Feed ratio optimization method and system for heavy oil processing device and medium

Abstract

The invention provides a feed ratio optimization method and system for a heavy oil processing device and a computer readable storage medium. The feed ratio optimization method for the heavy oil processing device comprises the following steps: determining a sulfur transfer model according to linear models of a plurality of processing devices, wherein the plurality of processing devices comprise an atmospheric and vacuum distillation device, a heavy oil processing device and a tank field device; establishing a monitoring model related to the sulfur transfer model so as to monitor the feeding state of the heavy oil processing device in real time; and in response to the fact that the total feed sulfur content of the heavy oil processing device is higher than the feed sulfur content fortification value of the heavy oil processing device, solving the sulfur transfer optimization model by adopting a linear programming interior point method according to the real-time monitoring value of the monitoring model so as to determine the optimized feed flow of the heavy oil processing device, the sulfur transfer optimization model is established according to an optimization objective function and constraint conditions determined based on actual process conditions.

Description

Technical Field

[0001] The present invention relates to the field of heavy oil processing, and in particular to a feed ratio optimization method for a heavy oil processing device, a feed ratio optimization system for a heavy oil processing device, and a computer-readable storage medium. Background Art

[0002] In order to reduce costs during the refining process, refineries often choose to process sulfur-containing or high-sulfur crude oil. However, high sulfur in heavy oil can cause corrosion to production equipment, shorten equipment life and bring safety risks. If the total sulfur content of the feed of the heavy oil processing unit exceeds the standard, it may also cause unit failure or accidents, seriously affecting the stability of production. In addition, high sulfur will also reduce the effectiveness of catalysts and adsorbents, thereby affecting the efficiency of the unit and the economic benefits of the enterprise. Therefore, effectively controlling the total sulfur content of the feed of each heavy oil processing unit in the refining process has become one of the keys to ensure the safe operation of the refining unit and improve the competitiveness of the enterprise.

[0003] In the oil refining process, the existing technology for controlling the total sulfur content of the feed of heavy oil processing units is usually based on experience and rough estimates, lacking an accurate modeling method, and thus cannot effectively avoid the problem of excessive total sulfur content in the feed of the unit.

[0004] In order to overcome the above-mentioned defects of the prior art, the art urgently needs a feed ratio optimization technology for heavy oil processing equipment, which can effectively control and manage the total sulfur content of the feed of the heavy oil processing equipment, maintain the normal operation of the heavy oil processing equipment and extend the life cycle of the heavy oil processing equipment, effectively solve the problem of excessive sulfur content in the feed, and maximize the use of high-sulfur raw materials and improve resource utilization efficiency under the premise that the sulfur content meets the standard. Summary of the invention

[0005] A brief summary of one or more aspects is given below to provide a basic understanding of these aspects. This summary is not an exhaustive overview of all conceived aspects, and is neither intended to identify the key or critical elements of all aspects nor to define the scope of any or all aspects. Its only purpose is to give some concepts of one or more aspects in a simplified form as a prelude to a more detailed description that will be given later.

[0006] In order to overcome the above-mentioned defects of the prior art, the present invention provides a feed ratio optimization method for a heavy oil processing device, a feed ratio optimization system for a heavy oil processing device, and a computer-readable storage medium. By effectively controlling and managing the total sulfur content of the feed of the heavy oil processing device, the normal operation of the heavy oil processing device is maintained and the life cycle of the heavy oil processing device is extended, the problem of excessive sulfur content in the feed is effectively solved, and on the premise that the sulfur content meets the standard, the use of high-sulfur raw materials is maximized to improve resource utilization efficiency.

[0007] Specifically, the above-mentioned feed ratio optimization method for a heavy oil processing unit provided in accordance with the first aspect of the present invention comprises the steps of: determining a sulfur transfer model based on linear models of a plurality of processing units, the plurality of processing units including a constant pressure reduction unit, a heavy oil processing unit and a tank area unit; establishing a monitoring model related to the sulfur transfer model to monitor the feed status of the heavy oil processing unit in real time; in response to the total sulfur content of the feed of the heavy oil processing unit being higher than the defense value of the feed sulfur content of the heavy oil processing unit, solving the sulfur transfer optimization model using a linear programming interior point method according to the real-time monitoring value of the monitoring model to determine the optimized feed flow rate of the heavy oil processing unit, the sulfur transfer optimization model being established according to the optimization objective function and constraints determined based on actual process conditions.

[0008] Preferably, in an embodiment of the present invention, the optimization objective function is to minimize the difference between the total sulfur content of the feed of the heavy oil processing unit and the sulfur content defense value of the feed of the heavy oil processing unit.

[0009] Preferably, in one embodiment of the present invention, the optimization objective function Z is: Z = |MS(k)-∑ i,j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j))|min, where Q act i is the actual flow rate of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit, Si is the sulfur content of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit, TQ act j is the actual flow rate of the j-th side line of the direct supply tank of the tank area device to the heavy oil processing device, TSj is the sulfur content of the j-th side line of the direct supply tank to the heavy oil processing device, and MS(k) is the defense value of the feed sulfur content of the k-th heavy oil processing device.

[0010] Preferably, in one embodiment of the present invention, the step of solving the sulfur transfer optimization model using a linear programming interior point method based on the real-time monitoring value of the monitoring model to determine the optimized feed flow rate of the heavy oil processing unit includes: in response to the optimization objective function being in a nonlinear form, converting the optimization objective function into a linear form; and solving the optimization objective function using a linear programming interior point method to determine the optimized feed flow rate of the heavy oil processing unit.

