Systems and methods for generating a chloride-reduced stripped fluid from a hydrotreated effluent

Abstract

The present disclosure relates to a process for generating a stripped fluid having a reduced chloride content, the process comprising stripping chloride from a hydrotreated effluent using a hot high pressure stripper to generate the stripped fluid and a vapor, wherein the stripped fluid comprises a lower chloride content than the hydrotreated effluent, and wherein the vapor comprises chloride.

Description

Technical Field

[0001] In some embodiments, this disclosure relates to methods and systems for generating stripped fluids (e.g., having at least 10% chloride) from hydrotreating reactor effluents formed by hydrotreating a feed fluid (e.g., crude oil feed fluid, biofeed fluid, or a combination of crude oil and biofeed fluids). Background Technology

[0002] Humans obtain energy from the combustion of hydrocarbon fuel products developed and refined from renewable (e.g., biofeedstock) and non-renewable (e.g., fossil fuels) sources. Hydrotreating systems are used to refine raw feed fluids (e.g., fossil fuels, biofeedstocks, combinations) into combustible hydrocarbon fuels. However, some contaminants in the feed treated in hydrotreating systems can rapidly degrade system components, thereby reducing the commercial and / or environmental viability of using such systems.

[0003] Hydrotreating of feed fluids chemically converts the hydrocarbons they contain into more desirable hydrocarbons through hydrogenation, hydrocracking, hydrorefining, hydrodeoxygenation, and other reactions. Because the feed fluids contain chloride components (e.g., inorganic chlorides, sodium or calcium chloride, organic chlorides), the hydrotreating reactors performing this method also generate and contain concentrated levels of hydrogen chloride derived from the chemical reaction of chlorides with hydrogen. Hydrogen chloride can deposit as ammonium chloride salts in hydrotreating system components, leading to pressure drop, scaling, and corrosion, which necessitates costly system downtime, repair, and replacement.

[0004] Existing methods for treating chlorides involve pretreating the feed fluid with an aqueous scrubber to remove water-soluble salts (e.g., NaCl). However, aqueous scrubbers only remove water-soluble chlorides (e.g., NaCl, KCl), leaving water-insoluble organic chlorides (e.g., benzyl chloride). In the hydrotreatment reactor, the remaining chlorides are converted to hydrogen chloride (HCl), which accumulates in the system. Ammonia (NH3) can also form in the hydrotreatment reactor from the chemical reaction of nitrogen compounds present in the fresh feed with hydrogen. As the reactor effluent is cooled from the required temperature in the hydrotreatment reactor to near ambient temperature (e.g., 50°C), ammonium chloride (NH4Cl) salts can form and deposit in the reactor effluent loop, leading to scaling and blockage. The deposition temperature of NH4Cl salts increases with the concentration of HCl and NH3 in the reactor effluent. If this concentration is too high, ammonium chloride salt deposition occurs before the salt precursors (NH3, HCl) can be removed from the reactor effluent by applying water scrubbing. If the wash water is mixed with the reactor effluent at excessively high temperatures, the wash water will evaporate completely and will not remove or dilute the chloride salt precursor.

[0005] There is a need for methods and systems that not only reduce the chloride content of the feed fluid entering the system, but also treat chloride waste products from the reactor effluent to produce a hydrocarbon liquid effluent with reduced chloride content and enable reliable system operation, thereby preventing maintenance-based downtime. Summary of the Invention

[0006] Therefore, there is a need for improved methods and systems for generating stripped fluids (e.g., having at least 10% chloride). In some embodiments, the method may include stripping chloride from a hydrotreatment effluent using a hot high-pressure stripper to generate stripped fluid and a vapor effluent. To generate the hydrotreatment effluent, the method may include combining a feed fluid with a hydrogen-rich gas in the presence of a catalyst in a hydrotreatment reactor to produce the hydrotreatment effluent. The stripped fluid generated from the hydrotreatment effluent can be used for quenching the hydrotreatment reactor. In some embodiments, the stripped fluid can be used by recycling a portion of the stripped fluid back into the hydrotreatment reactor. In addition to the hydrotreatment effluent, the hydrotreatment reactor may also generate hydrotreatment fluids that can be used as fuel. The disclosed methods include fractional distillation of the hydrotreated fluid to generate at least a first hydrocarbon fraction and a second hydrocarbon fraction.

[0007] The stripping fluid may contain a lower chloride content than the hydrotreatment effluent. The vapor may contain chlorides. The stripping fluid may contain at least 10% less chloride than the hydrotreatment effluent. The stripping fluid may contain at least 50% less chloride than the hydrotreatment effluent. The feed fluid may contain hydrocarbons and chlorides in the range of about 0.1 parts per million (wppm) to about 20 wppm. The catalyst may include one or more of cobalt, nickel, molybdenum, palladium, and platinum catalysts. The hydrotreatment reactor may be maintained at a temperature in the range of about 200°C to about 450°C. The hot high-pressure stripper may be maintained at a temperature in the range of about 150°C to about 300°C. Stripping chlorides may include stripping gas containing hydrogen concentrations in the range of about 50% to 99% hydrogen by volume of the stripping gas.

