Method and apparatus for heating hydrocarbon feed stream to reactor
By preheating and heating the feed stream, the hydrotreating reactor is enabled to operate in a lower temperature range, solving the problems of dew point margin and sulfur recombination, reducing the need for sulfur protection beds, and increasing the cycle length of the catalyst.
Patent Information
- Application Number
- CN202380053961.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Priority Date
- 2022-08-19
- Filing Date
- 2023-08-18
- Publication Date
- 2025-03-04
AI Technical Summary
Existing hydrotreatment reactors require high operating temperatures at the start of operation to solve the dew point margin problem, resulting in sulfur recombination and catalyst poisoning, and a sulfur protection bed is required to meet the sulfur limits of downstream treatment units.
By preheating the feed stream to form a vapor stream and further heating in the feed heater, the reactor is enabled to operate at a lower temperature range, thereby reducing the risk of sulfur recombination and catalyst poisoning and eliminating the need for sulfur protection beds.
The operation of the hydrotreatment reactor at a lower temperature range is achieved, reducing the risk of sulfur recombination and catalyst poisoning, reducing the need for sulfur protection beds, and increasing the cycle length of the catalyst.
Smart Images
Figure CN119563006A_ABST
Abstract
Description
[0001] Priority declaration
[0002] This application claims priority to U.S. patent application No. 63 / 371,905, filed on August 19, 2022, the entire contents of which are incorporated herein by reference. Technical Field
[0003] The present invention generally relates to methods and apparatus for heating a hydrocarbon feed stream to a reactor, and more particularly to methods and apparatus for heating a feed stream prior to passing the feed stream to a reactor to obtain a vapor stream for a fired heater. Background Art
[0004] Hydroprocessing is a catalytic chemical process widely used to remove sulfur, nitrogen and other heteroatoms from various hydrocarbon components in the refining process. The removal of sulfur compounds or more specifically sulfur hydrocarbon compounds such as mercaptans is important for reducing sulfur dioxide emissions and avoiding poisoning of precious metal catalysts (e.g., platinum, rhenium, etc.) in downstream catalytic reforming units for improving the octane number of naphtha streams. For example, heavy naphtha products with low octane numbers obtained by hydrocracking and / or hydrotreating processes must be catalytically "reformed" to improve the octane number. In addition, the presence of sulfur compounds will poison the catalyst used in the reforming unit.
[0005] However, when the reactor effluent material contains hydrogen sulfide above a certain temperature, recombinant sulfur compounds can be formed. The result is the formation of mercaptans, which affect the quality of certain products and boil in the naphtha range. This necessitates the need for a sulfur guard bed (SGB) to meet the sulfur limits of downstream processing units.
[0006] In addition, hydroprocessing reactors generally require a higher hydrogen to hydrocarbon ratio to meet the dew point margin when starting to operate the reactor feed heater. For full range and heavy naphtha hydroprocessing reactors, the requirement for the hydrogen to hydrocarbon ratio is sometimes at least 2 times the stoichiometric requirement.
[0007] New generation hydroprocessing catalysts have the ability to operate at temperatures below 316°C (600°F). However, dew point issues force hydroprocessing reactors to have operating temperatures of at least 316°C (600°F) or even 321°C to 327°C (610°F to 620°F) at the start of the run, but limit the reactor outlet temperature to 343°C (650°F) at the end of the run. This reduces the cycle length of the hydroprocessing catalyst, and at the same time, it results in sulfur recombination to form mercaptans.
[0008] Therefore, it would be desirable to have a more effective and efficient method to heat a feed stream to achieve dew point margin and address one or more of these issues. Summary of the invention
[0009] The present invention provides a method and apparatus for heating a feed stream to a reactor by alleviating the dew point margin problem of a feed heater having a lower hydrogen to hydrocarbon ratio. The present invention also allows a hydroprocessing reactor to be operated in the range of 304°C to 332°C (580°F to 630°F) from start to finish of the run to limit sulfur recombination reactions at higher reactor operating temperatures without dew point problems in the feed heater. This helps eliminate the need to treat SGB of the hydroprocessed naphtha stream for downstream processing units.
