Coil-wound heat exchanger for hydrogenation or hydrogenation

Abstract

To provide a device and a method for hydro-conversion or hydrotreatment which have improved energy efficiency and reduced operating cost.SOLUTION: The present invention comprises at least one coil-wound heat exchanger S-1. The coil-wound heat exchanger is a single-pass heat exchanger formed by a vertical chamber in which one or more bundles of tubes are helically wound around a central core, as numerous superposed layers. The present invention heats a hydrocarbon feedstock / hydrogen stream mixture and directly distributes it to a hydrotreatment or hydro-conversion reaction section R-1. The present invention also cools the reaction effluent from the hydrotreatment or hydro-conversion reaction section R-1.SELECTED DRAWING: Figure 2

Description

[Technical Field]

[0001] The present invention relates to the field of devices and methods for hydrogenation conversion (e.g., hydrocracking of heavy feedstocks) and hydrogenation treatment (e.g., hydrodemetallation, hydrodenitrification, and / or hydrodesulfurization of residues or gaseous oils). [Background technology]

[0002] Shell-and-tube heat exchangers have been known for a long time. Examples of this type of heat exchanger are described in Patent Documents 1-3. Well-known shell-and-tube heat exchangers are, for example, BEU or DEU standard heat exchangers, which include a bundle of U-shaped exchange tubes (U-tube bundles). These standards are defined by the Tubular Exchanger Manufacturers Association (TEMA; www.tema.org).

[0003] Coil-wound heat exchangers, also known as spiral-wound heat exchangers, are well known to those skilled in the art. Therefore, Patent Document 4 describes a coil-wound heat exchanger and its use in an LNG liquefaction method. Other configurations of coil-wound heat exchangers are described, for example, in Patent Documents 5 and 6.

[0004] The use of coil-wound heat exchangers, like other heat exchangers, has been envisioned in various ways, such as in methods for converting heavy feedstocks (Patent Documents 7 and 8) or in cryogenic air separation methods (Patent Document 9). However, this use has not resulted in any significant layout modifications compared to when other types of heat exchangers (e.g., shell-and-tube or plate heat exchangers) are used. [Prior art documents] [Patent Documents]

[0005] [Patent Document 1] U.S. Patent No. 2978226 [Patent Document 2] European Patent Application Publication No. 1113238 (Japanese Patent Publication No. 2001-194076) [Patent Document 3] European Patent Application Publication No. 2975353 [Patent Document 4] European Patent Application Publication No. 1367350 [Patent Document 5] International Publication No. 2004 / 063655 [Patent Document 6] International Publication No. 2014 / 067223 [Patent Document 7] U.S. Patent No. 8152994 [Patent Document 8] U.S. Patent No. 8,277,637 [Patent Document 9] U.S. Patent No. 671879 [Overview of the Initiative] [Means for solving the problem]

[0006] (overview) Within the scope of the above circumstances, the first objective of the description of the present invention is to improve devices and methods for hydrogenation conversion or hydrogenation treatment, particularly in terms of energy efficiency and operating costs.

[0007] According to the first aspect, the above-mentioned objectives and other advantages are provided for a device for the hydrogenation conversion or hydrogenation treatment of hydrocarbon feedstocks, At least one coil-wound heat exchanger; the coil-wound heat exchanger is a single-flow heat exchanger formed by a vertical chamber, in which one or more bundles of tubes are wound helically around a central core as a number of superimposed layers, Heating hydrocarbon feedstock and, optionally, a hydrogen flow or a mixture of hydrocarbon feedstock / hydrogen flow, and directly passing this through the reaction section of the hydrogenation treatment or hydrogenation conversion, and Cooling reaction effluents from the reaction section of a hydrogenation or hydrogenation process. Suitable for; A first mixing section suitable for mixing hydrocarbon feedstock with a hydrogen flow; the first mixing section may be located upstream or downstream of at least one coil-wound heat exchanger; Hydrogenation or hydrogenation reaction section suitable for hydrogenating or hydrogenating hydrocarbon feedstocks; A high-pressure cryogenic separator suitable for separating at least a portion of the cooled reaction effluent into a first liquid effluent containing at least one light fraction and a first gaseous effluent containing hydrogen; and A separation column suitable for separating a first liquid outflow containing at least one light fraction into a bottom liquid and a top outflow. Obtained by a device that includes this.

[0008] According to one or more embodiments, the device further includes a first compression section, which is suitable for compressing a first gaseous effluent containing hydrogen and for recirculating it to a first mixing section or at least one coil-wound heat exchanger.

[0009] According to one or more embodiments, the reaction section of the hydrogenation treatment or hydrogenation conversion includes at least one reactor, which includes at least one catalyst comprising at least one element selected from Group VIII of the periodic table.

[0010] According to one or more embodiments, the reactor includes at least one fixed bed.

[0011] According to one or more embodiments, the reactor includes at least one bubbling bed.

[0012] According to one or more embodiments, the device includes a device for filtering the hydrocarbon feedstock at the inlet of the unit. According to one or more embodiments, the filtering device is disposed downstream of a heat exchanger, which is suitable for heating the hydrocarbon feedstock to a temperature of 50 °C to 100 °C or 150 °C to 230 °C.

[0013] According to one or more embodiments, the device includes a feedstock drum, which is suitable for containing the optionally filtered hydrocarbon feedstock. The drum is disposed upstream of a pump for supplying the coiled heat exchanger S-1.

[0014] According to one or more embodiments, the device includes a single coiled heat exchanger.

[0015] According to one or more embodiments, the device further includes a first bypass, which is suitable for directly flowing a part of the hydrocarbon feedstock or a mixture of the hydrocarbon feedstock / hydrogen stream from the inlet of the coiled heat exchanger to the outlet of the coiled heat exchanger.

[0016] According to one or more embodiments, the device further includes a high-pressure high-temperature separator, which is suitable for separating the cooled reaction effluent into a first liquid effluent containing at least one heavy fraction and a first gaseous effluent containing a light fraction, and the first gaseous effluent is flowed to a high-pressure low-temperature separator.

[0017] According to one or more embodiments, the device further includes an intermediate-pressure high-temperature separator suitable for separating a first liquid effluent containing at least one heavy fraction into a second liquid effluent containing at least one heavy fraction and a second gaseous effluent containing a light fraction, the second liquid effluent being passed through a separation tower.

[0018] According to one or more embodiments, the device further includes an intermediate-pressure cryogenic separator suitable for separating a first liquid effluent containing at least one light fraction into a second liquid effluent containing at least one light fraction and a second gaseous effluent containing hydrogen, the second liquid effluent being passed through a separation column.