[0008] This disclosure relates to a hydrotreatment system for generating a stripped fluid with reduced chloride levels. The system may include a hydrotreatment reactor configured to produce a hydrotreated effluent from a feed fluid; and a hot high-pressure stripper configured to strip chlorides from the hydrotreated effluent to generate a stripped fluid and vapor. In some embodiments, in addition to the hydrotreated effluent, the system may be configured to generate a hydrotreated fluid that can be directly sold, used, or further refined. For example, the hydrotreated fluid may be further refined by a fractional distillation unit. The fractional distillation unit may include a fractional distillation column and heating elements. The fractional distillation unit may be configured to receive the hydrotreated fluid from the hydrotreatment reactor. The system may include a first heat exchanger connecting the hydrotreatment reactor to the hot high-pressure stripper; and a second heat exchanger connecting the hot high-pressure stripper to a feed fluid tank and the first heat exchanger. The system may include a steam scrubbing unit configured to use water scrubbing to remove a portion of the chlorides from the steam to produce clean hydrocarbons.

[0009] The hydrotreating system may include a feed recirculation reservoir connected to a hot high-pressure stripper. The feed recirculation reservoir is configured to receive a portion of the stripped fluid from the hot high-pressure stripper. The feed recirculation reservoir is further configured to combine a portion of the stripped fluid with the feed fluid. The hot high-pressure stripper may include a stripping gas delivery line configured to deliver stripping gas containing hydrogen-rich gas from a stripping gas storage tank to the hot high-pressure stripper. A stripped fluid collection container may be connected to the hot high-pressure stripper via a stripped fluid delivery line. The stripped fluid collection container may be configured to receive a portion of the stripped fluid from the hot high-pressure stripper via the stripped fluid delivery line. The hydrotreating system may include a quenching facility connected to the hot high-pressure stripper and the hydrotreating reactor. The quenching facility may be configured to receive a portion of the stripped fluid from the hot high-pressure stripper. The quenching facility can be configured to deliver a portion of the stripped fluid to the hydrotreating reactor. Attached Figure Description

[0010] Some embodiments of this disclosure can be understood by referring in part to this disclosure and the accompanying drawings, in which:

[0011] Figure 1 This is a diagram of a hydrogenation treatment system configured to generate stripped fluid according to a specific example embodiment of the present disclosure. Detailed Implementation

[0012] In some embodiments, this disclosure relates to systems and methods for generating stripped fluids (e.g., liquids, gases) from a hydrotreating reactor with reduced chloride levels (e.g., having at least 10% less chloride). The disclosed systems can operate on a wide variety of feed types, which is superior to existing systems that generally operate only on crude oil (e.g., hydrocarbons) or biofeedback (e.g., vegetable oils, animal fats). For example, the disclosed systems can operate with crude oil, biofeedback, or both simultaneously. Furthermore, the disclosed methods and systems can hydrotreat feed fluids containing chlorides (including relatively high concentrations of chlorides), such as those containing more than 1 part per million (wppm) of chloride. In existing systems, chlorides contained in the feed fluid accumulate as hydrogen chloride (HCl) or ammonium chloride (NH4Cl) during hydrotreating operations, which can contribute to corrosion, scaling, or blockage of system components and increase system downtime. Chloride accumulation can occur as chlorides sublimate onto various system components. In existing systems, the concentration of chloride in the feed fluid is preferably very low (e.g., <1 wppm) to minimize scaling and clogging of system components.

[0013] The disclosed systems and methods operate by removing chlorides from the effluent of a hydrotreatment reactor, preventing their accumulation and potential damage to the system. The disclosed systems remove chlorides from the effluent of a hydrotreatment reactor at temperatures well above the deposition temperature of chloride salts. Since the deposition temperature of chlorides increases with increasing chloride concentration in the effluent of the hydrotreatment reactor, the disclosed system for removing chlorides from the effluent of a hydrotreatment reactor prevents salt deposition in systems using that effluent.

[0014] System for generating stripped fluid

[0015] Figure 1An embodiment of the disclosed system 100 is shown that can generate a stripped fluid with a reduced chloride level. System 100 includes various components for hydrotreating a feed fluid to produce a hydrotreated effluent containing chlorides and hydrocarbons. System 100 may include a hydrotreating reactor 105 configured to generate a hydrotreated effluent that may contain hydrogen chloride (HXl) and ammonia (NH3). The system may include a hot high-pressure stripper 115 that strips chlorides (e.g., HCl) and ammonia from the hydrotreated effluent to generate chloride-containing vapor and a stripped fluid. The hydrogen chloride and ammonia content in the stripped fluid may be low. The stripped fluid may contain hydrocarbons (e.g., C1-C25 hydrocarbons). In some embodiments, the hot high-pressure stripper 115 may generate chloride-containing vapor from the top of the stripper and a stripped fluid from the bottom of the stripper. The system may include a first heat exchanger 110 connecting the hydrotreatment reactor 105 to a hot high-pressure stripper 115. The first heat exchanger 110 may cool and partially condense the effluent from the hydrotreatment reactor 105. In some embodiments, the first heat exchanger 110 may use the hydrotreatment reactor effluent to preheat a colder new feed before it is fed to the hydrotreatment reactor 105.