[0010] The present invention utilizes, for example, the feed heater outlet stream to preheat the feed at the feed heater inlet. This increases the feed heater inlet temperature and achieves the desired dew point margin. At the same time, this also allows the reactor to have a reactor inlet temperature of less than 316°C (600°F) when it starts running. This allows the reactor to operate at a lower range (typically 304°C to 332°C (580°F to 630°F)), thus reducing or eliminating sulfur recombination, and thus eliminating the need for SGB for most units. It is also contemplated that the effluent stream from the reactor can be heated and used to provide heat to the feed stream to achieve the dew point margin.
[0011] Thus, in at least one aspect, the present invention may be characterized in that a method for heating a hydrocarbon feed stream to a reactor is provided, the method being performed by the following steps: heating a hydrocarbon process stream associated with the reactor to provide a heated hydrocarbon process stream; transferring heat from the heated hydrocarbon process stream to the hydrocarbon feed stream to the reactor to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; conveying the heated hydrocarbon feed stream to the reactor; and recovering a hydrocarbon effluent stream from the reactor.
[0012] In one or more aspects, the present invention is generally characterized by providing a method for heating a hydrocarbon feed stream for a reactor, the method being carried out by the following steps: heating a hydrocarbon feed stream for a reactor in a heat exchanger to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream from the heat exchanger is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; conveying the heated hydrocarbon feed stream from the feed heater to the heat exchanger to heat the hydrocarbon feed stream and provide a preheated hydrocarbon feed stream; and, after the heated hydrocarbon feed stream has been conveyed to the heat exchanger, conveying the heated hydrocarbon feed stream to the reactor.
[0013] The present invention may also be broadly characterized in that, in one or more aspects, a method for heating a hydrocarbon feed stream to a reactor is provided, the method being carried out by the following steps: heating the hydrocarbon feed stream to the reactor in a heat exchanger to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; conveying the heated hydrocarbon feed stream to the reactor; recovering a hydrocarbon effluent stream from the reactor; heating the hydrocarbon effluent stream in a heating zone to provide a heated hydrocarbon effluent stream; and conveying the heated hydrocarbon effluent stream to the heat exchanger to heat the hydrocarbon feed stream and provide the preheated hydrocarbon feed stream.
[0014] Further aspects, embodiments and details of the invention (all of which may be combined in any manner) are set forth in the following detailed description of the invention. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] One or more exemplary embodiments of the present invention will be described below in conjunction with the following drawings, in which:
[0016] Figure 1 is a process flow diagram of one or more embodiments of the present invention; and,
[0017] Figure 2 is another process flow diagram of one or more embodiments of the present invention. DETAILED DESCRIPTION
[0018] As described above, the present invention relates to a hydrocarbon feed stream for heating a reactor. Typically, in the present invention, a hydrocarbon process stream associated with a reactor, such as a feed stream or a reactor effluent stream, is heated to provide a heated hydrocarbon process stream. Heat is transferred from the heated hydrocarbon process stream to the hydrocarbon feed stream of the reactor to provide a preheated hydrocarbon feed stream. The addition of heat causes the preheated hydrocarbon feed stream to be a vapor stream. The preheated hydrocarbon feed stream can then be heated in a feed heater to form a heated hydrocarbon feed stream. The heated hydrocarbon feed stream can be conveyed to a reactor, where the hydrocarbons will undergo some reaction, and the hydrocarbon effluent stream from the reactor can be recovered.
[0019] These processes allow for lower reactor temperatures while still avoiding dew point issues in the reactor's feed heater. This reduces sulfur recombination within the reactor relative to a hydroprocessing reactor and therefore reduces or eliminates the need for downstream sulfur management. Lower operating temperatures will also increase catalyst operating cycles and therefore improve catalyst cycle length.
[0020] Additionally, the process also utilizes a ratio of lower hydrocarbons to hydrogen of up to 50% for meeting the dew point margin of heavy / full range naphtha. This allows a smaller compressor to be used with the recycle hydrogen stream.
[0021] With these general principles in mind, one or more embodiments of the invention will be described with the understanding that the following description is not intended to be limiting.
[0022] An exemplary embodiment of the present invention for heating a hydrocarbon feed stream 10 to a reactor 12 in a reaction zone 14 is shown in Figure 1 In a preferred embodiment, reactor 12 is a naphtha hydroprocessing reactor, and preferably a gas phase hydroprocessing reactor. Therefore, the following description will proceed with the understanding that such features and descriptions are not intended to limit the described embodiments.