[0019] According to one or more embodiments, the medium-pressure cryogenic separator is suitable for separating a second gaseous effluent containing a light fraction.

[0020] According to one or more embodiments, the reaction section of the hydrogenation treatment or hydrogenation conversion is suitable for directly flowing the reaction effluent through a coil-wound heat exchanger.

[0021] According to one or more embodiments, the device further includes at least a second heat exchanger and / or a steam generator and / or a first air cooler, each of which is suitable for cooling and / or condensing a first gaseous effluent containing a light fraction.

[0022] According to one or more embodiments, the device further includes an amine scrubbing tower, which is suitable for removing at least a portion of H2S from a first gaseous effluent containing hydrogen.

[0023] According to one or more embodiments, the device further includes a second air cooler suitable for condensing a second gaseous effluent containing a light fraction and for flowing the condensed second gaseous effluent containing the light fraction to a medium-pressure low-temperature separator.

[0024] According to one or more embodiments, the device further includes a third heat exchanger, which is suitable for heating a first or second liquid effluent containing at least one light fraction and / or cooling a bottom liquid from a separation column.

[0025] According to one or more embodiments, the device further includes a fourth heat exchanger, which is suitable for cooling or heating a first or second liquid effluent containing at least one heavy fraction.

[0026] According to one or more embodiments, the device further includes a third air cooler, which is suitable for condensing top flow from a separation column.

[0027] According to one or more embodiments, the device further includes a reflux drum suitable for separating top effluent from a separation column into a top gaseous fraction and at least one hydrocarbon liquid fraction.

[0028] According to a second aspect, the above-mentioned objectives and other advantages are achieved by a method for hydrogenation conversion or hydrogenation treatment of hydrocarbon feedstock, comprising the following steps: A step of heating a hydrocarbon feedstock and optionally a flow of hydrogen or a mixture of hydrocarbon feedstock and hydrogen flow using at least one coil-wound heat exchanger, and passing this directly to a reaction section of a hydrogenation treatment or hydrogenation conversion, wherein the coil-wound heat exchanger is a single-flow heat exchanger formed by a vertical chamber, in which one or more bundles of tubes are spirally wound around a central core as a number of superimposed layers; A step of mixing hydrocarbon feedstock with a hydrogen flow in a first mixing section, wherein the mixing can be performed before or after a heating step; A step of cooling reaction effluents from the reaction section of a hydrogenation or hydrogenation treatment using at least one coil-wound heat exchanger; A step of hydrogenating or hydrogenating a hydrocarbon feedstock in a hydrogenation or hydrogenation reaction section, wherein the reaction section comprises at least one reactor, and the reactor comprises at least one catalyst comprising at least one element selected from Group VIII of the periodic table; A step of separating at least a portion of the cooled reaction effluent in a high-pressure cryogenic separator and passing through a first liquid effluent containing at least one light fraction and a first gaseous effluent containing hydrogen; and A process of separating a first liquid outflow containing at least one type of light fraction in a separation column and circulating the bottom liquid and the top outflow. It is obtained by a method that includes the following.

[0029] According to one or more embodiments, the method further includes the step of compressing a first gaseous effluent containing hydrogen by a first compression section and recirculating it to a first mixing section or at least one coil-wound heat exchanger.

[0030] According to one or more embodiments, the hydrogenation or hydrogenation of a hydrocarbon feedstock is carried out under hydrogenation or hydrogenation conditions, for example, under at least one of the following operating conditions: The temperature ranges from approximately 200°C to approximately 460°C. The total pressure is approximately 1 MPa to 20 MPa; The overall space velocity per hour of the liquid supply material is approximately 0.05h -1 ~about 12h -1 is; A hydrogen stream contains approximately 50% to 100% hydrogen relative to its volume; The amount of hydrogen relative to the liquid hydrocarbon feedstock is approximately 50 Nm³. 3 / m 3 ~about 2500Nm 3 / m 3 That is the case.

[0031] According to one or more embodiments, the initial boiling point of the hydrocarbon feedstock is greater than 120°C. For example, the hydrocarbon feedstock may be selected from the following feedstocks: atmospheric distillates, vacuum distillates, atmospheric or vacuum residues, or effluents from Fischer-Tropsch units. Preferably, hydrocarbon feedstocks are selected from the following feedstocks: atmospheric distillates (naphtha, petroleum, kerosene, and gas oils), direct distillation or conversion units of crude oil, e.g., FCCs (fluid catalytic cracking units), vacuum distillates derived from coker or bis-breaking units, e.g., gas oils, LCOs (light cycle oils) derived from catalytic cracking units, feedstocks originating from units for extracting aromatic compounds, lubricant bases or bases derived from solvent dewaxing of lubricant bases, ATRs (atmospheric residues) and / or VRs (vacuum residues) and / or distillates originating from fixed-bed or bubbling-bed methods for desulfurization or hydrogenation conversion of deasphalt oils, deasphalt oils, effluents from Fischer-Tropsch units, vegetable oils alone or in mixtures, or animal fats. The above list is not limiting.

[0032] According to one or more embodiments, the hydrocarbon feedstock contains at least 5% by weight of decomposed feedstock relative to the weight of the hydrocarbon feedstock; or the hydrocarbon feedstock contains less than 5% by weight of decomposed feedstock relative to the weight of the hydrocarbon feedstock, thereby enabling a temperature rise of more than 15°C between the inlet and outlet of the reaction section (R-1) of the hydrogenation treatment or hydrogenation conversion.

[0033] According to one or more embodiments, the high-pressure cryogenic separator is operated at a pressure lower than the pressure in the reaction section of the hydrogenation treatment or hydrogenation conversion.

[0034] According to one or more embodiments, the temperature of the high-pressure low-temperature separator is 20°C to 100°C.

[0035] According to one or more embodiments, the high-pressure, high-temperature separator is operated at a pressure lower than the pressure in the reaction section of the hydrogenation treatment or hydrogenation conversion.

[0036] According to one or more embodiments, the temperature of the high-pressure, high-temperature separator is 200°C to 450°C.

[0037] According to one or more embodiments, the hydrocarbon feedstock is at a temperature of 30°C to 110°C, preferably 34°C to 100°C, at the inlet of the unit.

[0038] According to one or more embodiments, the hydrocarbon feedstock is at a temperature of 150°C to 280°C, preferably 160°C to 260°C, at the inlet of the unit.

[0039] According to one or more embodiments, the method includes a step of filtering the hydrocarbon feedstock at the inlet of the unit, after which the feedstock is optionally heated to a temperature of 50°C to 100°C or 150°C to 230°C. According to one or more embodiments, the method includes a step of holding the filtered hydrocarbon feedstock in a feedstock drum. The feedstock can be supplied to the coil-wound heat exchanger S-1 by pumping it out of the drum.