[0016] System 100 may be configured to deliver feed fluid from feed fluid storage tank 145 to hydrotreatment reactor 105 via a feed fluid delivery line. The temperature of the feed fluid may be increased by exchanging heat with the hydrotreatment reactor effluent 105 in a first heat exchanger 110. Additionally, the temperature of the feed fluid may be increased by exchanging heat with stripped fluid received from the bottom of a stripper in a second heat exchanger 120. In some embodiments, an ignition heater may be used to preheat the feed fluid to a desired temperature before it enters the hydrotreatment reactor 105. In some embodiments, a portion of the feed fluid may be delivered to the hydrotreatment reactor 105 from another source instead of from feed fluid storage tank 145. For example, a portion of the feed fluid may be delivered from the bottom of a hot high-pressure stripper 115. The feed fluid may enter the hydrotreatment reactor 105 at various locations, including one or more side locations between the top of the hydrotreatment reactor 105 and the catalyst bed contained within the hydrotreatment reactor 105. System 100 may include a hydrogen-rich gas storage tank 150 connected to a hydrotreatment reactor 105 via a hydrogen-rich gas connector. System 100 may be configured to deliver hydrogen-rich gas from the hydrogen-rich gas storage tank 150 to the hydrotreatment reactor 105 via a hydrogen delivery line. The hydrogen-rich gas may be delivered from a recirculated gas stream generated within system 100 or from a hydrogen source outside system 100, or a combination of both. The hydrogen-rich gas 150 may be mixed with the feed fluid before entering the hydrotreatment reactor 105. The hydrogen-rich gas may be provided by quenching the hydrogen-rich gas storage tank 150 and may be used as a quench gas when directly delivered to the hydrotreatment reactor 105. According to some embodiments, the hydrotreatment reactor 105 may be configured to combine the feed fluid with the hydrogen-rich gas in the presence of a catalyst to produce a hydrotreated effluent containing hydrocarbons and other compounds containing hydrogen chloride and ammonia.

[0017] The feed fluid may contain chlorides ranging from about 0.1 wppm to about 20 wppm (e.g., wppm by weight). Chloride content can be expressed as chlorine (e.g., Cl). -In some embodiments, the feed fluid may contain chloride content ranging from about 0.1 wppm to about 0.5 wppm, or about 0.25 wppm to about 0.75 wppm, or about 0.5 wppm to about 1.0 wppm, or about 0.75 wppm to about 1.25 wppm, wherein about includes plus or minus 0.25 wppm. The feed fluid may contain chloride content ranging from about 1.0 wppm to about 5.0 wppm, or about 2.5 wppm to about 7.5 wppm, or about 5.0 wppm to about 10.0 wppm, or about 7.5 wppm to about 12.5 wppm, or about 10.0 wppm to about 15.0 wppm, or about 12.5 wppm to about 17.5 wppm, or about 15.0 wppm to about 20.0 wppm, wherein about includes plus or minus 1.25 wppm. The feed fluid may contain about 0.1 wppm, or about 0.5 wppm, or about 1.0 wppm, or about 1.5 wppm, or about 2.0 wppm, or about 2.5 wppm, or about 3.0 wppm, or about 3.5 wppm, or about 4.0 wppm, or about 4.5 wppm, or about 5.0 wppm, including approximately plus or minus 0.25 wppm. The feed fluid may contain about 5 wppm, or about 7.5 wppm, or about 10.0 wppm, or about 12.5 wppm, or about 15.0 wppm, or about 17.5 wppm, or about 20.0 wppm, including approximately plus or minus 2.5 wppm. In some embodiments, the feed fluid may be a high-chloride feed having a chloride content greater than about 1 wppm.

[0018] According to some embodiments, the hydrotreatment effluent may contain chloride concentrations ranging from about 0.1 wppm to about 100 wppm or higher. The hydrotreatment effluent may contain chloride concentrations ranging from about 0.1 wppm to about 100 wppm. The hydrotreatment effluent may contain about 0.1 wppm or about 10 wppm, or about 5 wppm or about 15 wppm, or about 10 wppm or about 20 wppm, or about 15 wppm or about 25 wppm, or about 20 wppm or about 30 wppm, or about 25 wppm or about 35 wppm, or about 30 wppm or about 40 wppm, or about 35 wppm or about 45 wppm, or about 40 wppm or about 50 wppm, or about 45 wppm or about 55 wppm. Chloride concentrations of approximately 50 wppm or 60 wppm, or approximately 55 wppm or 65 wppm, or approximately 60 wppm or 70 wppm, or approximately 65 wppm or 75 wppm, or approximately 70 wppm or 80 wppm, or approximately 75 wppm or 85 wppm, or approximately 80 wppm or 90 wppm, or approximately 85 wppm or 95 wppm, or approximately 90 wppm or 100 wppm, including approximately plus or minus 5 wppm. Hydrotreatment effluents may contain chloride concentrations of approximately 0.1 wppm, or approximately 2 wppm, or approximately 3 wppm, or approximately 4 wppm, or approximately 5 wppm, or approximately 6 wppm, or approximately 7 wppm, or approximately 8 wppm, or approximately 9 wppm, or approximately 10 wppm, including approximately plus or minus 0.5 wppm. Hydrotreating effluents may contain chloride concentrations of approximately 10 wppm, or approximately 20 wppm, or approximately 30 wppm, or approximately 40 wppm, or approximately 50 wppm, or approximately 60 wppm, or approximately 70 wppm, or approximately 80 wppm, or approximately 90 wppm, or approximately 100 wppm, of which approximately 5 wppm may be added or subtracted.

