Memory, isomerization process parameter control method, device and equipment

Abstract

The present invention discloses a storage device, an isomerization process parameter control method, a device and equipment, wherein the method comprises the steps of: obtaining the current flow rate of the side-line circulating logistics of the isomerization process device, the current operating temperature of the reactor and the current octane number of the product; adjusting the flow rate of the side-line circulating logistics multiple times within a preset flow rate range and obtaining the corresponding experimental octane numbers respectively; calculating the flow correction coefficient according to a first relationship formula; adjusting the operating temperature of the reactor multiple times within a preset temperature range and obtaining the corresponding experimental octane numbers respectively; and calculating the temperature correction coefficient according to a second relationship formula; determining the expected octane number of the device and determining the adapted flow rate of the side-line circulating logistics and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula; the present invention realizes the optimization and adjustment of the process parameters of the isomerization process device according to the adapted flow rate and / or the adapted operating temperature.

Description

Technical Field

[0001] The invention relates to the field of oil refining, and in particular to a storage device, an isomerization process parameter control method, a device and equipment. Background Art

[0002] The octane number of the crude oil can be effectively improved by isomerizing normal (C5 / C6) alkanes using isomerization processes such as straight-run gasoline or reforming raffinate.

[0003] There are many adjustable parameters in the operation of isomerization process. Different adjustable parameters affect product quality and separation energy consumption in different ways and degrees. By establishing a systematic parameter control method in the isomerization process, the purpose of controlling the product quality and device energy consumption of the isomerization process unit can be achieved.

[0004] The prior art includes:

[0005] Firstly, based on the combustion chemistry model of hydrocarbons in the cylinder, the combustion process was decomposed and a theory was proposed that the octane number is determined by the conversion rate of active nuclei in the system. Based on this, the octane number was calculated, thereby analyzing the contribution or influence of the nonlinear blending effect of each blending component in the raw oil during the blending process on the octane number of gasoline.

[0006] Then, the blending scheme of the raw oil is determined according to the contribution or influence of the nonlinear blending effect of each blending component on the gasoline octane number during the blending process, thereby achieving the purpose of improving the effect of isomerization of normal alkanes.

[0007] After research, the inventors found that the above-mentioned adjustable parameter control method in the prior art requires obtaining parameters that are difficult to measure, such as the reaction rate of each component to generate free radicals and the active core content, and is therefore not suitable for actual industrial applications.

[0008] The information disclosed in this background technology section is only intended to enhance the understanding of the overall background of the invention and should not be regarded as an acknowledgment or any form of suggestion that the information constitutes the prior art already known to a person skilled in the art. Summary of the invention

[0009] The purpose of the present invention is to avoid obtaining parameters that are difficult to measure, such as the reaction rate of each component to generate free radicals and the content of active cores, so as to be suitable for actual industrial applications.

[0010] The present invention provides a method for controlling isomerization process parameters, comprising the steps of:

[0011] S11, obtaining the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product;

[0012] S12, adjusting the flow rate of the side-line circulating stream multiple times within a preset flow rate range, and obtaining the corresponding experimental octane numbers respectively; and calculating the flow rate correction coefficient α according to the first relationship formula;

[0013] (First relation formula);

[0014] Among them, F is the flow value before adjustment; F° is the flow value after adjustment; RON is the octane number before flow adjustment; RON′ is the octane number after flow adjustment;

[0015] S13, adjusting the operating temperature of the reactor multiple times within a preset temperature range, and obtaining corresponding experimental octane numbers respectively; and calculating the temperature correction coefficient β according to the second relationship formula;

[0016] (Second relation formula);

[0017] Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment;

[0018] S14, determining the expected octane number of the isomerization process unit, and determining the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula;

[0019] The third relationship formula;

[0020] The third relationship formula is generated by fitting the first relationship formula and the second relationship formula.

[0021] In the present invention, the flow rate of the sideline circulating stream is adjusted within a preset flow rate range, and the corresponding experimental octane number is obtained; and the flow rate correction coefficient is calculated according to the first relationship formula, including:

[0022] Setting a plurality of target flow values ​​equidistantly within the flow range;

[0023] Using the plurality of target flow values ​​as flow control targets, adjusting the flow of the side-line circulating stream in sequence, and obtaining the experimental octane number corresponding to each adjustment;

[0024] Calculate the preliminary flow correction coefficient corresponding to each adjustment according to the target flow value and experimental octane number corresponding to each adjustment;

[0025] The flow correction coefficient is generated by calculating the average of a plurality of the preliminary flow correction coefficients.