[0011] Preferably, in one embodiment of the present invention, the heavy oil processing unit includes a delayed coking unit, a hydrocracking unit, a catalytic cracking unit, and a residual oil hydrogenation unit, and the tank area device includes a direct supply tank and a temporary storage tank.

[0012] Preferably, in one embodiment of the present invention, the constraints include sulfur balance constraints in the oil refining process, material balance constraints in the oil refining process, feed sulfur content defense value constraints, flow constraints, processing volume constraints, and tank capacity constraints.

[0013] Preferably, in one embodiment of the present invention, the real-time monitoring values ​​of the monitoring model include the real-time flow and sulfur content of each side line of the constant pressure reduction device, the real-time flow and sulfur content of each side line of the direct supply tank of the tank area device, and the defense value of the feed sulfur content of the heavy oil processing device.

[0014] Preferably, in one embodiment of the present invention, determining the optimized feed flow rate of the heavy oil processing unit includes determining the optimized feed flow rate of each side line of the constant pressure reduction unit to the heavy oil processing unit and the optimized feed flow rate of the direct supply tank of the tank area unit to the heavy oil processing unit.

[0015] In addition, the feed ratio optimization system for a heavy oil processing device provided according to the second aspect of the present invention includes a memory and a processor. The memory stores computer instructions. The processor is connected to the memory and is configured to execute the computer instructions stored in the memory to implement the feed ratio optimization method for a heavy oil processing device provided in any one of the above embodiments.

[0016] In addition, the computer readable storage medium provided according to the third aspect of the present invention stores computer instructions. When the computer instructions are executed by the processor, the feed ratio optimization method for a heavy oil processing device provided in any one of the above embodiments is implemented. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The above features and advantages of the present invention can be better understood after reading the detailed description of the embodiments of the present disclosure in conjunction with the following drawings. In the drawings, the components are not necessarily drawn to scale, and components with similar related properties or features may have the same or similar reference numerals.

[0018] Figure 1 A schematic diagram of a feed ratio optimization system for a heavy oil processing device provided according to some embodiments of the present invention is shown;

[0019] Figure 2 A flow chart of a feed ratio optimization method for a heavy oil processing device provided in some embodiments of the present invention is shown;

[0020] Figure 3 A simplified schematic diagram of a sulfur transfer model provided according to some embodiments of the present invention is shown;

[0021] Figure 4A schematic diagram of a process model related to wax oil provided according to some embodiments of the present invention is shown;

[0022] Figure 5 A comparative effect diagram of sulfur content control provided according to the first embodiment of the present invention is shown;

[0023] Figure 6 A comparative effect diagram of sulfur content control provided according to the second embodiment of the present invention is shown;

[0024] Figure 7 A schematic diagram of a process model related to residual oil provided in accordance with the third embodiment of the present invention is shown.

[0025] Reference numerals:

[0026] 100: Feed ratio optimization system for heavy oil processing unit;

[0027] 110: memory;

[0028] 111: Computer readable storage medium;

[0029] 120: Processor;

[0030] 200: Feed ratio optimization method for heavy oil processing unit;

[0031] 311: Direct supply tank;

[0032] 312: Temporary storage tank;

[0033] 320: Direct supply device part of the atmospheric and vacuum device;

[0034] 330: Heavy oil processing unit;

[0035] 411: 1# catalytic unit;

[0036] 412: 2# catalytic unit;

[0037] 420: 1# atmospheric and vacuum device 520;

[0038] 421: No. 1 normal pressure reducing device normal line 4;

[0039] 430: Catalytic low sulfur residue oil tank;

[0040] 441: Tank supply (DAO);

[0041] 442: Tank supply (wax residue) / direct supply;

[0042] 443: Tank supply (mixed wax oil);

[0043] 444: Supply of tanks G515 to G518;

[0044] 450: 1# cracked refined wax oil;

[0045] 461: Tank G931;

[0046] 462: G932 tank supply;

[0047] 470: 1# residue oil hydrogenated wax oil;

[0048] 471: 2# catalytic cycle oil;

[0049] 472: Purification of slurry oil;

[0050] 480: 5# hydrorefined wax oil;

[0051] 490: slag feeding tank;

[0052] 710: 3# atmospheric and vacuum device;

[0053] 711: Residue oil line of 3# atmospheric and vacuum unit;

[0054] 712: Washing oil line of 3# atmospheric and vacuum unit; and

[0055] S210~S230: steps. DETAILED DESCRIPTION

[0056] The present invention is described in detail below in conjunction with the accompanying drawings and specific embodiments. Note that the aspects described below in conjunction with the accompanying drawings and specific embodiments are only exemplary and should not be construed as limiting the scope of protection of the present invention in any way.

[0057] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0058] In addition, the terms "upper", "lower", "left", "right", "top", "bottom", "horizontal" and "vertical" used in the following description should be understood as the directions shown in the paragraph and the related drawings. Such relative terms are only used for the convenience of description and do not mean that the device described therein must be manufactured or operated in a specific direction, and therefore should not be understood as limiting the present invention.