[0019] According to some embodiments, system 100 may be configured to combine hydrogen-rich gas with a catalyst and feed fluid in a hydrotreatment reactor 105 to generate a hydrotreated effluent. In some embodiments, in addition to the hydrotreated effluent, the system may be configured to also generate a hydrotreated fluid that can be used directly as a hydrocarbon product or that can be further refined. The hydrotreated fluid can be generated in system 100 by combining hydrogen-rich gas with a catalyst and feed fluid. Hydrogen-rich gas can be supplied from a hydrogen-rich gas storage tank 150 to the hydrotreatment reactor 105 via a hydrogen-rich gas delivery line. The hydrotreatment reactor 105 can be filled with hydrogen-rich gas at a pressure ranging from about 150 psi to about 3000 psi. The pressure of the hydrogen-rich gas can range from about 150 psi to about 250 psi, or about 250 psi to about 500 psi, or about 750 psi, or about 750 psi to about 1,000 psi, about 1050 psi to about 1250 psi, or about 1250 psi to about 1500 psi, or about 1750 psi, or about 1750 psi to about 2000 psi, about 2050 psi to about 2250 psi, or about 2250 psi to about 2500 psi, or about 2750 psi, or about 2750 psi to about 3000 psi, wherein about 125 psi is included. The hydrogen-rich gas includes hydrogen and hydrocarbons. The hydrocarbons in the hydrogen-rich gas include C1-C5 alkanes. In some embodiments, the hydrocarbons in the hydrogen-rich gas may primarily consist of C1-C5 alkanes. The hydrogen-rich gas includes water, C6 alkanes, CO, and H2S. The hydrogen-rich gas may have a hydrogen content of about 50% to about 60%, or about 60% to about 70%, or about 70% to about 80%, or about 80% to about 90%, or about 90% to about 99% by volume, wherein about includes plus or minus 5%. The hydrogen-rich gas may have an alkane content of about 1% to about 10%, or 10% to about 20%, or 20% to about 30%, or 30% to about 40%, or about 50% to about 60%, or about 60% to about 70%, or about 70% to about 80%, or about 80% to about 90%, or about 90% to about 99% by volume, wherein about includes plus or minus 5%. The hydrogen-rich gas may include alkanes, including but not limited to methane, ethane, propane, butane, pentane, mixtures thereof, and isomers thereof.

[0020] In some embodiments, the hydrogenation reactor 105 may be configured to contain a catalyst, including one or more of palladium catalysts, platinum catalysts, nickel catalysts, cobalt catalysts, nickel catalysts, and molybdenum catalysts.

[0021] According to some embodiments, system 100 may include a hydrotreating reactor 105 containing a reactor vessel having one or more thermocouples. The thermocouples may be configured to maintain the reactor vessel temperature in a range from about 200°C to about 450°C. The thermocouples may also be configured to maintain the reactor temperature in a range from about 200°C to about 250°C, or about 250°C to about 300°C, or about 300°C to about 350°C, or 350°C to about 400°C, or 400°C to about 450°C, wherein about includes adding or subtracting 25°C.

[0022] In some embodiments, system 100 may be configured to generate a hydrotreated fluid in hydrotreatment reactor 105. The hydrotreated fluid may be a fluid that has already been treated by one or more of the following steps: hydrorefining, hydrogenation, hydroisomerization, and / or hydrocracking. In some embodiments, the hydrotreated fluid may include any hydrocarbon, including alkanes, branched alkanes, straight-chain alkanes, alkenes, alkynes, aryl hydrocarbons, aromatic hydrocarbons, and combinations thereof.

[0023] In some embodiments, the hydrotreated fluid may have a sulfur concentration of 5000 wppm or less. The hydrotreated fluid may have a sulfur concentration of less than about 5000 wppm, or less than about 4500 wppm, or less than about 4000 wppm, or less than about 3500 wppm, or less than about 3000 wppm, or less than about 2500 wppm, or less than about 2000 wppm, or less than about 1500 wppm, or less than about 1000 wppm, or less than about 500 wppm, or less than about 1 wppm, wherein approximately includes adding or subtracting 250 wppm. The hydrotreated fluid may have a sulfur concentration of less than about 100 wppm, or less than about 90 wppm, or less than about 80 wppm, or less than about 70 wppm, or less than about 60 wppm, or less than about 50 wppm, or less than about 40 wppm, or less than about 30 wppm, or less than about 20 wppm, or less than about 10 wppm, or less than about 1 wppm, wherein about 5 wppm is included or subtracted. The disclosed method can produce low-sulfur hydrotreated fluids that, when combusted (e.g., in motor vehicles, aircraft, railway locomotives, ships, gas or oil-fired power plants, residential and industrial furnaces, and other forms of fuel combustion), have reduced sulfur dioxide emissions compared to hydrotreated fuels with higher sulfur content.