[0026] In the present invention, the operating temperature of the reactor is adjusted within a preset temperature range, and the corresponding experimental octane number is obtained; and the temperature correction coefficient is calculated according to the second relationship formula, including:

[0027] Setting a plurality of target temperature values ​​equidistantly within the temperature range;

[0028] Using the plurality of target temperature values ​​as temperature control targets, sequentially adjusting the operating temperature of the reactor, and obtaining an experimental octane number corresponding to each adjustment;

[0029] Calculate the preliminary temperature correction coefficient corresponding to each adjustment according to the target temperature value and the experimental octane number corresponding to each adjustment;

[0030] The temperature correction coefficient is generated by calculating the average of a plurality of the preliminary temperature correction coefficients.

[0031] In the present invention, the multiple target flow values ​​are set equidistantly within the flow range, including:

[0032] With 0.1 t / h as the flow span value of adjacent target flow values, multiple target flow values ​​are equidistantly set within the flow range.

[0033] In the present invention, the setting of multiple target temperature values ​​equidistantly within the temperature range includes:

[0034] With 1° C. as the temperature span value of adjacent target temperature values, a plurality of target temperature values ​​are equidistantly set within the temperature range.

[0035] In the present invention, the step of determining the expected octane number of the device and determining the flow rate of the side circulation stream and / or the adjustment amount of the operating temperature of the reactor according to the calculation of the third relationship formula comprises:

[0036] Determining a preset composition of the product oil of the device, and determining an adapted operating temperature of the reactor according to the preset composition;

[0037] The adapted operating temperature is substituted into the third relationship formula as T' value, and the adjustment amount of the flow rate of the side line circulating stream is generated according to the third relationship formula.

[0038] In the present invention, the calculation formula for determining the adapted operating temperature of the reactor according to the preset composition includes:

[0039]

[0040] Where T(c) is the octane number of the adjusted product isomerized oil, E i is the activation energy of each isomerization reaction, A iis the pre-exponential factor of each isomerization reaction, c i is the mass fraction of each monomer hydrocarbon, Δ i is the mass fraction of monomer hydrocarbons converted from the upper reaction.

[0041] In another aspect of the present invention, there is also provided an isomerization process parameter control device, comprising:

[0042] A basic data acquisition unit, used to acquire the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product;

[0043] A flow coefficient calculation unit, used to adjust the flow of the side-line circulating stream multiple times within a preset flow range, and obtain the corresponding experimental octane numbers respectively; and calculate the flow correction coefficient α according to the first relationship formula;

[0044] (First relation formula);

[0045] Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment;

[0046] A temperature coefficient calculation unit is used to adjust the operating temperature of the reactor multiple times within a preset temperature range and obtain the corresponding experimental octane numbers respectively; and calculate the temperature correction coefficient β according to the second relationship formula;

[0047] (Second relation formula);

[0048] Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment;

[0049] An adjustment scheme generating unit is used to determine the expected octane number of the isomerization process unit, and determine the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula;

[0050] The third relationship formula;

[0051] The third relationship formula is generated by fitting the first relationship formula and the second relationship formula.

[0052] In another aspect of the present invention, a memory is provided, comprising a software program, wherein the software program is suitable for a processor to execute the steps of the above-mentioned isomerization process parameter control method.

[0053] On the other hand, an embodiment of the present invention further provides an isomerization process parameter control device, which includes a computer program stored in a memory, and the computer program includes program instructions. When the program instructions are executed by a computer, the computer executes the methods described in the above aspects and achieves the same technical effects.

[0054] Compared with the prior art, the present invention has the following beneficial effects:

[0055] In the present invention, two process parameters, namely, the flow rate control of the side-line circulating stream of the isomerization process unit and the operating temperature of the reactor, are used as control objects for optimizing the octane number of the product oil; in the present invention, a specific relationship formula (third relationship formula) is also set to characterize the correspondence between the flow rate control of the side-line circulating stream of the isomerization process unit and the operating temperature of the reactor and the octane number of the product oil; in the third relationship formula, the adaptive flow rate of the side-line circulating stream and the adaptive operating temperature of the reactor can be determined according to the current octane number of the product oil, the current flow rate control of the side-line circulating stream of the isomerization process unit, the current operating temperature of the reactor, and the expected octane number of the product oil.