[0023] The source of hydrocarbon feed stream 10 is typically straight run naphtha, condensate based naphtha, any hydrocracked naphtha, coker naphtha, visbroken naphtha.
[0024] The hydrocarbon feed stream 10 is mixed with a recycle vapor stream 16 comprising hydrogen and then passed to a mixed feed heat exchanger 18. The hydrocarbon feed stream 10 is passed from the mixed feed heat exchanger 18 to a second heat exchanger 20. In the second heat exchanger 20, the hydrocarbon feed stream 10 is heated to provide a preheated hydrocarbon feed stream 22. The preheated hydrocarbon feed stream 22 is a vapor stream.
[0025] However, despite being a vapor stream, the temperature of the preheated hydrocarbon feed stream 22 will still be too low, and therefore, the preheated hydrocarbon feed 22 is passed to a feed heater or fired heater 24. In the feed heater 24, the preheated hydrocarbon feed 22 is further heated to provide a heated hydrocarbon feed stream 26. The heated hydrocarbon feed stream 26 may be passed from the feed heater 24 to a heat exchanger 20 to heat the hydrocarbon feed stream 10 and provide a preheated hydrocarbon feed stream 22.
[0026] The temperature of the preheated hydrocarbon feed stream 22 is above its dew point. This temperature will vary based on the dew point requirement of the preheated hydrocarbon feed stream 22 from the heat exchanger 20. Such temperatures are typically in the range of 274°C to 302°C (525°F to 575°F). The temperature of the heated hydrocarbon feed stream 26 from the feed heater will typically be in the range of 302°C to 360°C (575°F to 680°F).
[0027] After the heated hydrocarbon feed stream 26 is passed to the heat exchanger 20, it may then be passed to the reactor 12 which is operated under conditions to remove heteroatoms in the presence of a hydrotreating catalyst and provide a hydrotreated effluent 28. Suitable cobalt-molybdenum and / or nickel-molybdenum hydrotreating catalysts are known in the art.
[0028] The use of heated hydrocarbon feed stream 26 to provide heat to hydrocarbon feed stream 10 / preheated hydrocarbon stream 22 allows the temperature of reactor 12 to be lower than that conventionally used. Typical operating conditions for the reactor are in the range of 2,068 kPa to 5,516 kPa (300 psig to 800 psig) and 316°C to 343°C (600°F to 650°F). At the beginning of the reactor run, the operating temperature may be 304°C (580°F). In order to effectively remove metals and trace metals from the hydrocarbon feed stream 26, a minimum reactor operating temperature of 316°C (600°F) may be required. Therefore, a dedicated metal removal bed 29 may be used. In such cases, the reactor 12 may not require such a metal removal bed.
[0029] The maximum operating temperature of reactor 12 is below the sulfur reforming reaction temperature to eliminate or reduce the effects of sulfur reforming in reactor 12. As described above, this allows hydroprocessed effluent 28 to meet sulfur specifications of downstream processing units without the need for a secondary sulfur management / removal system.
[0030] The hydrotreated effluent 28 is passed to the mixed feed heat exchanger 18 to provide heat to the hydrocarbon feed stream 10. A water wash 30 from the mixed feed heat exchanger 18 may be mixed with the hydrotreated effluent 28 and the combined stream may be passed to a condenser 32 and then to a separation vessel 34.
[0031] In the separation vessel 34, the first liquid phase may be an aqueous phase including sour water 36. The second liquid phase is a hydrocarbon phase 38, which may be sent to a product recovery section 40, which typically includes a stripper 42 and another separation vessel 44 to separate the hydrocarbon phase 38 into various streams including an LPG stream 46 and a heavy naphtha stream 48, which may be sent to a platform (not shown). The product recovery section 40 is known in the art.
[0032] The vapor stream 50 from the separation vessel 34 contains hydrogen which may be mixed with additional hydrogen 52, compressed in a compressor 54, and then mixed with the feed stream 10 as a recycle vapor stream 16. As described above, one of the benefits of the present invention is that the amount of recycle vapor stream 16 mixed with the feed stream 10 may be reduced. This allows a smaller compressor 54 to be used. It is contemplated that the ratio of the recycle vapor stream 16 to the hydrocarbon feed stream 10 (in standard ft 3 / BPSD) is less than 2:1, preferably 1:1.