[0024] According to some implementation plans, such as Figure 1As shown, system 100 may include a hydrotreatment reactor 105 connected to a hot high-pressure stripper 115 via a first heat exchanger 110. The hot high-pressure stripper 115 may contain a stripping column and may be configured to strip chlorides from the hydrotreatment effluent to generate a stripped fluid containing hydrocarbons and a chloride-containing vapor. The stripped fluid may have less chloride than the hydrotreatment effluent. The stripped fluid may have about 10% to about 99% less chloride than the hydrotreatment effluent. The stripped fluid may have about 10%, or about 20%, or about 30%, or about 40%, or about 50%, or about 60%, or about 70%, or about 80%, or about 90%, or about 99% less chloride than the hydrotreatment effluent, wherein about 5% is added or subtracted. The stripping fluid may contain about 10% to about 20% by weight less, or about 20% to about 30% by weight less, or about 30% to about 40% by weight less, or about 40% to about 50% by weight less, or about 50% to about 60% by weight less, or about 60% to about 70% by weight less, or about 80% to about 90% by weight less, or about 90% to about 99% by weight less, of which about 5% by weight is added or subtracted. The hot high-pressure stripper 115 may be configured to remove ammonia and chlorides in the form of hydrogen chloride, ammonium chloride, and combinations thereof. For example, the hot high-pressure stripper 115 may be configured to remove hydrogen chloride as a gas from the hydrotreated effluent to produce the stripping fluid. The stripping fluid may contain hydrocarbons, including alkanes, branched alkanes, straight-chain alkanes, alkenes, alkynes, aryl groups, aromatics, and combinations thereof.

[0025] According to some embodiments, the hot high-pressure stripper 115 can operate at pressures ranging from about 150 psi to about 3000 psi and at temperatures ranging from about 150°C to about 300°C. The hot high-pressure stripper 115 can operate at pressures ranging from about 150 psi to about 250 psi, or about 250 psi to about 500 psi, or about 750 psi, or about 750 psi to about 1,000 psi, about 1050 psi to about 1250 psi, or about 1250 psi to about 1500 psi, or about 1750 psi, or about 1750 psi to about 2000 psi, about 2050 psi to about 2250 psi, or about 2250 psi to about 2500 psi, or about 2750 psi, or about 2750 psi to about 3000 psi, where about 125 psi is added or subtracted. The hot high-pressure stripper 115 can operate at temperatures ranging from about 150°C to about 200°C, or 200°C to about 250°C, or about 250°C to about 300°C, including a difference of about 25°C. The pressure within the hot high-pressure stripper 115 can be generated by the hydrotreatment reactor loop pressure. The hot high-pressure stripper 115 may include thermocouples configured to regulate the temperature of the hydrotreatment reactor effluent supplied to the hot high-pressure stripper 115. In some embodiments, the hot high-pressure stripper 115 may use stripping gas supplied by a stripping gas storage tank 130 to strip chlorides from the hydrotreatment effluent. The stripping gas storage tank 130 is connected to the hot high-pressure stripper 115 via a stripping gas connector. The stripping gas may include a hydrogen-rich gas, which may be supplied from a recirculated gas stream generated within system 100 or from a hydrogen source outside system 100, or a combination of both.

[0026] The hot high-pressure stripper 115 can be configured to remove hydrogen chloride and ammonia from the hydrotreatment effluent. System 100 may include a steam scrubbing unit 125 configured to remove chlorides from the steam using water scrubbing to produce a chloride-containing aqueous solution and clean hydrocarbons.

[0027] like Figure 1As shown, in some embodiments, the disclosed system 100 may include a stripped fluid collection container 140 connected to a hot high-pressure stripper 115 via a stripped fluid delivery line. The stripped fluid delivery line connects the stripper bottom of the hot high-pressure stripper 115 to the stripped fluid collection container 140. System 100 may be configured to deliver a portion of the stripped fluid from the hot high-pressure stripper 115 to a quenching facility 135. The quenching facility 135 may be connected to the hydrotreatment reactor 105 in multiple sections via a series of quenching connectors. In some embodiments, the stripped fluid from the quenching facility 135 may be cooled before entering the hydrotreatment reactor. The stripped fluid from the quenching facility 135 may enter the hydrotreatment reactor at multiple locations between the catalyst beds. A portion of the stripped fluid from the hot high-pressure stripper 115 can be stored in the feed recirculation reservoir 155, allowing it to be mixed with the feed and added to the hydrotreatment reactor 105. This mixing can occur at various locations in the feed line leading to the hydrotreatment reactor 105 (e.g., upstream of a heat exchanger or between multiple heat exchangers). When a portion of the stripped fluid from the hot high-pressure stripper 115 is mixed with the feed just before entering the hydrotreatment reactor 105, it can act as a liquid quenching agent for the hydrotreatment reactor 105. A portion of the stripped fluid from the hot high-pressure stripper 115 (e.g., from the bottom of the hot high-pressure stripper 115) can supply heat to the feed of the hydrotreatment reactor 105 via a second heat exchanger 120 to improve the energy efficiency of the hydrotreatment reactor 105. In some embodiments, the second heat exchanger 120 can transfer heat to the first heat exchanger 110. Because the heat around the second heat exchanger 120 is sufficiently high, it ensures that the metal tubes of the first heat exchanger 110 maintain a sufficiently high temperature to prevent salt deposition where the first heat exchanger 110 connects to the hydrotreatment reactor 105. Maintaining a sufficiently high temperature to prevent salt deposition at the connection point of the first heat exchanger 110 to the hydrotreatment reactor 105 prevents scaling and clogging on the effluent side of the first heat exchanger 110 from the hydrotreatment reactor. In some embodiments, the second heat exchanger 120 connects the hot high-pressure stripper 115 to the quenching facility 135, the hydrotreated fluid reservoir 155, the feed fluid reservoir 145, and the first heat exchanger 110.