[0056] Through the present invention, the minimum flow rate of the side-line circulation stream required to achieve the expected octane number of the product oil, or the minimum value of the required operating temperature of the reactor, or the combination of the flow rate of the side-line circulation stream and the operating temperature of the reactor that can save the most energy can be obtained. Thus, the process parameters of the isomerization process device can be optimized and adjusted according to the adapted flow rate and / or adapted operating temperature.

[0057] As can be seen from the above, the present invention does not need to obtain parameters that are difficult to measure, such as the reaction rate of each component to generate free radicals and the active core content, and is therefore suitable for practical industrial applications.

[0058] The above description is only an overview of the technical solution of the present invention. In order to more clearly understand the technical means of the present invention and implement it according to the contents of the specification, and to make the above and other purposes, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with the accompanying drawings as follows. BRIEF DESCRIPTION OF THE DRAWINGS

[0059] Figure 1 It is a step diagram of the isomerization process parameter control method described in the present invention;

[0060] Figure 2 It is a schematic diagram of the structure of the isomerization process parameter control device of the present invention;

[0061] Figure 3It is a schematic diagram of the structure of the isomerization process parameter control equipment described in the present invention. DETAILED DESCRIPTION

[0062] The specific implementation modes of the present invention are described in detail below in conjunction with the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific implementation modes.

[0063] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.

[0064] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.

[0065] Embodiment 1

[0066] In order to avoid the difficulty in measuring parameters such as the reaction rate of each component to generate free radicals and the content of active cores, a control scheme for isomerization process parameters is generated to be suitable for actual industrial applications, such as Figure 1 As shown, in an embodiment of the present invention, a method for controlling isomerization process parameters is provided, comprising the steps of:

[0067] S11, obtaining the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product;

[0068] For the isomerization cycle process, the increase in the flow rate of the side cycle stream of the isomerization process unit and the increase in the operating temperature of the reactor will increase the octane number of the product oil.

[0069] The overall inventive concept of the embodiment of the present invention is: by regulating the flow rate of the side-line circulating logistics of the isomerization process unit and the operating temperature of the reactor, the isomerization circulation process is optimized so that the flow rate of the side-line circulating logistics and the operating temperature of the reactor can be as low as possible under the premise that the octane number of the product oil reaches the expected level, thereby reducing energy consumption and avoiding unnecessary energy waste.

[0070] In the embodiment of the present invention, for the target isomerization process unit, firstly, the current flow rate of the side-line circulating stream, the current operating temperature of the reactor, and the current octane number of the product are obtained.

[0071] S12, adjusting the flow rate of the side-line circulating stream multiple times within a preset flow rate range, and obtaining the corresponding experimental octane numbers respectively; and calculating the flow rate correction coefficient α according to the first relationship formula;

[0072] In the embodiment of the present invention, according to the curve graph corresponding to the octane number and the current flow rate of the side-line circulating stream of the isomerization process unit and the current operating temperature of the reactor, a fitting formula form closest to the curve graph can be selected according to curve fitting forms such as linear fitting, power function fitting, and polynomial fitting, and a relationship formula (first relationship formula) between the octane number and the flow rate of the side-line circulating stream of the isomerization process unit, as well as a relationship formula (second relationship formula) between the octane number and the operating temperature of the reactor can be established respectively.

[0073] In the embodiment of the present invention, the relationship between the octane number and the flow rate of the side-line circulating stream of the isomerization process unit can be expressed as follows:

[0074] (First relation formula);

[0075] Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment; α is the flow correction coefficient;

[0076] In practical applications, it is necessary to obtain the flow correction coefficient α in the first relational formula applicable to the isomerization process unit according to different flow values ​​of the side-line circulating stream of the isomerization process unit and the corresponding octane number, specifically:

[0077] S121, setting a plurality of target flow values ​​equidistantly within the flow range;

[0078] The flow range in the embodiment of the present invention may be equivalent to the flow adjustment range of the side-line circulating logistics of the isomerization process unit, and those skilled in the art may determine it according to actual working conditions, and no specific limitation is made here.

