol%. A method of hydrotreating at least two separate hydrocarbonaceous feedstocks to form at least two separate hydrotreated products comprising:
Coupling the first hydrotreating reactor that receives the first hydrocarbonaceous feedstock to the interbed separator to allow the hydrotreated first hydrocarbonaceous feedstock to flow , wherein the interbed separator is receiving a first hydrocarbon feedstock is hydrotreated and the second hydrocarbon feedstock, the inter bed separation apparatus in the second hydrotreating reactor, the second to the hydrocarbon feedstock flowing Combined with
The first hydrocarbon raw material has a higher boiling range than the second hydrocarbon raw material, and the method comprises:
The first hydrocarbon-based hydrotreated first hydrocarbon material is used to preheat and vaporize at least a portion of the second hydrocarbon-based material, whereby preheated and at least partially vaporized first Producing a hydrocarbon feedstock of 2;
Supplying at least a portion of the preheated and at least partially vaporized second hydrocarbonaceous feedstock to the second hydrotreating reactor;
Separately recovering the hydrotreated first hydrocarbon-based fluid from the interbed separator and the hydrotreated second hydrocarbon-based fluid from the second hydrotreating reactor; A method of hydrotreating.   20. The method of claim 19, wherein the first feed comprises a gas oil boiling range material and the second feed comprises a material having a lower boiling range than light oil.   20. The interbed separator operates at a pressure between 3.45 Mpa and 16.55 Mpa, and the second hydrotreating reactor operates at a pressure between 4.83 MPa and 13.79 MPa. the method of.   The method of claim 19, wherein the second hydrotreating reactor produces a product that absorbs components from the recycle gas produced at least partially in the first hydrotreating reactor. A system for integrated hydroprocessing of separate first and second feedstocks having different boiling ranges,
Receiving a first hydrocarbon feedstock is hydrotreated and the second hydrocarbon feedstock comprises inter bed separation apparatus for forming a first hydrotreated liquid, first with hydrotreated The hydrocarbon-based raw material of the second hydrocarbon-based raw material is preheated and vaporized by at least a part of the second hydrocarbon-based raw material in the inter-bed separation device, thereby preheated and at least partially vaporized. Produce raw materials,
The hydrotreated first hydrocarbon-based material is provided by the first hydroprocessing reactor, and at least a portion of the pre-heated and at least partially vaporized second hydrocarbon-based material is hydrogenated. Fed to a second hydrotreating reactor that produces hydrotreated product;
The first hydrocarbon-based raw material has a higher boiling range than the second hydrocarbon-based raw material;
At least a portion of the second hydrocarbon-based raw material is supplied to the second hydrotreating reactor;
The interbed separator is coupled to the first hydroprocessing reactor such that the hydrotreated first hydrocarbonaceous feedstock flows, and the interbed separator is preheated and at least partially Coupled to the second hydrotreating reactor so that the vaporized second hydrocarbon-based raw material flows ;
The system is further configured such that the system can separately collect the first hydrotreated liquid and the hydrotreated product. A system for integrated hydroprocessing of separate first and second feedstocks having different boiling ranges,
Comprising interline bed separation apparatus which receives a first hydrocarbonaceous feedstock, and the second hydrocarbon feedstock is hydrotreated first hydrocarbon feedstock, a second hydrocarbon which is hydrotreated Preheating and vaporizing at least a portion of the feedstock, thereby producing a preheated and at least partially vaporized second hydrocarbonaceous feedstock;
At least a portion of the hydrotreated first hydrocarbon-based feedstock is provided by the first hydrotreating reactor and is preheated and at least partially vaporized at least one of the second hydrocarbon-based feedstocks. Is fed to a second hydrotreating reactor that produces the product,
The first hydrocarbon-based raw material has a higher boiling range than the second hydrocarbon-based raw material;
The interbed separator is coupled to the first hydroprocessing reactor such that the hydrotreated first hydrocarbonaceous feedstock flows, and the interbed separator is preheated and at least partially Coupled to the second hydrotreating reactor so that the vaporized second hydrocarbon-based raw material flows;
A third feedstock is supplied to the second hydrotreating reactor ;
A system for separately recovering a hydrotreated first hydrocarbon-based fluid from an interbed separator and a hydrotreated product from a second hydrotreating reactor .

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