[0028] The disclosed system 100 may include more than one hydrotreatment stage. Each hydrotreatment stage may include one or more hydrotreatment reactors. Each hydrotreatment reactor may include one or more catalyst beds. System 100 may have one, two, three, four, or more hydrotreatment stages. If hydrotreatment reactor 105 has two hydrotreatment stages, stripped fluid may be sent to a second hydrotreatment stage of system 100 via a stage connector. For example, stripped fluid from stripped fluid storage tank 140 may be sent to a second stage of hydrotreatment reactor 105 via a second-stage connector. In some embodiments, stripped fluid from hot high-pressure stripper 115 may be sent to a second stage of system 100 via a second-stage connector.

[0029] In some embodiments, the hydrotreated fluid generated by the hydrotreatment reactor 105 can be used directly or further processed (e.g., distilled). System 100 may include a stage section configured to distill the hydrotreated fluid into one or more hydrocarbon fractions. The stage section may be connected to the hydrotreatment reactor 105 via a stage connector. The stage section may be configured to receive the hydrotreated fluid from the hydrotreatment reactor 105 via the stage connector.

[0030] Methods for generating stripped fluid

[0031] According to some embodiments, this disclosure relates to a method for generating a stripped fluid from a hydrotreated effluent produced by a hydrotreated reactor 105. The stripped fluid may have a lower chloride content than the hydrotreated effluent (e.g., at least 10% less chloride content).

[0032] According to some embodiments, the method may include combining a feed fluid with a hydrogen-rich gas in a hydrotreatment reactor 105 in the presence of a catalyst to produce a hydrotreated effluent. The feed fluid may be supplied to the hydrotreatment reactor 105 from a feed fluid storage tank 145 via a feed fluid delivery line. The hydrogen-rich gas may be supplied to the hydrotreatment reactor 105 from a hydrogen gas storage tank 150 via a hydrogen delivery line. In some embodiments, the feed fluid may include crude oil (e.g., hydrocarbons), biofeedback (e.g., vegetable oils), or a combination thereof. The feed fluid may include a hydrocarbon and chloride content (e.g., in the range of about 0.1 wppm to about 100 wppm, expressed as chlorine and by weight). The feed fluid may contain chlorides at concentrations of about 0.1 w ppm, or about 5 w ppm, or about 10 w ppm, or about 15 w ppm, or about 20 w ppm, or about 25 w ppm, or about 30 w ppm, or about 35 w ppm, or about 40 w ppm, or about 45 w ppm, or about 50 w ppm, or about 55 w ppm, or about 60 w ppm, or about 65 w ppm, or about 70 w ppm, or about 75 w ppm, or about 80 w ppm, or about 85 w ppm, or about 90 w ppm, or about 95 w ppm, or about 100 w ppm, where approximately includes additions or subtractions of 5 w ppm. In some embodiments, the method may include washing the feed fluid (e.g., with an aqueous solution) before feeding it to the hydrotreatment reactor 105 to remove a portion of the chlorides from the feed fluid. For example, the method may include washing the feed fluid (e.g., with water or brine) to remove chlorides from the feed fluid.

[0033] According to some embodiments, the method may include combining a feed fluid with a hydrogen-rich gas in a hydrotreatment reactor 105 and in the presence of a catalyst to produce a hydrotreated effluent. The method may combine the feed fluid and the hydrogen-rich gas with a catalyst, which may be one or more of a palladium catalyst, a platinum catalyst, a nickel catalyst, a cobalt catalyst, and a molybdenum catalyst.

[0034] According to some embodiments, the disclosed method produces a hydrotreated effluent from a hydrotreated reactor 105. The method can produce a hydrotreated effluent having a chloride concentration in the range of about 0.1 wppm to about 100 wppm or higher. The method can generate a hydrotreated effluent having a chloride concentration of about 0.1 wppm, or about 5 wppm, or about 10 wppm, or about 15 wppm, or about 20 wppm, or about 25 wppm, or about 30 wppm, or about 35 wppm, or about 40 wppm, or about 45 wppm, or about 50 wppm, or about 55 wppm, or about 60 wppm, or about 65 wppm, or about 70 wppm, or about 75 wppm, or about 80 wppm, or about 85 wppm, or about 90 wppm, or about 95 wppm, or about 100 wppm, wherein about 5 wppm is added or subtracted. In some embodiments, the method includes the step of conveying the hydrotreated effluent from the hydrotreated reactor 105 to the hot high-pressure stripper 115 via a first heat exchanger 110.