[0079] In the embodiment of the present invention, the purpose of setting a plurality of target flow values ​​is to obtain a plurality of data samples that can reflect the corresponding relationship between the octane number and the flow rate of the side-line circulating stream of the isomerization process unit.

[0080] In practical applications, multiple target flow values ​​can be set equidistantly within the flow range. Specifically, 0.1 t / h is used as the flow span value of adjacent target flow values, and multiple target flow values ​​are set equidistantly within the flow range. For example, if the span of the preset flow range is 10 t / h, 100 (10 / 0.1) target flow values ​​can be set.

[0081] S122, using the plurality of target flow values ​​as flow control targets, adjusting the flow of the side-line circulation stream in sequence, and obtaining an experimental octane number corresponding to each adjustment;

[0082] After each adjustment of the flow rate of the side-line circulating stream, the corresponding experimental octane number is obtained, thereby forming a plurality of data samples that can reflect the corresponding relationship between the octane number and the flow rate of the side-line circulating stream of the isomerization process unit.

[0083] S123, calculating a preliminary flow correction coefficient corresponding to each adjustment according to the target flow value and the experimental octane number corresponding to each adjustment;

[0084] By bringing a plurality of data samples capable of reflecting the corresponding relationship between the octane number and the flow rate of the side-line circulating stream of the isomerization process unit into the first relationship formula, the preliminary flow rate correction coefficient after each adjustment can be solved;

[0085] For example, after setting 100 target flow values, 100 adjustments are required, and the adjustment range is 0.1 t / h each time. After each adjustment, the flow correction coefficient corresponding to each adjustment can be calculated according to the target flow value and experimental octane number corresponding to each adjustment. The flow correction coefficient obtained after this adjustment can be called the preliminary flow correction coefficient. The 100 preliminary flow correction coefficients can be α1~α 100 .

[0086] S124. Generate the flow correction coefficient by calculating the average of the plurality of preliminary flow correction coefficients.

[0087] In order to increase the universality of the flow correction coefficient in different flow ranges, in the embodiment of the present invention, a universal flow correction coefficient α is obtained by calculating the average of multiple preliminary flow correction coefficients.

[0088] S13, adjusting the operating temperature of the reactor multiple times within a preset temperature range, and obtaining corresponding experimental octane numbers respectively; and calculating the temperature correction coefficient β according to the second relationship formula;

[0089] In the embodiment of the present invention, the relationship between the octane number and the operating temperature of the reactor can be expressed as follows:

[0090] (Second relation formula);

[0091] Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment;

[0092] In practical applications, it is necessary to obtain the flow correction coefficient β in the second relationship formula applicable to the isomerization process unit according to the different operating temperatures of the reactor and the corresponding octane numbers. Specifically:

[0093] S131, setting a plurality of target temperature values ​​equidistantly within the temperature range;

[0094] The temperature range in the embodiment of the present invention may be equivalent to the temperature adjustment range of the reactor, and those skilled in the art may determine it according to actual working conditions, and no specific limitation is made here.

[0095] In the embodiment of the present invention, the purpose of setting multiple target temperature values ​​is to obtain multiple data samples that can reflect the corresponding relationship between the octane number and the operating temperature of the reactor flow.

[0096] In practical applications, multiple target temperature values ​​may be set equidistantly within the temperature range. Specifically, multiple target temperature values ​​may be set equidistantly within the temperature range, with 1°C being the temperature span value of adjacent target temperature values. For example, if the overall span of the preset flow temperature range is 30°C, 30 (30 / 1) target temperature values ​​may be set.

[0097] S132, using the plurality of target temperature values ​​as temperature control targets, adjusting the operating temperature of the reactor in sequence, and obtaining an experimental octane number corresponding to each adjustment;

[0098] After each adjustment of the operating temperature of the reactor, the corresponding experimental octane number is obtained, thereby forming a plurality of data samples that can reflect the corresponding relationship between the octane number and the operating temperature of the reactor.