[0040] According to one or more embodiments, the temperature of the hydrocarbon feedstock and, optionally, the hydrogen flow or mixture of hydrocarbon feedstock / hydrogen flow is 30°C to 280°C, preferably 34°C to 260°C, at the outlet of the mixing section (located upstream of the coil-wound heat exchanger) and / or at the inlet of the coil-wound heat exchanger and / or at the inlet of the bypass. According to one or more particularly preferred embodiments, the above temperature is 40°C to 60°C (low-temperature scheme). According to one or more particularly preferred embodiments, the above temperature is 200°C to 250°C (high-temperature scheme).

[0041] According to one or more embodiments, the temperature of the hydrocarbon feedstock and / or hydrogen stream or the mixture of heated hydrocarbon feedstock / hydrogen stream is 200°C to 460°C, preferably 240°C to 440°C, at the outlet of the coil-wound heat exchanger.

[0042] According to one or more embodiments, the temperature of the heated hydrocarbon feedstock / hydrogen flow mixture is 200°C to 460°C, preferably 240°C to 440°C, at the inlet of the reaction section for hydrogenation or hydrogenation conversion.

[0043] According to one or more embodiments, the temperature of the reaction effluent is 205°C to 475°C, preferably 245°C to 455°C, at the outlet of the reaction section of the hydrogenation treatment or hydrogenation conversion and / or at the inlet of the coil-wound heat exchanger.

[0044] According to one or more embodiments, the temperature of the cooled reaction effluent is 70°C to 450°C, preferably 80°C to 380°C, at the outlet of the coil-wound heat exchanger.

[0045] According to a third aspect, the above-mentioned objectives and other advantages are obtained by the use of a coil-wound heat exchanger in a hydrogenation or hydrogen conversion method, the coil-wound heat exchanger being a single-flow heat exchanger formed by a vertical chamber, in which one or more bundles of tubes are spirally wound around a central core as a number of superimposed layers.

[0046] According to one or more embodiments, the coil-wound heat exchanger is Heating a mixture of hydrocarbon feedstock / hydrogen flow and directly passing it through the reaction section of the hydrogenation treatment or hydrogenation conversion; and Cooling effluent from the reaction section of a hydrogenation or hydrogenation process. It is used for that purpose.

[0047] The devices, methods, and embodiments of use mentioned above, as well as other features and advantages, will become clear as you read the following description. These descriptions are given for illustrative purposes only, are not limiting, and will be illustrated with reference to the following drawings. [Brief explanation of the drawing]

[0048] [Figure 1] Figure 1 shows the layout of a reference device, in which the feedstock for the reaction section is preheated by the reaction effluent in a train of shell-and-tube heat exchangers, then heated in a furnace, and subsequently enters the reaction section. [Figure 2] Figure 2 shows the device layout according to the description of the present invention, in which the feed material for the reaction section is heated by the reaction effluent in a coil-wound heat exchanger S-1 and then enters the reaction section directly. [Modes for carrying out the invention]

[0049] (Detailed explanation) The description of the present invention relates to devices and methods for hydrogenation conversion, for example, devices and methods for hydrocracking heavy feedstocks, such as vacuum residues or vacuum gas oils. The description of the present invention also relates to devices and methods for hydrogenation treatment, for example, devices and methods for hydrodemetallation, hydrodenitrification and / or hydrodesulfurization of residues or gas oils.

[0050] Referring to Figure 1, the reference device for the hydrogenation or hydrogenation of hydrocarbon feedstocks, such as gaseous oil, vacuum distillates, atmospheric or vacuum residues, or effluents from Fischer-Tropsch units, is - First section for mixing hydrocarbon feedstock (line 1) and hydrogen flow (line 4); - One or more shell-and-tube heat exchanger trains E-1A / B / C / D and E-1E / F / G / H for preheating the hydrocarbon feedstock / hydrogen flow mixture (hereinafter referred to as the hydrocarbon mixture) (line 5) derived from the first mixing section with the reaction effluent (line 9) from the hydrogenation or hydrogenation conversion reaction section R-1; - Furnace F-1 at the reactor inlet for heating a preheated hydrocarbon mixture (line 7) originating from one or more trains E-1 of a shell-and-tube heat exchanger, and for flowing the heated hydrocarbon mixture (line 8) to the hydrogenation or hydrogenation conversion reaction section R-1; - Hydrogenation or hydrogenation reaction section R-1; - Depending on the circumstances, a bypass (bypass line 19); this allows a portion of the hydrocarbon mixture (line 5) to bypass one or more trains E-1 of the shell-and-tube heat exchanger, thereby regulating the reaction temperature of the hydrogenation or hydrogenation conversion reaction section R-1; - Depending on the circumstances, a high-pressure, high-temperature separator B-1; its feedstock is formed by reaction effluent (line 11) that has been cooled after passing through train E-1 of a shell-and-tube heat exchanger, and it passes through a first liquid effluent (line 22) containing at least one heavy fraction and a first gaseous effluent (line 14) containing a light fraction; - High-pressure cryogenic separator B-2; its feedstock is formed from at least a portion of the reaction effluent (lines 11 and 14) that originates from the reaction section R-1 of the hydrogenation or hydrogenation conversion and has been cooled after passing through one or more trains E-1 of the shell-and-tube heat exchanger, and passes through a first liquid effluent (line 25) containing at least one light fraction and a first gaseous effluent (line 16) containing hydrogen; - Optionally, a second heat exchanger E-3; this is for cooling at least a portion of the reaction effluent (or, optionally, the first gaseous effluent containing light fractions originating from the high-pressure, high-temperature separator B-1); - Optionally, a first air cooler A-1; which is intended to condense at least a portion of the reaction effluent (or, optionally, a first gaseous effluent containing a light fraction originating from the high-pressure high-temperature separator B-1 and possibly further from the second heat exchanger E-3); - Depending on the circumstances, an amine washing tower C-2; this makes it possible to remove at least a portion of H2S from the first gaseous effluent (also called recirculated hydrogen) (line 16) containing hydrogen originating from the high-pressure cryogenic separator B-2; - Depending on the circumstances, a first compression section K-1; this is for compressing recirculated and amine-washed hydrogen (line 17); - Depending on the circumstances, a second compression section K-2; this is for compressing the replenishment hydrogen (line 2); - A second section for mixing, depending on the circumstances, recirculated, washed, and compressed hydrogen (line 18) and compressed replenishment hydrogen (line 3); - Depending on the circumstances, a medium-pressure high-temperature separator B-3; its feedstock is a first liquid outflow (line 22) containing at least one heavy fraction originating from the high-pressure high-temperature separator B-1, one of which is a second liquid outflow (line 26) containing at least one heavy fraction, which is supplied to the separation tower C-1; - Depending on the circumstances, a second air cooler A-2; which condenses the second gaseous outflow (line 23) containing the light fraction originating from the medium-pressure high-temperature separator B-3, and allows the condensed second gaseous outflow (line 24) containing the light fraction to flow through; - Optionally, a medium-pressure cryogenic separator B-4; this is for separating a first liquid outflow (line 25) containing at least one light fraction originating from the high-pressure cryogenic separator B-2 (and optionally, a second gaseous outflow (line 23) containing a light fraction originating from the medium-pressure high-temperature separator B-3 (and optionally, condensed in the second air cooler A-2 (line 24)), and for facilitating the flow of the second liquid outflow (lines 27 and 28) containing at least one light fraction into the separation column C-1, and for removing a second gaseous outflow containing hydrogen; - Separation column C-1 (for example, a conventional fractionation column or stripping column using fluid added via line 32); this is for circulating the bottom liquid (line 39) and the top effervescence, starting from the liquid effluent from high-pressure cryogenic separator B-2 (line 25), possibly from high-pressure high-temperature separator B-1 (line 22), possibly from medium-pressure separator B-3 (line 26), and possibly from medium-pressure cryogenic separator B-4 (line 27); - Optionally, a third heat exchanger E-4; this is for heating the feedstock (line 25, possibly line 27) to separation column C-1 and / or cooling the bottom liquid (line 39) from separation column C-1; - Depending on the circumstances, a fourth heat exchanger (not shown); which is suitable for cooling or heating the first or second liquid effluent containing at least one heavy fraction; - Depending on the circumstances, a third air cooler A-3; this is for condensing the top spill from separation tower C-1; and - Depending on the circumstances, reflux drum B-6; this is for separating the top effluent into a gaseous top fraction (e.g., sour gas) (line 35) and a hydrocarbon liquid fraction (e.g., naphtha) (line 38). Includes.