[0035] The method may include stripping chlorides from the effluent of a hydrotreatment reactor 105 using a hot high-pressure stripper 115 to generate chloride-containing vapor and a stripped fluid. The hot high-pressure stripper may be maintained at a temperature ranging from about 150°C to about 300°C. The stripped fluid may have less chloride than the hydrotreatment effluent. The stripped fluid may have about 10% by weight to about 99% by weight less chloride than the hydrotreatment effluent. The stripped fluid may have about 10% by weight, or about 20% by weight, or about 30% by weight, or about 40% by weight, or about 50% by weight, or about 60% by weight, or about 70% by weight, or about 80% by weight, or about 90% by weight, or about 99% by weight less chloride than the hydrotreatment effluent, wherein about 5% by weight is added or subtracted. The hot high-pressure stripper 115 may be configured to remove chlorides from the hydrotreatment effluent, the chlorides being in the form of hydrogen chloride, ammonium chloride, sodium chloride, potassium chloride, and combinations thereof.

[0036] In some embodiments, the method may include preheating the feed fluid before it is introduced into the hydrotreatment reactor 105 using stripped fluid via a second heat exchanger 120. The stripped fluid may be used to preheat the feed fluid to a temperature ranging from about 50°C to about 350°C. The stripped fluid may preheat the feed fluid to a temperature of about 50°C, or about 75°C, or about 100°C, or about 125°C, or about 150°C, or about 175°C, or about 200°C, or about 225°C, or about 250°C, or about 275°C, or about 300°C, or about 325°C, or about 350°C, where about includes adding or subtracting 12.5°C. The method may include using a heat exchanger to prevent chloride salts from depositing on the effluent side of the hydrotreatment reactor 105. The heat transfer from the second heat exchanger 120 to the heat exchanger 110 can be sufficiently high to ensure that the metal tubes of the heat exchanger 110 on the reactor effluent side (e.g., the reactor effluent side of the hydrotreatment reactor 105) are above the chloride deposition temperature. This prevents salt deposits that could lead to scaling and blockage on the reactor effluent side of the heat exchanger 110. Preheating the feed fluid before it is introduced into the hydrotreatment reactor 105 reduces the overall energy cost of the system 100 because less energy will be required to maintain the reaction temperature within the hydrotreatment reactor 105.

[0037] According to some embodiments, the method includes generating a hydrotreated fluid from a hydrotreatment reactor. The hydrotreated fluid generated by hydrotreatment reactor 105 can be used directly or further processed (e.g., distilled). In some embodiments, the hydrotreated fluid can be conveyed to a classification section via a classification section conveying line. The method may include distilling the hydrotreated fluid in the classification section to produce one or more hydrocarbon fractions. The hydrocarbon fractions may include multiple fractions within a boiling point range. In some embodiments, one or more hydrocarbon fractions can be conveyed from the classification distillation unit to the hydrotreated fluid reservoir 155 via a distillation fluid conveying line. In some embodiments, one or more hydrocarbon fractions can be conveyed from the classification distillation unit to any collection container.

[0038] Without departing from the scope of this disclosure, those skilled in the art can make various changes to the shape, size, number, separation characteristics, and / or arrangement of the components. According to some embodiments, each disclosed component, system, and process step can be performed in connection with and in any order with any other disclosed component, system, or process step. When the verb "may" appears, it is intended to convey optional and / or permitted conditions, but its use is not intended to imply any lack of operability unless otherwise stated. Those skilled in the art can make various changes in the preparation and use of the compositions, apparatus, and / or systems of this disclosure. Where desired, some embodiments of this disclosure can be practiced to exclude other embodiments.

[0039] Furthermore, where a range has been provided, the disclosed endpoints can be considered as precise values ​​and / or approximate values ​​as desired or required by a particular embodiment. Where the endpoints are approximate values, the degree of flexibility can vary proportionally to the order of magnitude of the range. For example, in one aspect, an endpoint of a range of about 50 in the context of a range of about 5 to about 50 may include 50.5, but not 52.5 or 55, and in another aspect, an endpoint of a range of about 50 in the context of a range of about 0.5 to about 50 may include 55, but not 60 or 75. Furthermore, in some embodiments, it may be desirable to mix and match range endpoints. Additionally, in some embodiments, each disclosed figure (e.g., in one or more of the examples, tables, and / or figures) may form the basis of the range (e.g., depicted values ​​+ / - about 10%, depicted values ​​+ / - about 50%, depicted values ​​+ / - about 100%) and / or range endpoints. Regarding the former, the value 50 depicted in the examples, tables and / or figures may form the basis of, for example, a range of about 45 to about 55, about 25 to about 100 and / or about 0 to about 100.

[0040] These equivalents and substitutes, as well as obvious changes and modifications, are intended to be included within the scope of this disclosure. Therefore, the foregoing disclosure is intended to illustrate, and not limit, the scope of this disclosure as defined by the appended claims.