[0099] S133, calculating a preliminary temperature correction coefficient corresponding to each adjustment according to the target temperature value and the experimental octane number corresponding to each adjustment;

[0100] By substituting a plurality of data samples that can reflect the corresponding relationship between the octane number and the operating temperature of the reactor into the second relationship formula, the preliminary temperature correction coefficient after each adjustment can be solved;

[0101] For example, after setting 30 target temperature values, 30 adjustments are required, and each adjustment range is 1°C. After each adjustment, the temperature correction coefficient corresponding to each adjustment can be calculated based on the target flow value and experimental octane number corresponding to each adjustment. The temperature correction coefficient obtained after this adjustment can be called the preliminary temperature correction coefficient. The 30 preliminary temperature correction coefficients can be β1~β2, respectively. 30 .

[0102] S134. Generate the temperature correction coefficient by calculating the average of the multiple preliminary temperature correction coefficients.

[0103] In order to increase the universality of the temperature correction coefficient in different temperature ranges, in the embodiment of the present invention, a universal temperature correction coefficient β is obtained by calculating the average of multiple preliminary temperature correction coefficients.

[0104] S14, determining the expected octane number of the isomerization process unit, and determining the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula;

[0105] The third relationship formula; the third relationship formula is generated by fitting the first relationship formula and the second relationship formula.

[0106] By fitting the first relational formula and the second relational formula, a third relational formula with known flow correction coefficient α and temperature correction coefficient β can be obtained.

[0107] The expected octane number in the embodiment of the present invention refers to the set index for the octane number of the product oil of the isomerization process unit in the embodiment of the present invention; after the expected octane number RON′ is determined, it is necessary to obtain the current octane number RON of the isomerization process unit, the current flow rate F of the side-line circulating stream, and the current operating temperature T of the reactor;

[0108] By substituting the above-mentioned expected octane number RON′, the current octane number RON of the isomerization process unit, the current flow rate F of the side-line circulation logistics, and the current operating temperature T of the reactor into the third relationship formula with known flow correction coefficient α and temperature correction coefficient β, the flow rate (F′) and operating temperature (T′) adapted to the expected octane number can be obtained according to the adjustment step of the flow rate and the adjustment step of the temperature.

[0109] Furthermore, in an embodiment of the present invention, the expected component composition of the product oil of the isomerization process unit can be set first, and then the corresponding ideal reaction temperature can be calculated as the adapted operating temperature of the reactor; then, the adapted operating temperature can be substituted into the third relationship formula as T′; in this way, by solving the adapted flow rate (F′) which is the only unknown number in the third relationship formula, the minimum flow rate of the side-line circulation logistics required for the product oil to reach the expected octane number can be obtained.

[0110] Determining the operating temperature adapted for the reactor according to the preset composition comprises:

[0111]

[0112] Where T(c) is the operating temperature of the reactor, E i is the activation energy of each isomerization reaction, A i is the pre-exponential factor of each isomerization reaction, ci is the mass fraction of each monomer hydrocarbon, Δ i is the mass fraction of monomer hydrocarbons converted from the upper reaction.

[0113] In summary, in the embodiment of the present invention, the two process parameters of the flow rate control of the side-line circulating stream of the isomerization process unit and the operating temperature of the reactor are used as the control objects for optimizing the octane number of the product oil; in the present invention, a specific relationship formula (the third relationship formula) is also set to characterize the correspondence between the flow rate control of the side-line circulating stream of the isomerization process unit and the operating temperature of the reactor and the octane number of the product oil; in the third relationship formula, the adaptive flow rate of the side-line circulating stream and the adaptive operating temperature of the reactor can be determined according to the current octane number of the product oil, the current flow rate control of the side-line circulating stream of the isomerization process unit, the current operating temperature of the reactor, and the expected octane number of the product oil.

[0114] Through the embodiments of the present invention, the minimum flow rate of the side-line circulation stream required to achieve the expected octane number of the product oil, or the minimum value of the required operating temperature of the reactor, or the combination of the flow rate of the side-line circulation stream and the operating temperature of the reactor that can save the most energy can be obtained. Thus, the process parameters of the isomerization process device can be optimized and adjusted according to the adapted flow rate and / or adapted operating temperature.