[0051] Figures 1 and 2 show that identical devices for hydrogenation or hydrogenation conversion have the same reference numerals (numbers).

[0052] Referring to Figure 2, the device according to the first aspect of the description of the present invention includes elements of the reference device, with the exception that one or more trains E-1 (Figure 1) of shell-and-tube heat exchangers are replaced by at least one coil-wound heat exchanger S-1. It is also important to note that the reactor inlet furnace F-1 for heating the feedstock used in the reference device (Figure 1) is no longer necessary in the device according to the description of the present invention. According to one or more embodiments, the feedstock for the reaction section enters the reaction section directly after being heated only by the reaction effluent, preferably by a single coil-wound heat exchanger S-1.

[0053] Specifically, the inventors have demonstrated that a hydrogenation or hydrogenation device that includes at least one coil-wound heat exchanger S-1 instead of one or more shell-and-tube heat exchanger trains E-1 to heat the feedstock of the hydrogenation or hydrogenation reaction section R-1 with the reaction effluent allows for the elimination of a reactor inlet furnace F-1 provided for heating the feedstock.

[0054] The coil-wound heat exchanger S-1 is a single-flow heat exchanger formed by a vertical chamber, in which one or more bundles of tubes are spirally wound around a central core as a number of superimposed layers (see Technique de l'Iingenieur, J 3 601 V2 paragraph 4.2). The exchanger enables heat exchange between a fluid flowing through the chamber and at least one fluid flowing through the tube bundles.

[0055] According to one or more embodiments, the coil-wound heat exchanger S-1 is used with a high-temperature fluid on the shell side and a low-temperature fluid on the tube side.

[0056] According to one or more embodiments, the coil-wound heat exchanger S-1 is used with a high-temperature fluid on the tube side and a low-temperature fluid on the shell side.

[0057] In the example shown in Figure 2, the first mixing section is located upstream of at least one coil-wound heat exchanger S-1. In one or more embodiments, the first mixing section is located downstream of at least one coil-wound heat exchanger S-1.

[0058] In the example from Figure 2, the coil-wound heat exchanger (S-1) is positioned to heat a mixture of hydrocarbon feedstock / hydrogen flow. Alternatively, the coil-wound heat exchanger (S-1) may be configured to heat the hydrocarbon feedstock and optionally the hydrogen flow.

[0059] It should also be noted that the device described in this invention may include a starter furnace (not shown) located at the inlet of the hydrogenation or hydrogenation reaction section (i.e., on line 7 between S-1 and R-1). On the other hand, the starter furnace is used solely for starting the method; the method does not include a heating step between the coil-wound heat exchanger and the hydrogenation or hydrogenation reaction section during stable operation.

[0060] According to one or more embodiments, the initial boiling point of the hydrocarbon feedstock is higher than 120°C. For diesel, the initial boiling point is generally about 150°C, and the distillation range is typically 170°C to 390°C. For atmospheric residue, the initial boiling point is typically higher than 300°C, preferably 340°C to 380°C. For vacuum residue, the initial boiling point is typically 450°C to 600°C, preferably 500°C to 550°C. Light vacuum gas oil (LVGO) is characterized by a distillation range of 300°C to 430°C, preferably 340°C to 400°C. Heavy vacuum gas oil (HVGO) is characterized by a distillation range of 400°C to 620°C, preferably 440°C to 550°C. Therefore, the usable feedstocks are within a wide range of boiling points.

[0061] According to one or more embodiments, the hydrocarbon feedstock contains a compound that boils at over 340°C in an amount of at least 10% by volume, generally at least 20% by volume, and often at least 80% by volume.

[0062] According to one or more embodiments, the nitrogen content of the hydrocarbon feedstock is higher than 500 ppm by weight, generally 500 to 10,000 ppm by weight, more generally 700 to 4,500 ppm by weight, and even more generally 800 to 4,500 ppm by weight.

[0063] According to one or more embodiments, the sulfur content of the hydrocarbon feedstock is 0.01% to 5% by weight, generally 0.2% to 4% by weight, and more generally 0.5% to 3% by weight.

[0064] According to one or more embodiments, the hydrocarbon feedstock contains metal. According to one or more embodiments, the combined content of nickel and vanadium in the hydrocarbon feedstock is less than 10 ppm by weight, preferably less than 5 ppm by weight, and more preferably less than 2 ppm by weight.

[0065] According to one or more embodiments, the asphaltene content of the hydrocarbon supply raw material is less than 3000 ppm by weight, preferably less than 1000 ppm by weight, and more preferably less than 300 ppm by weight.