[0059] It is understood that although the terms "first", "second", "third", etc. may be used herein to describe various components, regions, layers and / or parts, these components, regions, layers and / or parts should not be limited by these terms, and these terms are only used to distinguish different components, regions, layers and / or parts. Therefore, the first component, region, layer and / or part discussed below may be referred to as a second component, region, layer and / or part without departing from some embodiments of the present invention.

[0060] As mentioned above, in the oil refining process, the existing technology for controlling the total sulfur content of the feed to the device is usually based on experience and rough estimation, lacking an accurate modeling method, and thus cannot effectively avoid the problem of exceeding the total sulfur content of the feed to the device.

[0061] In order to overcome the above-mentioned defects of the prior art, the present invention provides a feed ratio optimization method for a heavy oil processing device, a feed ratio optimization system for a heavy oil processing device, and a computer-readable storage medium. By effectively controlling and managing the total sulfur content of the feed of the heavy oil processing device, the normal operation of the heavy oil processing device is maintained and the life cycle of the heavy oil processing device is extended, the problem of excessive sulfur content in the feed is effectively solved, and on the premise that the sulfur content meets the standard, the use of high-sulfur raw materials is maximized to improve resource utilization efficiency.

[0062] In some non-limiting embodiments, the feed ratio optimization method for a heavy oil processing device provided in the first aspect of the present invention can be implemented via the feed ratio optimization system for a heavy oil processing device provided in the second aspect of the present invention.

[0063] Please refer to Figure 1 , Figure 1 A schematic diagram of a feed ratio optimization system for a heavy oil processing unit provided according to some embodiments of the present invention is shown.

[0064] like Figure 1 As shown, the feed ratio optimization system 100 for a heavy oil processing device may be configured with a memory 110 and a processor 120. The memory 110 includes but is not limited to the computer-readable storage medium 111 provided in the third aspect of the present invention, on which computer instructions are stored. The processor 120 is connected to the memory 110 and is configured to execute the computer instructions stored in the memory 110 to implement the feed ratio optimization method for a heavy oil processing device provided in the first aspect of the present invention.

[0065] The following will first describe the working principle of the above-mentioned feed ratio optimization system for heavy oil processing equipment in conjunction with some embodiments of the feed ratio optimization method for heavy oil processing equipment. Those skilled in the art will understand that these embodiments of the feed ratio optimization method for heavy oil processing equipment are only some non-limiting implementation methods provided by the present invention, and are intended to clearly demonstrate the main concept of the present invention and provide some specific solutions that are convenient for the public to implement, rather than to limit all functions or all working modes of the feed ratio optimization system for heavy oil processing equipment. Similarly, the feed ratio optimization system for heavy oil processing equipment is also only a non-limiting implementation method provided by the present invention, and does not constitute a limitation on the execution subject and execution order of each step in these feed ratio optimization methods for heavy oil processing equipment.

[0066] Please refer to Figure 2 , Figure 2 A flow chart of a feed ratio optimization method for a heavy oil processing unit provided according to some embodiments of the present invention is shown.

[0067] like Figure 2 As shown, the feed ratio optimization method 200 for a heavy oil processing unit may include step S210: determining a sulfur transfer model according to linear models of multiple processing units, wherein the multiple processing units include a constant pressure reduction unit, a heavy oil processing unit, and a tank farm unit.

[0068] Please refer to Figure 3 , Figure 3 A simplified schematic diagram of a sulfur transfer model provided according to some embodiments of the present invention is shown.

[0069] like Figure 3 As shown, the feed ratio optimization system can determine the sulfur transfer model according to the linear model of multiple processing devices used in the oil refining process, and the multiple processing devices can be configured according to actual needs. The multiple processing devices can be a direct supply tank 311 of the tank farm device, a temporary storage tank 312 of the tank farm device, a direct supply device part 320 of the atmospheric and vacuum device, and a heavy oil processing device 330. Here, the heavy oil processing device 330 can include but is not limited to a delayed coking device, a hydrocracking device, a catalytic cracking device, and a residual oil hydrogenation device.

[0070] The processing device that feeds the heavy oil processing device 330 may include the direct supply tank 311 of the tank farm device and the direct supply device part 320 of the atmospheric and vacuum device. In the case where the flow of the direct supply device part 320 of the atmospheric and vacuum device to the heavy oil processing device 330 needs to be reduced, the reduced part of the flow may flow to the temporary storage tank 312 of the tank farm device. In other embodiments, the processing device that feeds the heavy oil processing device 330 may also include each feed stream of the heavy oil processing device 330.

[0071] Through the sulfur transfer model, the feed ratio optimization system can describe the distribution and flow of sulfur between different process units in the refining process, so as to accurately calculate the sulfur content of each unit.

[0072] Afterwards, the feed ratio optimization method 200 for the heavy oil processing device may include step S220: establishing a monitoring model related to the sulfur transfer model to monitor the feed status of the heavy oil processing device in real time.

[0073] The feed ratio optimization system can monitor multiple processing units in the refining process through the monitoring model related to the sulfur transfer model to obtain and record real-time monitoring values ​​related to multiple processing units. Figure 3 As shown, the real-time monitoring value may include the real-time flow rate Q of each side line of the direct supply device part 320 of the atmospheric and vacuum distillation device. rt i and sulfur content Si, the real-time flow rate TQ of each side line of the direct supply tank 311 of the tank area device rt j and sulfur content TSj, and the feed sulfur content defense value MS(k) of the heavy oil processing unit 330. In other embodiments, the real-time monitoring value may also include the real-time flow rate and sulfur content of each feed stream of the heavy oil processing unit 330.