[0115] As can be seen from the above, the embodiments of the present invention do not need to obtain parameters that are difficult to measure, such as the reaction rate of each component to generate free radicals and the active core content, and are therefore suitable for actual industrial applications.

[0116] Embodiment 2

[0117] In another aspect of the embodiment of the present invention, a device for controlling isomerization process parameters is also provided. Figure 2 The schematic diagram of the structure of the isomerization process parameter control device provided in the embodiment of the present invention is shown. Figure 1 The device corresponding to the isomerization process parameter control method described in the corresponding embodiment, that is, implemented by a virtual device Figure 1 In the corresponding embodiment of the isomerization process parameter control method, each virtual module constituting the isomerization process parameter control device can be executed by an electronic device, such as a network device, a terminal device, or a server. Specifically, the isomerization process parameter control device in the embodiment of the present invention includes:

[0118] The basic data acquisition unit 01 is used to obtain the current flow rate of the side circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product;

[0119] The flow coefficient calculation unit 02 is used to adjust the flow of the side-line circulation flow multiple times within a preset flow range, and obtain the corresponding experimental octane number respectively; and calculate the flow correction coefficient α according to the first relationship formula;

[0120] (First relation formula);

[0121] Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment;

[0122] The temperature coefficient calculation unit 03 is used to adjust the operating temperature of the reactor multiple times within a preset temperature range, and obtain the corresponding experimental octane number respectively; and calculate the temperature correction coefficient β according to the second relationship formula;

[0123] (Second relation formula);

[0124] Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment;

[0125] The adjustment scheme generating unit 04 is used to determine the expected octane number of the isomerization process unit, and determine the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula;

[0126] The third relationship formula;

[0127] The third relationship formula is generated by fitting the first relationship formula and the second relationship formula.

[0128] Since the working principle and beneficial effects of the isomerization process parameter control device in the embodiment of the present invention have been Figure 1 The corresponding isomerization process parameter control method is also recorded and explained, so they can be cross-referenced and will not be repeated here.

[0129] Embodiment 3

[0130] In an embodiment of the present invention, a memory is further provided, wherein the memory includes a software program, and the software program is suitable for the processor to execute Figure 1 The corresponding steps in the isomerization process parameter control method.

[0131] The embodiments of the present invention can be implemented by means of a software program, that is, by writing a program for implementing Figure 1The corresponding software program (and instruction set) for each step in the isomerization process parameter control method is stored in a storage device, and the storage device is arranged in a computer device, so that the software program can be called by the processor of the computer device to achieve the purpose of the embodiment of the present invention.

[0132] Embodiment 4

[0133] In an embodiment of the present invention, an isomerization process parameter control device is further provided. The memory included in the isomerization process parameter control device includes a corresponding computer program product. When the program instructions included in the computer program product are executed by a computer, the computer can execute the isomerization process parameter control method described in the above aspects and achieve the same technical effect.

[0134] Figure 3 Schematic diagram of the hardware structure of the isomerization process parameter control device of the electronic device according to the embodiment of the present invention. Figure 3 As shown, the device includes one or more processors 610, a bus 630, and a memory 620. Taking one processor 610 as an example, the device may also include: an input device 640, and an output device 650.

[0135] The processor 610, the memory 620, the input device 640 and the output device 650 may be connected via a bus or other means. Figure 3 The example of connecting through bus is taken in the following.

[0136] The memory 620 is a non-transitory computer-readable storage medium that can be used to store non-transitory software programs, non-transitory computer executable programs, and modules. The processor 610 executes various functional applications and data processing of the electronic device by running the non-transitory software programs, instructions, and modules stored in the memory 620, that is, the processing method of the above method embodiment is implemented.

[0137] The memory 620 may include a program storage area and a data storage area, wherein the program storage area may store an operating system, an application required for at least one function; the data storage area may store data, etc. In addition, the memory 620 may include a high-speed random access memory, and may also include a non-transitory memory, such as at least one disk storage device, a flash memory device, or other non-transitory solid-state storage device. In some embodiments, the memory 620 may optionally include a memory remotely arranged relative to the processor 610, and these remote memories may be connected to the processing device via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.

[0138] The input device 640 can receive input digital or character information and generate signal input. The output device 650 can include a display device such as a display screen.