[0066] According to one or more embodiments, the reaction effluent from the reaction section R-1 of the hydrogenation or hydrogenation conversion consists of a hydrocarbon fraction, which generally, as a mixed phase, contains hydrogen, gases derived from decomposition, particularly H2S and NH3 derived from the reaction in the reaction section, in proportion to the sulfur and nitrogen content in the feedstock, and optionally includes CO2 and other gases, a light fraction originating from a secondary reaction, such as LPG (liquefied petroleum gas), and at least naphtha, and optionally includes the following hydrocarbon fractions: diesel, kerosene and / or unconverted residue, etc., depending on the properties of the feedstock and the type of reaction.

[0067] According to one or more embodiments, a first liquid effluent containing at least one heavy fraction comprises at least a portion of the heaviest fraction of the effluent from the reaction section, which may include naphtha, diesel, kerosene, and / or unconverted residue, depending on the properties of the feedstock and the type of reaction. The first liquid effluent containing at least one heavy fraction may also include an intermediate fraction of the effluent from the reaction section, which may optionally include diesel, kerosene, and / or naphtha, depending on the properties of the feedstock and the type of reaction.

[0068] According to one or more embodiments, a first gaseous effluent containing a light fraction comprises at least a portion of the lightest fraction of the reaction effluent, which contains hydrogen, gases derived from decomposition, in particular H2S and NH3 derived from the reaction section, in proportion to the sulfur and nitrogen content contained in the feedstock, and optionally CO2 and other gases, light fractions originating from secondary reactions, such as LPG, and at least naphtha.

[0069] According to one or more embodiments, the first liquid effluent comprising at least one light fraction comprises a fraction of the reaction effluent, which comprises a light fraction originating from a secondary reaction, such as LPG, and at least naphtha.

[0070] According to one or more embodiments, the first gaseous effluent containing hydrogen contains gases derived from decomposition, particularly H2S derived from the reaction section, in proportion to the sulfur content in the feedstock, and optionally contains CO2.

[0071] According to one or more embodiments, a second liquid effluent comprising at least one heavy fraction comprises the heaviest fraction of the effluent from the reaction section, which includes diesel, kerosene, and / or unconverted residue, depending on the nature of the feedstock and the type of reaction.

[0072] According to one or more embodiments, a second gaseous effluent containing a light fraction comprises a first intermediate fraction of the effluent from the reaction section, which optionally contains diesel, kerosene, and / or naphtha, depending on the nature of the feedstock and the type of reaction.

[0073] According to one or more embodiments, a second liquid effluent containing at least one light fraction comprises the heaviest fraction of the first liquid effluent containing at least one light fraction. The second liquid effluent containing at least one light fraction may also comprise a second intermediate fraction of the effluent from the reaction section, which comprises diesel, kerosene, and / or naphtha, depending on the nature of the feedstock and the type of reaction.

[0074] According to one or more embodiments, the second gaseous effluent containing hydrogen comprises at least a portion of the lightest fraction of the reaction effluent, which includes hydrogen, gases derived from decomposition, in particular H2S derived from the reaction section, in proportion to the sulfur content contained in the feedstock, and optionally CO2 and other gases.

[0075] According to one or more embodiments, the top effluent includes gases derived from decomposition, in particular H2S, optionally CO2 and other gases, LPG, naphtha and optionally stripping fluid.

[0076] According to one or more embodiments, the gaseous column top fraction includes gases derived from decomposition, particularly H2S, and optionally CO2 and other gases, such as LPG.

[0077] According to one or more embodiments, the liquid hydrocarbon fraction includes naphtha.

[0078] According to one or more embodiments, the bottom liquid comprises the heaviest fraction of the effluent from the reaction section, which includes diesel, kerosene, and / or unconverted residue, depending on the nature of the feedstock and the type of reaction.

[0079] In the device described in the present invention, the hydrogenation or hydrogenation conversion reaction section R-1 may include one or a plurality of reactors arranged in series or parallel, for example, two reactors arranged in series. Each reactor in the reaction section includes at least one catalyst bed. The catalyst may be used in a fixed bed, an expanded bed, or a bubbling bed. In the case of a catalyst used in a fixed bed, it is possible to position a plurality of catalyst beds within at least one reactor. Each reactor may be equipped with a cooling means, for example, a liquid or gaseous quench flow, which is located between two consecutive beds to control the temperature at the inlet of each bed in the reactor. On the other hand, the hydrogenation or hydrogenation conversion reactor does not have a heating means.

[0080] According to one or more embodiments, the reaction section R-1 of the hydrogenation treatment or hydrogenation conversion is the reaction section of the hydrogen cracking unit.

[0081] According to one or more embodiments, the reaction section R-1 for hydrogenation or hydrogenation is the reaction section of the unit for hydrogenation and / or desulfurization of diesel and / or kerosene and / or vacuum distillates.

[0082] According to one or more embodiments, the reaction section R-1 for hydrogenation or hydrogenation conversion is the reaction section of the unit for hydrogenation desulfurization of naphtha.

[0083] According to one or more embodiments, the reaction section R-1 for hydrogenation or hydrogenation conversion is included in a unit for hydrogenation conversion of residue or distillate or deasphalt oil in a bubbling bed.

[0084] Separation column C-1 is primarily intended to remove gases resulting from decomposition (commonly called sour gases), particularly H2S resulting from the reactions in the reaction section. This column is preferably stripped with any stripping gas, for example, a gas containing hydrogen or water vapor. Preferably, water vapor is used to perform the stripping.

[0085] According to a second aspect, the description of the present invention also relates to a method for carrying out the device according to the first aspect.

[0086] According to one or more embodiments, the operating conditions of the reaction section R-1 of the hydrogenation treatment or hydrogenation conversion include at least one of the following features: - The temperature range is approximately 200°C to 460°C, with a preference for approximately 240°C to 450°C; - The total pressure is approximately 1 to approximately 20 MPa, for example 2 to 20 MPa, preferably 2.5 to 18 MPa, and very preferably 3 to 18 MPa; - The overall hourly space velocity of the liquid feedstock for each catalytic step is about 0.05 h -1 ~ about 12 h -1 Preferably, it is about 0.05 h -1 ~ about 10 h -1 ; - The purity of the hydrogen used is about 50 vol% to 100 vol% with respect to the volume of the hydrogen feed (i.e., the mixture of recycled hydrogen / makeup hydrogen); - The amount of hydrogen with respect to the liquid hydrocarbon feedstock is about 50 Nm 3 / m 3 ~ about 2500 Nm 3 / m 3 ; and - The amount of the decomposed feedstock in the hydrocarbon feedstock is at least 5 wt%, preferably at least 10 wt%, for example 10 wt% to 50 wt% with respect to the weight of the hydrocarbon feedstock.