[0033] Steering Figure 2 In the embodiments of the present invention, in which the same reference numerals are used for the same features described above, it is also contemplated that the hydrotreated effluent stream 28 can be used as a process stream to heat the hydrocarbon feed stream 10 for the reactor 12 in the mixed feed heat exchanger 18, thereby providing a preheated hydrocarbon feed stream.
[0034] Thus, the hydrotreated effluent stream 28 is heated in the heating zone 56 to provide a heated hydrocarbon effluent stream 58. The heating zone 56 may include a heat exchanger 60 that receives steam or any hydrocarbon heat stream (vapor or liquid) of sufficient temperature. It is also contemplated that the heating zone 56 may include an electric heater or one or more electric heating coils. It is believed that the electric heater, which operates with electricity, may in turn reduce the size or even replace the charge (fired) heater 24. In addition, the electric heater provides the opportunity to use green electricity, which can be used to reduce greenhouse gas emissions and reduce the carbon footprint to achieve carbon neutrality.
[0035] The heated hydrocarbon effluent stream 58 is passed to the mixed feed heat exchanger 18, which heats the hydrocarbon feed stream 10 and provides a preheated hydrocarbon feed stream 22. The heated hydrocarbon effluent stream 58 from the mixed feed heat exchanger 18 may be processed in the same manner as discussed above with respect to effluent stream 28.
[0036] The preheated hydrocarbon feed stream 22, which is also a vapor stream, is passed to a feed heater 24 which provides a heated hydrocarbon feed stream 26. The heated hydrocarbon feed stream 26 may be passed from the feed heater 24 to the reactor 12.
[0037] The signals, measurements and / or data generated or recorded by the monitoring components may be transmitted to one or more controllers 62. The controller 62 may include at least one processor and a memory storing computer-readable instructions that, when executed by the at least one processor, cause the one or more controllers 62 to perform a method that may include one or more steps. For example, the one or more controllers 62 may be configured to receive data related to the following from one or more monitoring components, sensors, probes, etc.: at least one piece of equipment associated with the process or a process stream associated with the process. The one or more controllers 62 may be configured to analyze the data. Based on analyzing the data, the one or more controllers 62 may be configured to determine one or more recommended adjustments to one or more parameters of one or more methods described herein. The one or more controllers 62 may be configured to transmit encrypted or unencrypted data, which includes one or more recommended adjustments to one or more parameters of one or more methods described herein.
[0038] For example, in order to control the temperature of the various hydrocarbon streams 22, 26, the temperature sensor 64 can be used to measure or otherwise obtain the temperature of the various streams 22, 26. The obtained temperature can be sent to the controller 62. The controller 62 can compare the obtained temperature relative to a target temperature or a desired temperature or temperature range. If the obtained temperature is outside the desired range or is higher or lower than the target temperature, the controller 62 can send a signal to adjust one or more process conditions, thereby adjusting the amount of heat generated by the fired heater 24. For example, the controller 62 can send a signal to a valve or other piece of equipment to change the amount of fuel gas to the feed heater 24, change the residence time in the feed heater 24, the volume flow rate, the amount of combustion air delivered to the feed heater 24, etc. The adjusted process conditions result in changes in the operating parameters of the feed heater 24, so that the feed heater 24 operates at different temperatures to provide a heated hydrocarbon feed stream 26 with a temperature within the desired range or closer to the target temperature.
[0039] It should be understood that the network connections shown are exemplary and other means of establishing a communication link between the computers may be used. It is assumed that there are any of a variety of network protocols (such as TCP / IP, Ethernet, FTP, HTTP, etc.) and any of a variety of wireless communication technologies (such as GSM, CDMA, Wi-Fi, and WiMAX), and the various computing device parameter data system components described herein may be configured to communicate using any of these network protocols or technologies.
[0040] experiment
[0041] In a computer simulation of a hydroprocessing reactor according to the first embodiment, it was shown that dew point margin can be achieved by increasing the temperature of the feed heater. In addition, the ratio of hydrocarbons to hydrogen was halved. Similar results were predicted for simulations according to the second embodiment.
[0042] Those of ordinary skill in the art will recognize and appreciate that various other components such as valves, pumps, filters, coolers, etc. are not shown in the accompanying drawings because it is believed that their details are well within the knowledge of those of ordinary skill in the art and their description is not necessary for the practice or understanding of the embodiments of the present invention.