[0139] The one or more modules are stored in the memory 620, and when executed by the one or more processors 610, perform:

[0140] S11, obtaining the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product;

[0141] S12, adjusting the flow rate of the side-line circulating stream multiple times within a preset flow rate range, and obtaining the corresponding experimental octane numbers respectively; and calculating the flow rate correction coefficient α according to the first relationship formula;

[0142] (First relation formula);

[0143] Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment;

[0144] S13, adjusting the operating temperature of the reactor multiple times within a preset temperature range, and obtaining corresponding experimental octane numbers respectively; and calculating the temperature correction coefficient β according to the second relationship formula;

[0145] (Second relation formula);

[0146] Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment;

[0147] S14, determining the expected octane number of the isomerization process unit, and determining the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula;

[0148] The third relationship formula;

[0149] The third relationship formula is generated by fitting the first relationship formula and the second relationship formula.

[0150] The above product can execute the method provided by the embodiment of the present invention, and has the functional modules and beneficial effects corresponding to the execution method. For technical details not described in detail in this embodiment, please refer to the method provided by the embodiment of the present invention.

[0151] In the several embodiments provided by the present invention, it should be understood that the disclosed systems, devices and methods can be implemented in other ways. For example, the device embodiments described above are only schematic. For example, the division of the units is only a logical function division. There may be other division methods in actual implementation, such as multiple units or components can be combined or integrated into another system, or some features can be ignored or not executed. Another point is that the mutual coupling or direct coupling or communication connection shown or discussed can be an indirect coupling or communication connection through some interfaces, devices or units, which can be electrical, mechanical or other forms.

[0152] The units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the units may be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0153] In addition, each functional unit in each embodiment of the present invention may be integrated into one processing unit, or each unit may exist physically separately, or two or more units may be integrated into one unit. The above-mentioned integrated unit may be implemented in the form of hardware or in the form of software functional units.

[0154] If the integrated unit is implemented in the form of a software functional unit and sold or used as an independent product, it can be stored in a computer-readable storage medium. Based on this understanding, the technical solution of the present invention is essentially or the part that contributes to the prior art or all or part of the technical solution can be embodied in the form of a software product. The computer software product is stored in a storage device, including several instructions to enable a computer device (which can be a personal computer, server, or network device, etc.) to perform all or part of the steps of the method described in each embodiment of the present invention. The aforementioned storage device includes: U disk, mobile hard disk, read-only memory (ROM, Read-Only Memory), random access memory (RAM, Random Access Memory), ReRAM, MRAM, PCM, NAND Flash, NOR Flash, Memristor, disk or optical disk and other media that can store program codes.

[0155] As described above, the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit the same. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some of the technical features thereof may be replaced by equivalents. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for controlling isomerization process parameters, characterized in that: include: S11, obtaining the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product; S12, adjusting the flow rate of the side-line circulation stream multiple times within a preset flow rate range, and obtaining corresponding experimental octane numbers respectively; And calculate the flow correction coefficient α according to the first relationship formula; First relation formula; Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment; S13, adjusting the operating temperature of the reactor multiple times within a preset temperature range, and obtaining corresponding experimental octane numbers respectively; and calculating the temperature correction coefficient β according to the second relationship formula; The second relational formula; Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment; S14, determining the expected octane number of the isomerization process unit, and determining the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula; The third relationship formula; The third relationship formula is generated by fitting the first relationship formula and the second relationship formula; The third relationship formula is used to determine the adaptive flow rate of the side-line circulation logistics and the adaptive operating temperature of the reactor according to the current octane number of the product oil, the current flow control of the side-line circulation logistics of the isomerization process unit, the current operating temperature of the reactor, and the expected octane number of the product oil.

2. The isomerization process parameter control method according to claim 1, characterized in that: The flow rate of the side-line circulating stream is adjusted multiple times within a preset flow rate range, and corresponding experimental octane numbers are obtained respectively; And the flow correction coefficient α is calculated according to the first relationship formula, including: Setting a plurality of target flow values ​​equidistantly within the flow range; Using the plurality of target flow values ​​as flow control targets, adjusting the flow of the side-line circulating stream in sequence, and obtaining the experimental octane number corresponding to each adjustment; Calculate the preliminary flow correction coefficient corresponding to each adjustment according to the target flow value and experimental octane number corresponding to each adjustment; The flow correction coefficient is generated by calculating the average of a plurality of the preliminary flow correction coefficients.