[0074] The feed ratio optimization system can monitor the feed status of each heavy oil processing unit in real time according to the real-time monitoring values ​​of multiple processing units in the refining process obtained by the monitoring model. Through the monitoring model, the feed ratio optimization system realizes real-time monitoring of the feed status of each heavy oil processing unit. Once the total sulfur content of the feed of the heavy oil processing unit is detected to be too high, it can be optimized and adjusted in time to ensure the real-time and flexibility of the production process.

[0075] like Figure 3 As shown, by optimizing and adjusting the feed ratio optimization system, the actual flow rate Q of each side line of the direct supply device part 320 of the atmospheric and vacuum device to the heavy oil processing device 330 can be determined. act i. Actual flow rate TQ of each side line of the direct supply tank 311 of the tank farm device to the heavy oil processing device 330 act j is the optimized feed flow rate. In other embodiments, the optimized feed flow rate may also include the actual flow rate of each feed stream of the heavy oil processing device 330 to the heavy oil processing device 330.

[0076] like Figure 2As shown, the feed ratio optimization method 200 for the heavy oil processing unit may include step S230: in response to the total sulfur content of the feed of the heavy oil processing unit being higher than the feed sulfur content defense value of the heavy oil processing unit, according to the real-time monitoring value of the monitoring model, a linear programming interior point method is used to solve the sulfur transfer optimization model to determine the optimized feed flow of the heavy oil processing unit, and the sulfur transfer optimization model is established according to the optimization objective function and the constraints determined based on the actual process conditions.

[0077] When the monitoring model detects that the total sulfur content of the feed of the heavy oil processing unit is higher than the sulfur content defense value of the feed of the heavy oil processing unit, the feed ratio optimization system can determine the optimized feed flow rate of the heavy oil processing unit according to the established sulfur transfer optimization model.

[0078] The feed ratio optimization system can first determine the constraints based on the actual process conditions, and then establish a sulfur transfer optimization model according to the optimization objective function and the constraints.

[0079] Here, the optimization objective function of the sulfur transfer optimization model is to minimize the difference between the total sulfur content of the feed of the heavy oil processing unit and the sulfur content defense value of the feed of the heavy oil processing unit, so as to reduce the reduction of the total sulfur content of the feed as much as possible. By setting the optimization objective function, the feed ratio optimization system can be more targeted in the optimization process and more in line with production needs. Clear optimization goals make the optimization process more comprehensive and integrated, not only focusing on sulfur content control, but also paying more attention to sulfur content fluctuations in the production process.

[0080] The optimization objective function Z is:

[0081] Z=|MS(k)-∑ i,j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j))|min,

[0082] Among them, Q act i is the actual flow rate of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit, Si is the sulfur content of the i-th side line of the atmospheric and vacuum unit, and the sulfur content of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit is the same as the sulfur content of the i-th side line of the atmospheric and vacuum unit; TQ act j is the actual flow rate of the j-th side line of the direct supply tank of the tank area unit to the heavy oil processing unit, TSj is the sulfur content of the j-th side line of the direct supply tank, the sulfur content of the j-th side line of the direct supply tank to the heavy oil processing unit is the same as the sulfur content of the j-th side line of the direct supply tank; MS(k) is the defense value of the feed sulfur content of the k-th heavy oil processing unit.

[0083] The feed ratio optimization system can accurately adjust the feed flow of the heavy oil processing unit through the set optimization objective function, reduce the sulfur content fluctuation of the heavy oil processing unit, ensure stable production, and maximize the use of high-sulfur raw materials and improve resource utilization efficiency under the premise that the sulfur content meets the requirements.

[0084] The constraints determined based on the actual process conditions may include sulfur balance constraints in the refining process, material balance constraints in the refining process, feed sulfur content protection value constraints, flow constraints, processing volume constraints, and tank capacity constraints. The set constraints comprehensively consider the synergy between multiple processing units, and adapt to the actual production situation through dynamic constraints to ensure that the optimization process can better reflect production needs. In addition, the constraints comprehensively consider the actual process conditions, which can better ensure the feasibility of the optimized feed flow solved, making the optimization process more robust.

[0085] Meeting the sulfur balance constraint in the refining process means maintaining a balanced relationship between the sulfur content of the inlet and outlet materials of the atmospheric and vacuum units, heavy oil processing units, and tank farm units. Introducing sulfur balance as the basis for optimization makes the feed ratio optimization method more in line with the characteristics of the sulfur transfer model, thereby improving the feasibility of sulfur content regulation.

[0086] Specifically, the sulfur balance formula of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit can be:

[0087] Q rt i*Si=Q act *Si+GQi*Si,

[0088] Among them, GQi is the actual flow rate of the i-th side line of the constant pressure reduction device to the temporary storage tank.

[0089] In addition, the sulfur balance formula of the jth side line of the direct supply tank to the heavy oil processing unit can be:

[0090] TSj=TZSj,

[0091] Among them, TZSj is the actual sulfur content in the discharge of the direct supply tank. Based on the sulfur balance constraint, the actual sulfur content TZSj in the discharge of the direct supply tank is equal to the sulfur content TSj of the j-th side line of the direct supply tank to the heavy oil processing unit.