[0043] Any of the above-mentioned pipelines, conduits, units, equipment, containers, surrounding environments, zones, or the like may be equipped with one or more monitoring components, including sensors, measuring devices, data capture devices, or data transmission devices. Signals, process or state measurements and data from the monitoring components can be used to monitor conditions in, around, and related to the process equipment. The signals, measurements, and / or data generated or recorded by the monitoring components can be collected, processed, and / or transmitted via one or more networks or connections, which can be private or public, general or dedicated, direct or indirect, wired or wireless, encrypted or unencrypted, and / or combinations thereof; the present specification is not intended to be limiting in this regard.
[0044] Specific implementation plan
[0045] While the following is described in conjunction with specific embodiments, it should be understood that this description is intended to illustrate and not to limit the scope of the foregoing description and the appended claims.
[0046] A first embodiment of the present invention is a method for heating a hydrocarbon feed stream to a reactor, the method comprising heating a hydrocarbon process stream associated with the reactor to provide a heated hydrocarbon process stream; transferring heat from the heated hydrocarbon process stream to the hydrocarbon feed stream of the reactor to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; transferring the heated hydrocarbon feed stream to the reactor; and, recovering a hydrocarbon effluent stream from the reactor. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the first embodiment in this paragraph, wherein the hydrocarbon process stream comprises a hydrocarbon effluent stream from the reactor. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the first embodiment in this paragraph, wherein the hydrocarbon process stream comprises the hydrocarbon feed stream.
[0047] A second embodiment of the present invention is a method for heating a hydrocarbon feed stream to a reactor, the method comprising heating a hydrocarbon feed stream to a reactor in a heat exchanger to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream from the heat exchanger is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; transferring the heated hydrocarbon feed stream from the feed heater to the heat exchanger to heat the hydrocarbon feed stream and provide the preheated hydrocarbon feed stream; and, after the heated hydrocarbon feed stream has been transferred to the heat exchanger, transferring the heated hydrocarbon feed stream to the reactor. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the reactor comprises a gas phase hydroprocessing reactor. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the hydrocarbon feed stream is mixed with a recycled vapor stream. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the ratio of the feed stream to the recycle vapor stream is 1:1. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, further comprising measuring the temperature of the preheated hydrocarbon feed stream, the heated hydrocarbon feed stream, or both, and adjusting the process parameters associated with the fired heater based on the measured temperature to increase or decrease the amount of heat generated by the feed heater. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, further comprising measuring the temperature of the heated hydrocarbon feed stream. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the temperature of the heated hydrocarbon feed stream is measured between the feed heater and the heat exchanger. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the temperature of the heated hydrocarbon feed stream is measured between the heat exchanger and the reactor. One embodiment of the invention is one, any or all of the previous embodiments in this paragraph through the second embodiment in this paragraph, wherein the temperature of the heated hydrocarbon feed stream is also measured between the feed heater and the heat exchanger. One embodiment of the invention is one, any or all of the previous embodiments in this paragraph through the second embodiment in this paragraph, wherein the temperature of the heated feed stream is between 302°C and 360°C (575°F to 680°F). One embodiment of the invention is one, any or all of the previous embodiments in this paragraph through the second embodiment in this paragraph, wherein the temperature of the preheated feed stream is above the dew point of the preheated feed stream.One embodiment of the invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the temperature of the heated feed stream is between 302°C and 360°C (575°F to 680°F). One embodiment of the invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, wherein the maximum operating temperature of the reactor is below the sulfur recombination reaction temperature. One embodiment of the invention is one, any or all of the previous embodiments in this paragraph to the second embodiment in this paragraph, further comprising passing the heated hydrocarbon stream to a metal removal bed before passing the heated hydrocarbon stream to the heat exchanger.