[0087] Any catalyst known to those skilled in the art can be used in the method according to the description of the present invention. For example, a catalyst containing at least one element selected from elements from Group VIII of the Periodic Table (Groups 8, 9 and 10 of the new Periodic Table), and optionally at least one element selected from elements from Group VIB of the Periodic Table (Group 6 of the new Periodic Table).

[0088] Hereinafter, the groups of chemical elements are given according to the CAS classification (CRC Handbook of Chemistry and Physics, published by CRC Press, editor-in-chief D.R. Lide, 81st edition, 2000 - 2001). For example, Group VIII according to the CAS classification corresponds to metals from columns 8, 9 and 10 according to the new IUPAC classification; Group VIB according to the CAS classification corresponds to metals from column 6 according to the new IUPAC classification.

[0089] For carrying out the methods described in the present invention, it is possible to use conventional hydrogenation-conversion catalysts containing at least one metal or metal compound having hydrogenation-dehydrogenation function on an amorphous support. This catalyst may contain a metal from Group VIII, such as nickel and / or cobalt, often in combination with at least one metal from Group VIB, such as molybdenum and / or tungsten. For example, a catalyst containing 0.5% to 10% by weight of nickel (expressed as nickel oxide (NiO)) and 1% to 30% by weight of molybdenum, preferably 5% to 20% by weight of molybdenum (expressed as molybdenum oxide (MoO3)) on an amorphous mineral support may be used. The total content of oxides of metals from Group VIB and Group VIII in the catalyst is generally 5% to 40% by weight, preferably 7% to 30% by weight, on an amorphous mineral support. The weight ratio (expressed based on metal oxides) between one or more metals from Group VIB and one or more metals from Group VIII is generally about 20 to about 1, and usually about 10 to about 2. The support is selected from the group formed by, for example, alumina, silica, silica-alumina, magnesia, clay, and mixtures of at least two of these minerals. This support may also contain oxides selected from other compounds, such as boron oxide, zirconia, titanium oxide, and phosphoric anhydride.

[0090] Another type of catalyst that may be used is one comprising at least one matrix, at least one Y zeolite, and at least one hydride-dehydrogenated metal. The matrix, metal, and additional elements may be incorporated into the composition of this catalyst. Advantageous Y zeolites are described in patent application WO00 / 71641, as well as patents EP 0 911 077, US4,738,940, and US4,738,941.

[0091] According to one or more embodiments, the high-pressure low-temperature separator B-2 is operated at a pressure lower than the pressure of the reaction section R-1 for hydrogenation or hydrogenation conversion or the pressure of the high-pressure high-temperature separator B-1, for example, at a pressure 0.1 MPa to 1.0 MPa lower than the pressure of the reaction section R-1 for hydrogenation or hydrogenation conversion or the pressure of the high-pressure high-temperature separator B-1.

[0092] The temperature of the high-pressure cryogenic separator B-2 is generally kept as low as possible, taking into account the available cooling means. This is to maximize the purity of the recirculated hydrogen. The temperature of the high-pressure cryogenic separator B-2 is generally 20°C to 100°C, preferably 35°C to 70°C. The first liquid effluent, containing at least one light fraction, originating from the high-pressure cryogenic separator B-2 is sent to the separation tower C-1. This separation tower C-1 is preferably of the stripper type and preferably includes a reflux drum B-6.

[0093] According to one or more embodiments, the cooled reaction effluent is optionally sent to a high-pressure high-temperature separator B-1. This high-pressure high-temperature separator B-1 is operated at a lower pressure, for example, 0.1 MPa to 1.0 MPa lower than the pressure of the reaction section R-1 of the hydrogenation treatment or hydrogenation conversion. The temperature of the high-pressure high-temperature separator B-1 is generally 200°C to 450°C, preferably 250°C to 380°C, and very preferably 260°C to 360°C.

[0094] According to one or more embodiments, a first liquid effluent containing at least one heavy fraction originating from a high-pressure, high-temperature separator B-1 is sent to a first valve V-1 or optionally to a turbine, and optionally to an intermediate-pressure, high-temperature separator B-3. The pressure of the intermediate-pressure, high-temperature separator B-3 is selected to supply an optionally intermediate-pressure, low-temperature separator B-4 with a second liquid effluent containing at least one heavy fraction originating from the intermediate-pressure, high-temperature separator B-3.

[0095] According to one or more embodiments, the medium-pressure high-temperature separator B-3 is operated at a pressure of 1.0 to 4.0 MPa, preferably 1.5 to 3.5 MPa. The temperature of the medium-pressure high-temperature separator B-3 is generally 150°C to 380°C, preferably 200°C to 360°C.

[0096] According to one or more embodiments, a first liquid effluent containing at least one light fraction originating from a high-pressure cryogenic separator B-2 is expanded in a second valve V-2 or optionally in a turbine and optionally sent to a medium-pressure cryogenic separator B-4. The total pressure of the medium-pressure cryogenic separator B-4 is preferably the pressure necessary to effectively recover hydrogen into the second gaseous effluent containing hydrogen separated in separator B-4. This hydrogen recovery is preferably carried out in a pressure swing adsorption unit. The total pressure of the medium-pressure cryogenic separator B-4 is generally 1.0 MPa to 4.0 MPa, preferably 1.5 MPa to 3.5 MPa. The temperature of the medium-pressure cryogenic separator B-4 is generally 20°C to 100°C, preferably 35°C to 70°C.

[0097] The bottom liquid (line 39) from separation column C-1 may be cooled by a third heat exchanger E-4 and then sent via line 40 to a fractional distillation section (not shown). This fractional distillation section allows for the separation of the naphtha, kerosene, and gas oil fractions from the residue.

[0098] The method described in this invention is particularly suitable for feedstocks containing at least 5% by weight, preferably at least 10% by weight, of decomposed feedstock relative to the total weight of the hydrocarbon feedstock, i.e., those originating from pyrolysis or catalytic cracking units. Typically, the decomposed feedstock originates from visbreaking, coking, or FCC units. According to one or more embodiments, the decomposed feedstock originates from catalytic cracking units and includes LCO (light cycle oil) or HCO (heavy cycle oil) produced, for example, by FCC units. According to one or more embodiments, the decomposed feedstock contains olefins, whose bromine index is typically 4-20 mg / 100g, preferably 7-20 mg / 100g, as measured according to the ASTM D2710 method. The method is also suitable for feedstocks containing feedstock that is little to no decomposed. This is the case, for example, when the reaction in the reaction section is sufficiently exothermic, and as a result, it is possible to operate at a temperature of the effluent at the outlet of the reaction section that is at least 5°C, preferably at least 15°C, higher than the temperature of the feed material at the inlet of the reaction section.