[0092] Meeting the material balance constraint in the oil refining process means that the inlet and outlet flow rates between the atmospheric and vacuum unit, the heavy oil processing unit and the tank farm unit are kept in a balanced relationship. Specifically, the material balance formula of the side line of the atmospheric and vacuum unit to the heavy oil processing unit can be: Q rt i=Q act i+GQi, i.e., the real-time flow rate Q of the side line of the atmospheric and vacuum distillation device rt i must be greater than the actual flow rate Q acti.

[0093] Meeting the feed sulfur content defense value constraint means ensuring that the total feed sulfur content of the heavy oil processing unit does not exceed its tolerance sulfur content. The tolerance sulfur content, i.e., the feed sulfur content defense value constraint, is:

[0094] ZAVG(k)-MS(k)≤0,

[0095] Wherein, ZAVG(k) represents the weighted average of the feed flow rate and the feed sulfur content of the k-th heavy oil processing unit, that is, the total sulfur content of the feed of the k-th heavy oil processing unit. The total sulfur content of the feed of the k-th heavy oil processing unit ZAVG(k) can be specifically:

[0096] ZAVG(k)=∑ i,j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j)),

[0097] Through the determined feed sulfur content defense value constraint, the feed ratio optimization system can ensure that the heavy oil processing unit can handle the sulfur content in the feed to prevent it from exceeding the feed sulfur content defense value, thereby maintaining the stable operation and performance of the heavy oil processing unit. The feed sulfur content defense value constraint can also be applied to the monitoring model of the feed ratio optimization system, so that the feed ratio optimization system can optimize the optimized feed flow of the processing unit when the total sulfur content of the feed of the heavy oil processing unit is monitored to be higher than the feed sulfur content defense value of the heavy oil processing unit.

[0098] Meeting the flow constraint means ensuring that the actual flow to the heavy oil processing unit is within an acceptable range. In some embodiments, the flow constraint may be:

[0099] EXP (expected value) <= Q act i+TQ act j<=Max(maximum value),

[0100] Among them, EXP (expected value) can be the expected value set to prevent the product quantity from decreasing, and Max (maximum value) can be the maximum value set to maximize the material output while meeting the sulfur content requirements, while taking into account equipment capacity, safety, stability, product quality and market demand.

[0101] The processing volume constraint is related to the design conditions of the heavy oil processing unit. When the actual processing volume of the heavy oil processing unit is Pi, the processing volume constraint can be expressed as:

[0102] Pmin≤Pi≤Pmax,

[0103] Among them, Pmin is the minimum processing capacity of the heavy oil processing device, and Pmax is the maximum processing capacity of the heavy oil processing device.

[0104] The tank capacity constraint is related to the capacity limit of the tank in the tank farm. The tank capacity constraint is used to ensure that the material in the tank does not exceed the upper limit of the tank capacity and does not fall below the lower limit of the tank capacity. When the actual capacity of the tank is Ci, the tank capacity constraint can be expressed as:

[0105] Cmin≤Ci≤Cmax,

[0106] Among them, Cmax is the upper limit of the tank capacity, Cmin is the lower limit of the tank capacity, and Ci is the amount of material in the tank, that is, the actual capacity of the tank.

[0107] According to the above optimization objective function and constraint conditions, the feed ratio optimization system can establish a sulfur transfer optimization model. After that, the real-time monitoring value obtained by the monitoring model is input into the sulfur transfer optimization model, and the linear programming interior point method is used to solve the sulfur transfer optimization model to determine the optimized feed flow rate of the heavy oil processing unit. Solving the sulfur transfer optimization model by the linear programming interior point method improves the accuracy and efficiency of sulfur content regulation in the refining process.

[0108] Specifically, when the optimization objective function is in a nonlinear form, the feed ratio optimization system can first convert the nonlinear optimization objective function into a linear form, and then use the linear programming interior point method to solve the optimization objective function to determine the optimized feed flow rate of the heavy oil processing unit.

[0109] Here, the determined optimized feed flow rate of the heavy oil processing unit may include the optimized feed flow rate from each side line of the atmospheric and vacuum unit to the heavy oil processing unit and the optimized feed flow rate from the direct supply tank of the tank farm unit to the heavy oil processing unit.

[0110] The determined optimized feed flow rate can be used for on-site operation guidance, thus effectively solving the problem of excessive feed sulfur content caused by raw material changes. This allows the heavy oil processing unit to more accurately adjust the feed flow rate without exceeding the sulfur content tolerance to ensure that the sulfur content does not exceed the standard, and reduce the sulfur content fluctuation during the production process, making production more stable.

[0111] The following are three specific non-limiting preferred embodiments, based on which the feed ratio optimization system for a heavy oil processing device and the feed ratio optimization method for a heavy oil processing device proposed in the present invention are further described.

[0112] In the first embodiment, the feed ratio optimization system can optimize the feed flow rate of a heavy oil processing unit whose sulfur content exceeds the tolerance range.

[0113] Please refer to Figure 4 , Figure 4 A schematic diagram of a process model related to wax oil provided according to some embodiments of the present invention is shown.

[0114] like Figure 4 As shown, the heavy oil processing unit can be a 1# catalytic unit 411, and the processing device for the feed stream of the 1# catalytic unit 411 can be the normal four lines 421 of the 1# normal and low pressure reduction unit 420, the catalytic low-sulfur residual oil tank 430, the tank supply (DAO) 441, the 1# cracked refined wax oil 450, the tank supply (residue wax) / direct supply 442, and the tank supply (mixed wax oil) 443.