[0048] A third embodiment of the present invention is a method for heating a hydrocarbon feed stream to a reactor, the method comprising heating a hydrocarbon feed stream to a reactor in a heat exchanger to provide a preheated hydrocarbon feed stream, wherein the preheated hydrocarbon feed stream is a vapor stream; heating the preheated hydrocarbon feed stream in a feed heater to form a heated hydrocarbon feed stream; conveying the heated hydrocarbon feed stream to the reactor; recovering a hydrocarbon effluent stream from the reactor; heating the hydrocarbon effluent stream in a heating zone to provide a heated hydrocarbon effluent stream; and conveying the heated hydrocarbon effluent stream to the heat exchanger to heat the hydrocarbon feed stream and provide the preheated hydrocarbon feed stream. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the third embodiment in this paragraph, wherein the reactor comprises a gas phase hydroprocessing reactor. An embodiment of the present invention is one, any one, or all of the previous embodiments in this paragraph to the third embodiment in this paragraph, wherein the hydrocarbon feed stream is mixed with a recycled vapor stream. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the third embodiment in this paragraph, wherein the heating zone comprises an electric heater or one or more electric heating coils. One embodiment of the present invention is one, any or all of the previous embodiments in this paragraph to the third embodiment in this paragraph, wherein the heating zone comprises a vapor heat exchanger or a process exchanger configured to receive a hydrocarbon heat stream.
[0049] Although there is no further detailed description, it is believed that those skilled in the art can utilize the present invention to the greatest extent by using the foregoing description and can easily determine the essential characteristics of the present invention without departing from the spirit and scope of the present invention to make various changes and modifications of the present invention and adapt it to various usages and conditions. Therefore, the aforementioned preferred specific embodiments should be understood as merely illustrative and not to limit the rest of the present disclosure in any way, and are intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.
[0050] In the foregoing, all temperatures are set forth in degrees Celsius and all parts and percentages are by weight unless otherwise indicated.
[0051] Although at least one exemplary embodiment has been presented in the foregoing specific embodiments of the present invention, it should be understood that there are a large number of variations. It should also be understood that an exemplary embodiment or multiple exemplary embodiments are only examples and are not intended to limit the scope, applicability or configuration of the present invention in any way. On the contrary, the foregoing specific embodiments will provide a convenient roadmap for those skilled in the art to implement the exemplary embodiments of the present invention, and it should be understood that various changes can be made to the functions and arrangements of the elements described in the exemplary embodiments without departing from the scope of the present invention as set forth in the attached claims and their legal equivalents.
Claims
1. A method for heating a hydrocarbon feed stream (10) to a reactor (12), the method comprising: heating a hydrocarbon process stream (26, 28) associated with the reactor (12) to provide a heated hydrocarbon process stream; transferring heat from the heated hydrocarbon process stream (26, 28) to the hydrocarbon feed stream (10) of the reactor (12) to provide a preheated hydrocarbon feed stream (22), wherein the preheated hydrocarbon feed stream (22) is a vapor stream; heating the preheated hydrocarbon feed stream (22) in a feed heater (24) to provide a heated hydrocarbon feed stream (26); passing the heated hydrocarbon feed stream (26) to the reactor (12); and, A hydrocarbon effluent stream (28) is recovered from the reactor (12).
2. The method of claim 1, wherein the hydrocarbon process stream (26, 28) comprises the hydrocarbon effluent stream (28) from the reactor (12).
3. The method of claim 1, wherein the hydrocarbon process stream (26, 28) comprises a heated hydrocarbon feed stream (26).
4. The process according to any one of claims 1 to 3, wherein the reactor (12) comprises a gas phase hydroprocessing reactor.
5. The process according to any one of claims 1 to 3, wherein the hydrocarbon feed stream (10) is mixed with a recycle vapor stream (16).
6. The process according to claim 5, wherein the ratio of the feed stream (10) to the recycle vapor stream (16) is 1:
1.
7. The method according to any one of claims 1 to 3, further comprising: measuring the temperature of the preheated hydrocarbon feed stream (22), the heated hydrocarbon feed stream (26), the hydrocarbon effluent stream (28), or any combination thereof, and, A process parameter associated with the feed heater (24) is adjusted based on the measured temperature to increase or decrease the amount of heat generated by the feed heater (24).
8. The process of any one of claims 1 to 3, wherein the temperature of the heated hydrocarbon feed stream (26) is between 302°C and 360°C (575°F and 680°F).
9. The process according to any one of claims 1 to 3, wherein the temperature of the preheated hydrocarbon feed stream (22) is above the dew point of the preheated hydrocarbon feed stream (22).
10. The method according to any one of claims 1 to 3, further comprising: heating the hydrocarbon effluent stream (28) in a heating zone (56) to provide a heated hydrocarbon effluent stream; as well as, The heated hydrocarbon effluent stream is passed to a heat exchanger (18) to heat the hydrocarbon feed stream (10) and provide the preheated hydrocarbon feed stream (22).