[0099] The method described in this invention is suitable for feedstocks containing less than 5% by weight of decomposed feedstock relative to the total weight of the hydrocarbon feedstock, and is also suitable for feedstocks containing no decomposed feedstock at all (e.g., less than 1% by weight). For example, the method may be carried out such that the temperature rise between the inlet and outlet of the reaction section is greater than 15°C.

[0100] According to a third aspect, the description of the present invention also relates to the use of a coil-wound heat exchanger S-1 in a device according to the first aspect or a method according to the second aspect, in particular for heating a hydrocarbon mixture and passing it directly through a reaction section R-1 of a hydrogenation or hydrogenation conversion; and for cooling effluent from the reaction section R-1 of a hydrogenation or hydrogenation conversion.

[0101] The devices, methods, and uses described in this invention have the following advantages: - The presence of decomposed feedstock in the coil-wound heat exchanger S-1 and, optionally, in the hydrocarbon feedstock (decomposed feedstock causes a temperature rise in the reaction section, so the reaction effluent is at a higher temperature at the inlet of the coil-wound heat exchanger) allows the hydrocarbon mixture to be heated to a temperature high enough to remove furnace F-1 at the reactor inlet of the reaction section R-1 for hydrogenation or hydrogenation conversion in normal operation; - The coil-wound heat exchanger S-1 allows the reaction effluent to be cooled to a lower temperature in the reference device, resulting in a lower required output for the first air cooler A-1; - The coil-wound heat exchanger S-1 makes it possible to reduce the floor space required to install the device equipment; - The coil-wound heat exchanger S-1 reduces the pressure drop in the reaction loop, which in turn reduces the power required in the first compression section K-1.

[0102] (Examples) Figure 1 constitutes a reference comparison, and Figure 2 illustrates an example of an embodiment of a device and method consistent with the description of the present invention.

[0103] The hydrocarbon feedstock is a mixture of fractions with boiling points of 187°C to 365°C, containing 61% by weight of atmospheric pressure gas oil, 11% by weight of heavy vacuum distillate, 14% by weight of decomposed gas oil, and 14% by weight of coker gas oil, relative to the total weight of the hydrocarbon feedstock, and has the following characteristics.

[0104] [Table 1A]

[0105] In this application, the specific gravity of the hydrocarbon feedstock is dimensionless.

[0106] According to the description of the present invention, as shown in Figure 2, the hydrocarbon feedstock is supplied via line 1. A supplement hydrogen is preferably in excess of the hydrocarbon feedstock, and this is supplied via line 2 and a second compression section K-2 (e.g., a compressor), then via line 3, where it is mixed with recirculated hydrogen in line 4. The hydrogen is then mixed with the hydrocarbon feedstock (line 1), and the resulting hydrocarbon mixture is then passed through line 5 to a coil-wound heat exchanger S-1. The coil-wound heat exchanger S-1 allows the hydrocarbon mixture to be heated by the reaction effluent. In this embodiment, the coil-wound heat exchanger S-1 is similar to that described in patent application WO2014 / 067223. After this heat exchange, the hydrocarbon mixture is transported directly to a hydrodesulfurization section via line 7. This hydrogenadesulfurization section is formed by at least one hydrogenadesulfurization reactor (an example being reaction section R-1 for hydrogenation or hydrogenation conversion), which contains at least one hydrogenadesulfurization catalyst. The temperature required for the hydrogenadesulfurization reaction is controlled by bypassing a portion of the hydrocarbon mixture via line 19 (and possibly via valve V-3).

[0107] In this embodiment, the hydrogenation or hydrogenation reaction section R-1 consists of a hydrogenadesulfurization reactor containing three catalyst beds. The beds of the hydrogenadesulfurization reactor are composed of Axens HR1248 catalyst (of the CoMo type on Al2O3). The beds are operated at approximately 7.50 MPa and a temperature of 325°C to 390°C. The chemical hydrogen consumption in the reaction section is 1.1% by weight relative to the new hydrocarbon feedstock.

[0108] The reaction effluent is then sent via line 9 to coil-wound heat exchanger S-1, then via line 11 to first air cooler A-1, and subsequently to high-pressure cryogenic separator B-2 via line 15. High-pressure cryogenic separator B-2 enables both gas-liquid separation and decantation of the aqueous liquid phase.

[0109] The first liquid effluent, containing at least one light fraction originating from the high-pressure cryogenic separator B-2, is supplied via line 25 to the third heat exchanger E-4 and via line 28 to the stripper (example: separation tower C-1). The stripper is operated at 0.69 MPa at the top of the tower.

[0110] Recirculated hydrogen from the high-pressure cryogenic separator B-2 is sent to the amine scrubbing tower C-2 via line 16. The amine scrubbing tower C-2 makes it possible to remove at least a portion of H2S. The recirculated hydrogen is then passed through lines 17 and 18 to the first mixing section, then compressed by the first compression section K-1 and mixed with the feedstock (line 1), before being passed through the hydrogenation reactor together with the hydrocarbon feedstock.

[0111] The stripper is supplied with stripping vapor via line 32. At the top of the stripper, the gaseous fraction of the top effluent (commonly called sour gas) is recovered via line 35, and the naphtha-type fraction is recovered via line 38, the final boiling point of which is usually above 100°C. The bottom liquid from the stripper is recovered via line 39, which is cooled in a third heat exchanger E-4 and then sent via line 40 to an optional fractional distillation section (not shown). This fractional distillation section allows for the recovery of naphtha, kerosene, gas oil fractions and residues.

[0112] Table 1 compares the following: - Reference hydrogenation apparatus and method using a train of three feedstock / fluid shell-and-tube heat exchangers E-1A / B / C (Figure 1) according to TEMA BEU standards, and furnace F-1 at the reactor inlet; and - A device and method for hydrogenation treatment that conforms to the description of the present invention, using a single coil-wound heat exchanger S-1 (Figure 2) and without using any furnace F-1 at the reactor inlet.

[0113] The reference method is operated using the same feedstocks and operating conditions as described above for the examples of the method consistent with the description of the present invention.

[0114] [Table 1B]

[0115] As demonstrated in Table 1, in devices and methods consistent with the description of the present invention: - While reactor inlet F-1 is unnecessary, it is essential for the reference device and method; - The output of the first air cooler A-1 is divided by 1.5 with respect to the reference device and method; - The combined output of reactor inlet F-1 and first air cooler A-1 is divided by 2 for the reference device and method; and - The output of the first compression section K-1 is divided by 1.3 with respect to the reference device and method.