[0115] First, the feed ratio optimization system can obtain the data related to the actual flow and sulfur content of the 1# catalytic unit 411 in the heavy oil processing unit during the operation of the refinery through the monitoring model. The real-time flow and sulfur content of the processing unit corresponding to each feed stream of the 1# catalytic unit 411 are shown in Table 1:

[0116]

[0117]

[0118] Table 1

[0119] The real-time flow rate of the normal fourth line 421 of the 1# normal and vacuum unit 420 in the feed stream is 10.58 t / h, and the sulfur content is 2%; the real-time flow rate of the catalytic low-sulfur residue oil tank 430 in the feed stream is 18.54 t / h, and the sulfur content is 2%; the real-time flow rate of the tank supply (DAO) 441 in the feed stream is 40.15 t / h, and the sulfur content is 1%; the real-time flow rate of the 1# cracked refined wax oil 450 in the feed stream is 90.62 t / h, and the sulfur content is 0.27%; the real-time flow rate of the tank supply (residue wax) / direct supply 442 in the feed stream is 20 t / h, and the sulfur content is 0.47%; the real-time flow rate of the tank supply (mixed wax oil) 443 in the feed stream is 19.74 t / h, and the sulfur content is 0.5%.

[0120] The feed ratio optimization system can determine the total feed sulfur content ZAVG of the 1# catalytic device 411 according to the real-time monitored feed state, that is, the real-time flow rate and sulfur content of each feed stream of the 1# catalytic device 411. By formula:

[0121] ZAVG(k)=∑ i,j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j)),

[0122] The current total sulfur content ZAVG of the feed to the 1# catalytic unit 411 can be determined:

[0123] ZAVG=(10.58*2+18.54*2+40.15*1+90.62*0.27+20*0.47+19.74*0.5) / (10.5+18.54+40.15+90.62+20+19.74)=0.71.

[0124] When the feed sulfur content defense value MS of the 1# catalytic device 411 is 0.65, the feed total sulfur content ZAVG of the 1# catalytic device 411 is higher than the feed sulfur content defense value MS. Therefore, the feed ratio optimization system can optimize the feed flow rate according to the sulfur transfer optimization model.

[0125] In order to prevent the sulfur content from changing greatly during the refining process, the feed ratio optimization system can choose the optimization objective function Z = |MS(k)-∑ i,j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j))|min.

[0126] To simplify the algorithm, the feed ratio optimization system can simplify the nonlinear programming problem into a linear programming problem. Specifically, the feed ratio optimization system can transform the optimization objective function Z from a nonlinear form to a linear form through appropriate approximation and transformation. This transformation can greatly simplify the solution process while maintaining the effectiveness of the optimization objective function.

[0127] Specifically, the linear programming method can be used to directly minimize the objective function Z, that is: Z = |MS(k)*∑ i,j (Q act i+TQ act j)-∑ i,j (Q act i*Si+TQ act j*TSj)|min.

[0128] Afterwards, the feed ratio optimization system can add constraints according to the actual production process. In the first embodiment, the constraints may include sulfur balance constraints in the oil refining process, material balance constraints in the oil refining process, feed sulfur content defense value constraints, flow constraints, processing volume constraints, and tank capacity constraints.

[0129] The sulfur balance constraints in the oil refining process include the sulfur balance of the side line of the atmospheric and vacuum unit to the heavy oil processing unit and the sulfur balance of the side line of the direct supply tank to the heavy oil processing unit. The sulfur balance formula of the side line of the atmospheric and vacuum unit to the heavy oil processing unit can be:

[0130] Q rt i*Si=Q act*Si+GQi*Si,

[0131] The sulfur balance formula for the side line of the direct supply tank to the heavy oil processing unit can be:

[0132] TSj=TZSj.

[0133] The material balance constraint in the refining process can be: Q rt i=Q act i+GQi.

[0134] The feed sulfur content defense value constraint can be ZAVG(k)-MS(k)≤0.

[0135] The flow constraint ensures that the actual flow to the heavy oil processing unit is within an acceptable range and can be:

[0136] EXP (expected value) <= Q act i+TQ act j<=Max (maximum value).

[0137] The processing volume constraint can be expressed as: Pmin≤Pi≤Pmax, and the tank capacity constraint can be expressed as: Cmin≤Ci≤Cmax.

[0138] Based on the constraints and the optimization objective function, the sulfur transfer optimization model is determined. According to the real-time monitoring value, the linear programming interior point method is used to solve the optimized feed flow of each feed stream, thereby minimizing the change in the operating sulfur content and adjusting the feed flow to achieve sulfur content control. The results of the optimized feed flow of each feed stream determined by the sulfur transfer optimization model are shown in Table 2:

[0139]

[0140]