[0041] The title of the invention, the abstract, the background art, and the subheadings are provided in accordance with regulations and / or for the convenience of the reader. They do not include an admission of the scope and content of the prior art, nor do they include limitations applicable to all disclosed embodiments.

Claims

1. A method for generating a stripped fluid with reduced chloride content, the method comprising: The feed is hydrotreated in a hydrotreatment reactor to obtain a hydrotreated effluent with a chloride concentration in the range of 0.1 wppm to 100 wppm, and the chloride is stripped from the hydrotreated effluent using a hot high-pressure stripper to produce stripped fluid and vapor effluent. The stripped fluid contains a lower chloride content than the hydrotreated effluent, and the hydrotreated reactor is connected to the hot high-pressure stripper via a first heat exchanger. A portion of the stripping fluid from the hot high-pressure stripper is used to heat the feed to the hydrotreating reactor via a second heat exchanger. The first heat exchanger cools and partially condenses the effluent from the hydrotreatment reactor, and increases the feed temperature through heat exchange with the effluent. The second heat exchanger transfers heat to the first heat exchanger.

2. The method of claim 1, wherein the method comprises exposing the hydrotreated effluent to a stripping gas containing a hydrogen concentration ranging from 50% to 99% hydrogen by volume of the stripping gas.

3. The method according to claim 1, the method further comprising maintaining the hot high-pressure stripper at a temperature ranging from 200°C to 350°C.

4. The method according to claim 1, wherein the method further comprises: In a hydrotreating reactor, a feed fluid containing hydrocarbons and chlorides with a content greater than 1 w ppm is combined with a hydrogen-rich gas in the presence of a catalyst to produce a hydrotreated effluent containing hydrocarbons and other compounds including hydrogen chloride and ammonia, as well as a hydrotreated fluid that can be used directly as a hydrocarbon product or can be further refined.

5. The method according to claim 4, wherein the method further comprises one or more of the following: The hydrogenation reactor is quenched with the stripped fluid; A portion of the stripped fluid is recycled back to the hydrotreating reactor; and The hydrogenated fluid is subjected to fractional distillation to produce at least a first hydrocarbon fraction and a second hydrocarbon fraction.

6. The method of claim 4, further comprising one or more of the following: The feed fluid and the hydrogen-rich gas are exposed to a catalyst, which includes one or more of a cobalt catalyst, a nickel catalyst, a molybdenum catalyst, a palladium catalyst, and a platinum catalyst. At least a portion of the stripped fluid is used to preheat the feed fluid to a temperature ranging from 25°C to 350°C before it enters the hydrotreatment reactor, and to maintain the hydrotreatment reactor at a temperature ranging from 200°C to 450°C.

7. A hydrotreatment system for generating stripped fluid with reduced chloride levels, the system comprising: (a) A hydrotreatment reactor, the hydrotreatment reactor being configured to produce a hydrotreated effluent and a hydrotreated fluid from a feed fluid; and (b) A hot high-pressure stripper configured to strip chloride from the hydrotreatment effluent to generate the stripped fluid and vapor. (c) A second heat exchanger, wherein a portion of the stripped fluid from the hot high-pressure stripper supplies heat to the feed fluid of the hydrotreating reactor, and (d) A first heat exchanger for cooling and partially condensing the hydrotreatment reactor effluent and increasing the feed temperature by heat exchange with the hydrotreatment reactor effluent, wherein the stripped fluid contains a lower chloride content than the hydrotreatment reactor effluent. The vapor contains chloride, The second heat exchanger transfers heat to the first heat exchanger.

8. The hydrotreating system of claim 7, further comprising a fractionation unit including a fractionation tower, the fractionation unit being configured to receive the hydrotreated fluid from the hydrotreating reactor.

9. The hydrogenation treatment system according to claim 7, wherein the hydrogenation treatment system further comprises one or more of the following: A KO tank, which is connected to the hot high-pressure stripper via a stripping gas delivery line, wherein the KO tank is configured to contain hydrogen-rich gas, and wherein the stripping gas delivery line is configured to deliver the hydrogen-rich gas from the KO tank to the hot high-pressure stripper. A steam scrubbing unit configured to use water scrubbing to remove a portion of the chloride from the steam to produce clean hydrocarbons.

10. The hydrogenation treatment system according to claim 8, wherein the hydrogenation treatment system further comprises one or more of the following: A stripped fluid collection container is connected to the hot high-pressure stripper via a stripped fluid delivery line, wherein the stripped fluid collection container is configured to receive a portion of the stripped fluid from the hot high-pressure stripper via the stripped fluid delivery line. A quenching facility connected to the hot high-pressure stripper and the hydrotreating reactor, wherein the quenching facility is configured to receive a portion of the stripped fluid from the hot high-pressure stripper, and wherein the quenching facility is further configured to deliver a portion of the stripped fluid to the hydrotreating reactor. and A second hydrotreating stage is connected via a second-stage connector to one or more of the hot high-pressure stripper and the stripped fluid collection container, wherein the second hydrotreating stage is configured to receive a portion of the stripped fluid from one or more of the hot high-pressure stripper and the stripped fluid collection container via the second-stage connector.

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