Claims

1. A device for the hydrogenation conversion or hydrogenation treatment of hydrocarbon feedstocks, At least one coil-wound heat exchanger (S-1): The coil-wound heat exchanger is a single-flow heat exchanger formed by a vertical chamber, in which one or more tubes or bundles of tubes are wound helically around a central core as a number of superimposed layers, Heating a hydrocarbon feedstock or a mixture of hydrocarbon feedstock and hydrogen flow, and directly passing this through the hydrogenation or hydrogenation reaction section (R-1), and Cooling of reaction effluent from the hydrogenation or hydrogenation reaction section (R-1). It is for the purpose of; A first mixing section for mixing hydrocarbon feedstock with a hydrogen flow; the first mixing section is located upstream or downstream of at least one coil-wound heat exchanger (S-1); Hydrogenation or hydrogenation reaction section (R-1) for hydrogenating or hydrogenating hydrocarbon feedstocks; A high-pressure cryogenic separator (B-2) for separating at least a portion of the cooled reaction effluent into a second liquid effluent containing at least one light fraction and a second gaseous effluent containing hydrogen; and Separation column (C-1) for separating a second liquid outflow containing at least one type of light fraction into bottom liquid and top outflow. A device that includes this.

2. The device for hydrogenation conversion or hydrogenation treatment according to claim 1, comprising a single coil-wound heat exchanger (S-1).

3. The hydrogenation conversion or hydrogenation treatment device according to claim 1 or 2, further comprising a bypass (19) for directing a portion of the hydrocarbon feedstock or a portion of the mixture of the hydrocarbon feedstock and hydrogen flow from the inlet of the coil-wound heat exchanger (S-1) to the outlet of the coil-wound heat exchanger (S-1).

4. A device for hydrogenation conversion or hydrogenation treatment according to any one of claims 1 to 3, further comprising a high-pressure high-temperature separator (B-1) for separating cooled reaction effluent into a first liquid effluent containing at least one heavy fraction and a first gaseous effluent containing a light fraction, wherein the first gaseous effluent, rather than the cooled reaction effluent, is passed through a high-pressure low-temperature separator (B-2).

5. The device for hydrogenation conversion or hydrogenation treatment according to claim 4, further comprising a medium-pressure high-temperature separator (B-3), the medium-pressure high-temperature separator (B-3) for separating a first liquid effluent containing at least one heavy fraction into a third liquid effluent containing at least one heavy fraction and a third gaseous effluent containing a light fraction, the third liquid effluent being passed through a separation tower (C-1).

6. The device for hydrogenation conversion or hydrogenation treatment according to any one of claims 1 to 5, further comprising a medium-pressure low-temperature separator (B-4), the medium-pressure low-temperature separator (B-4) for separating a second liquid effluent containing at least one light fraction into a fourth liquid effluent containing at least one light fraction and a fourth gaseous effluent containing hydrogen, the fourth liquid effluent being passed through a separation tower (C-1).

7. A device for hydrogenation conversion or hydrogenation treatment according to claim 6, dependent on claim 5, wherein the medium-pressure low-temperature separator (B-4) is suitable for separating a third gaseous effluent containing a light fraction.

8. A method for the hydrogenation conversion or hydrogenation treatment of hydrocarbon feedstock, comprising the following steps: A step of heating a hydrocarbon feedstock or a mixture of hydrocarbon feedstock and hydrogen flow using at least one coil-wound heat exchanger (S-1), and directly flowing this mixture to a hydrogenation or hydrogenation reaction section (R-1); A step of mixing hydrocarbon feedstock with a hydrogen flow in a first mixing section, wherein the mixing is performed before or after the heating step; A step of cooling reaction effluent from a hydrogenation or hydrogenation reaction section (R-1) with at least one coil-wound heat exchanger (S-1), wherein the coil-wound heat exchanger is a single-flow heat exchanger formed by a vertical chamber, in which one or more tubes or bundles of tubes are wound helically around a central core as a number of superimposed layers; A step of hydrogenating or hydrogenating a hydrocarbon feedstock in a hydrogenation or hydrogenation reaction section (R-1), wherein the hydrogenation or hydrogenation reaction section (R-1) includes at least one reactor, the reactor includes at least one catalyst comprising at least one element selected from Group VIII of the periodic table; A step of separating at least a portion of the cooled reaction effluent in a high-pressure cryogenic separator (B-2) and passing through a first liquid effluent containing at least one light fraction and a first gaseous effluent containing hydrogen; and A process of separating a first liquid outflow containing at least one type of light fraction in a separation column (C-1) and circulating the bottom liquid and the top outflow. Methods that include...

9. Hydrogenation or hydrogenation of hydrocarbon feedstocks is performed under the following operating conditions: The temperature ranges from approximately 200°C to approximately 460°C; The total pressure is approximately 1 MPa to 20 MPa; The overall space velocity per hour of the liquid supply material is approximately 0.05 h －１ ~about 12 hours －１ It is; A hydrogen stream contains approximately 50% to 100% hydrogen by volume relative to the volume of the hydrogen stream; The amount of hydrogen relative to the liquid hydrocarbon feedstock is approximately 50 Nm³. ３ / m ３ ~Approx. 2500Nm ３ / m ３ It is; A method of hydrogenation conversion or hydrogenation treatment according to claim 8, carried out under at least one of the following conditions.

10. The hydrogenation conversion or hydrogenation treatment method according to claim 8 or 9, wherein the initial boiling point of the hydrocarbon supply material is higher than 120°C.

11. The hydrocarbon feedstock contains at least 5% by weight of decomposed feedstock relative to the weight of the hydrocarbon feedstock; or A method for hydrogenation or hydrogenation according to any one of claims 8 to 10, wherein the hydrocarbon feedstock comprises less than 5% by weight of decomposed feedstock relative to the weight of the hydrocarbon feedstock, and a temperature increase of more than 15°C is performed between the inlet and outlet of the hydrogenation or hydrogenation reaction section (R-1).

12. A method for hydrogenation or hydrogenation treatment according to any one of claims 8 to 11, wherein a high-pressure low-temperature separator (B-2) is operated at a pressure lower than the pressure of the reaction section (R-1) for hydrogenation or hydrogenation conversion.

13. The method for hydrogenation conversion or hydrogenation treatment according to any one of claims 8 to 12, wherein the temperature of the high-pressure low-temperature separator (B-2) is 20°C to 100°C.

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