[0141] Table 2

[0142] As shown in Table 2, through the sulfur transfer optimization model, the feed ratio optimization system can determine that the real-time flow rate of the four-line 421 of the 1# atmospheric and vacuum unit 420 is 10.58 t / h, and the sulfur content is 2%. After optimization, the actual flow rate of the four-line 421 of the 1# atmospheric and vacuum unit 420 to the 1# catalytic unit 411 is 5.43 t / h; the real-time flow rate of the catalytic low-sulfur residual oil tank 430 is 18.54 t / h, and the sulfur content is 2%. After optimization, the actual flow rate of the catalytic low-sulfur residual oil tank 430 to the 1# catalytic unit 411 is 10.89 t / h; the real-time flow rate of the tank supply (DAO) 441 is 100 t / h, and the sulfur content is 1%. After optimization, the actual flow rate of the tank supply (DAO) 441 to the 1# catalytic unit 411 is 10. The actual flow rate is 82.01t / h; the real-time flow rate of 1# cracked refined wax oil 450 is 90.62t / h, and the sulfur content is 0.27%. After optimization, the actual flow rate of 1# cracked refined wax oil 450 to 1# catalytic device 411 is 106.20t / h; the real-time flow rate of tank supply (residue wax) / direct supply 442 is 20t / h, and the sulfur content is 0.47%. After optimization, the actual flow rate of tank supply (residue wax) / direct supply 442 to 1# catalytic device 411 is 31.95t / h; the real-time flow rate of tank supply (mixed wax oil) 443 is 19.74t / h, and the sulfur content is 0.5%. After optimization, the actual flow rate of tank supply (mixed wax oil) 443 to 1# catalytic device 411 is 30.95t / h. By adjusting the feed flow rate according to the optimized feed flow rate, the value of the optimized total feed sulfur content ZAVG of the 1# catalytic device 411 is adjusted from 0.71 to 0.6499. After the adjustment, when the feed sulfur content defense value MS of the 1# catalytic device 411 is 0.65, the total feed sulfur content ZAVG of the 1# catalytic device 411 is less than the feed sulfur content defense value MS.

[0143] Please refer to Figure 5 , Figure 5 A comparative effect diagram of sulfur content control provided according to Example 1 of the present invention is shown.

[0144] like Figure 5 As shown, the actual flow rate of each feed stream to the 1# catalytic unit 411 is adjusted less than the real-time flow rate of each feed stream before optimization, so the feed impact on other heavy oil processing units can be ignored. The total sulfur content ZAVG of each feed stream before optimization is higher than the total sulfur content ZAVG of each feed stream after optimization, and the total sulfur content ZAVG of each feed stream after optimization is less than the feed sulfur content defense value MS of the 1# catalytic unit 411.

[0145] Embodiment 2 Based on Embodiment 1, the feed amount of other heavy oil processing devices is further optimized.

[0146] In the second embodiment, the sulfur content of the 2# catalytic device 412 is considered in particular.

[0147] like Figure 4 As shown, the processing device for the feed stream of the 2# catalytic unit 412 can be a catalytic low-sulfur residual oil tank 430, a G931 tank 461, a 1# cracked refined wax oil 450, a 1# residual oil hydrogenated wax oil 470, a tank supply (DAO) 441, a 5# hydrogenated refined wax oil 480, and G517 and G518 of tank supplies 444 of G515 to G518.

[0148] The feed ratio optimization system can obtain data related to the actual flow and sulfur content of the 2# catalytic device 412 in the heavy oil processing unit during the operation of the refinery through the monitoring model. The real-time flow and sulfur content of the processing unit corresponding to each feed stream of the 2# catalytic device 412 are shown in Table 3:

[0149] Feed stream Real-time flow (t / h) Sulfur content (%) 430 9.62 0.5 461 67.85 0.5 450 4 0.27 470 62.23 0.47 441 30 1.01 480 202.84 0.13 G517 / G518 10 0.5 ZAVG 0.34 MS 0.3

[0150] Table 3

[0151] The real-time flow rate of the catalytic low-sulfur residue tank 430 in the feed stream is 9.62 t / h, and the sulfur content is 0.5%; the real-time flow rate of the G931 tank 461 in the feed stream is 67.85 t / h, and the sulfur content is 0.5%; the real-time flow rate of the 1# cracked refined wax oil 450 in the feed stream is 4 t / h, and the sulfur content is 0.27%; the real-time flow rate of the 1# residual oil hydrogenated wax oil 470 in the feed stream is 62.23 t / h , the sulfur content is 0.47%; the real-time flow rate of tank supply (DAO) 441 in the feed stream is 30 t / h, and the sulfur content is 1.01%; the real-time flow rate of 5# hydrorefined wax oil 480 in the feed stream is 202.84 t / h, and the sulfur content is 0.13%; the real-time flow rate of G517 and G518 of tank supply 444 from G515 to G518 in the feed stream is 10 t / h, and the sulfur content is 0.5%.

[0152] The feed ratio optimization system can determine that the total sulfur content ZAVG of the feed of the 2# catalytic device 412 is 0.34 according to the real-time monitored feed state. When the feed sulfur content defense value MS of the 2# catalytic device 412 is 0.3, the total sulfur content ZAVG of the feed of the 2# catalytic device 412 is higher than the feed sulfur content defense value MS. Therefore, the feed ratio optimization system can optimize the feed flow rate according to the sulfur transfer optimization model.

[0153] In Example 2, since there is no atmospheric and vacuum device in the processing device for the feed stream, the optimization objective function can be selected as:

[0154] Z=|MS(k)-∑ j (TQ actj*TSj) / TQ act j)|min.

[0155] To simplify the algorithm, the feed ratio optimization system can simplify the nonlinear programming problem into a linear programming problem. Specifically, the feed ratio optimization system can transform the optimization objective function Z from a nonlinear form to a linear form through appropriate approximation and transformation. Specifically, the linear programming method can be used to directly minimize the objective function Z, that is: Z = |MS(k)*TQ act j-∑ j (TQ act j*TSj)|min.