3. The isomerization process parameter control method according to claim 1, characterized in that: The operating temperature of the reactor is adjusted multiple times within a preset temperature range, and corresponding experimental octane numbers are obtained respectively; And the temperature correction coefficient β is calculated according to the second relationship formula, including: Setting a plurality of target temperature values ​​equidistantly within the temperature range; Using the plurality of target temperature values ​​as temperature control targets, sequentially adjusting the operating temperature of the reactor, and obtaining an experimental octane number corresponding to each adjustment; Calculate the preliminary temperature correction coefficient corresponding to each adjustment according to the target temperature value and the experimental octane number corresponding to each adjustment; The temperature correction coefficient is generated by calculating the average of a plurality of the preliminary temperature correction coefficients.

4. The isomerization process parameter control method according to claim 2, characterized in that: The multiple target flow values ​​are set equidistantly within the flow range, including: With 0.1 t / h as the flow span value of adjacent target flow values, multiple target flow values ​​are equidistantly set within the flow range.

5. The isomerization process parameter control method according to claim 3, characterized in that: The setting of multiple target temperature values ​​equidistantly within the temperature range comprises: With 1° C. as the temperature span value of adjacent target temperature values, a plurality of target temperature values ​​are equidistantly set within the temperature range.

6. The isomerization process parameter control method according to claim 1, characterized in that: The step of determining the expected octane number of the isomerization process unit and determining the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula comprises: Determining a preset composition of the product oil of the device, and determining an adapted operating temperature of the reactor according to the preset composition; The adapted operating temperature is substituted into the third relationship formula as T' value, and the adjustment amount of the flow rate of the side line circulating stream is generated according to the third relationship formula.

7. The isomerization process parameter control method according to claim 6, characterized in that: Also includes: The calculation formula for determining the adapted operating temperature of the reactor according to the preset composition includes: Where T(c) is the operating temperature of the reactor, E i is the activation energy of each isomerization reaction, A i is the pre-exponential factor of each isomerization reaction, c i is the mass fraction of each monomer hydrocarbon, Δ i is the mass fraction of monomer hydrocarbons converted from the upper reaction.

8. An isomerization process parameter control device, characterized in that: include: A basic data acquisition unit, used to acquire the current flow rate of the side-line circulation stream of the isomerization process unit, the current operating temperature of the reactor, and the current octane number of the product; A flow coefficient calculation unit, used to adjust the flow of the side-line circulating stream multiple times within a preset flow range, and obtain corresponding experimental octane numbers respectively; And calculate the flow correction coefficient α according to the first relationship formula; First relation formula; Among them, F is the flow value before adjustment; F' is the flow value after adjustment; RON is the octane number before flow adjustment; RON' is the octane number after flow adjustment; A temperature coefficient calculation unit is used to adjust the operating temperature of the reactor multiple times within a preset temperature range and obtain the corresponding experimental octane numbers respectively; and calculate the temperature correction coefficient β according to the second relationship formula; The second relational formula; Wherein, T is the temperature value before adjustment; T' is the temperature value after adjustment; RON is the octane number before temperature adjustment; RON' is the octane number after temperature adjustment; An adjustment scheme generating unit is used to determine the expected octane number of the isomerization process unit, and determine the adapted flow rate of the side-line circulation stream and / or the adapted operating temperature of the reactor according to the calculation of the third relationship formula; The third relationship formula; The third relationship formula is generated by fitting the first relationship formula and the second relationship formula; The third relationship formula is used to determine the adaptive flow rate of the side-line circulation logistics and the adaptive operating temperature of the reactor according to the current octane number of the product oil, the current flow control of the side-line circulation logistics of the isomerization process unit, the current operating temperature of the reactor, and the expected octane number of the product oil.

9. A memory, characterized in that: The method comprises a software program, wherein the software program is suitable for executing the steps of the isomerization process parameter control method according to any one of claims 1 to 7 by a processor.

10. An isomerization process parameter control device, characterized in that: comprising a bus, a processor and a memory as claimed in claim 9; The bus is used to connect the memory and the processor; The processor is configured to execute an instruction set in the memory.

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