[0156] Afterwards, the feed ratio optimization system can add constraints according to the actual production process. In the second embodiment, the constraints can include sulfur balance constraints in the refining process, material balance constraints in the refining process, feed sulfur content defense value constraints, flow constraints, processing volume constraints, and tank capacity constraints.

[0157] Since there is no atmospheric and vacuum unit in the processing unit for the feed stream, the sulfur balance constraint in the refining process can be the sulfur balance of the side line of the direct supply tank to the heavy oil processing unit. The sulfur balance formula of the side line of the direct supply tank to the heavy oil processing unit can be: TSj = TZSj.

[0158] In the second embodiment, the material balance constraint in the oil refining process can be used to ensure that the inlet and outlet flow rates between the heavy oil processing unit and the tank farm remain in a balanced relationship.

[0159] The feed sulfur content defense value constraint can be ZAVG(k)-MS(k)≤0.

[0160] The flow constraint ensures that the actual flow to the heavy oil processing unit is within an acceptable range and can be:

[0161] EXP (expected value) <= TQ act j<=Max (maximum value).

[0162] The processing volume constraint can be expressed as: Pmin≤Pi≤Pmax.

[0163] The tank capacity constraint can be expressed as: Cmin≤Ci≤Cmax. Furthermore, since the 1# catalytic device 411 and the 2# catalytic device 412 can share a feed and be stored in the same tank, after optimizing the 1# catalytic device 411, the tank capacity of the 2# catalytic device 412 can be adjusted and constrained. That is, in the second embodiment, the following constraints can be added to the tank capacity constraints:

[0164] Cmin_2≤Ci_2≤Cmax_2,

[0165] Among them, Ci_2 can refer to the amount of material in the tank, Ci_2 = Ci + TQ act j; Cmin_2 and Cmax_2 are the lower and upper limits of the capacity of the tank of the 2# catalytic device 412, respectively. Cmin_2 and Cmax_2 can be set according to actual conditions.

[0166] The addition of this tank capacity constraint can ensure that the tank capacity of the direct supply tank for the 2# catalytic unit 412 not only meets its own capacity limitation, but also takes into account the impact of the optimization result of the 1# catalytic unit 411 on the direct supply tank, thereby further ensuring the material balance and sulfur content control of the entire refining system.

[0167] Based on the constraints and the optimization objective function, the sulfur transfer optimization model is determined. According to the real-time monitoring value, the optimized feed flow rate of each feed stream is solved by the linear programming interior point method. The optimized feed flow rate of each feed stream determined by the sulfur transfer optimization model is shown in Table 4:

[0168] Feed stream Real-time flow (t / h) Sulfur content (%) Actual flow rate (t / h) 430 9.62 0.5 15.21 461 67.85 0.5 64.78 450 4 0.27 12.32 470 62.23 0.47 60.31 441 30 1.01 14.79 480 202.84 0.13 205.37 G517 / G518 10 0.5 14.70 ZAVG 0.34 0.3 MS 0.3

[0169] Table 4

[0170] As shown in Table 4, through the sulfur transfer optimization model, the feed ratio optimization system can determine that the real-time flow rate of the catalytic low-sulfur residue oil tank 430 is 9.62 t / h, and the sulfur content is 0.5%. After optimization, the actual flow rate of the catalytic low-sulfur residue oil tank 430 to the 2# catalytic unit 412 is 15.21 t / h; the real-time flow rate of the G931 tank 461 is 67.85 t / h, and the sulfur content is 0.5%. After optimization, the actual flow rate of the G931 tank 461 to the 2# catalytic unit 412 is 64.78 t / h; the real-time flow rate of the 1# cracked refined wax oil 450 is 4 t / h, and the sulfur content is 0.27%. After optimization, the actual flow rate of the 1# cracked refined wax oil 450 to the 2# catalytic unit 412 is 12.32 t / h; the real-time flow rate of the 1# residue oil hydrogenated wax oil 470 is 62.23 t / h, and the sulfur content is 0.47%. After optimization, the real-time flow rate of the 1# residue oil hydrogenated wax oil 470 is 62.23 t / h, and the sulfur content is 0.47%. The actual flow rate of hydrogenated wax oil 470 to 2# catalytic unit 412 is 60.31t / h; the real-time flow rate of tank supply (DAO) 441 is 30t / h, and the sulfur content is 1.01%. After optimization, the actual flow rate of tank supply (DAO) 441 to 2# catalytic unit 412 is 14.79t / h; the real-time flow rate of 5# hydrorefined wax oil 480 is 202.84t / h, and the sulfur content is 0.13%. After optimization, , the actual flow rate of 5# hydrorefined wax oil 480 to 2# catalytic unit 412 is 205.37t / h; the real-time flow rate of G517 and G518 supplied by tanks G515 to G518 for 444 is 10t / h, and the sulfur content is 0.5%. After optimization, the actual flow rate of G517 and G518 supplied by tanks G515 to G518 for 444 to 2# catalytic unit 412 is 14.70t / h.

[0171] The value of the optimized total sulfur content ZAVG of the feed of the 2# catalytic device 412 is adjusted from 0.34 to 0.3. After the adjustment, when the defense value MS of the feed sulfur content of the 2# catalytic device 412 is 0.3, the total sulfur content ZAVG of the feed of the 2# catalytic device 412 is equal to the defense value MS of the feed sulfur content.

[0172] Please refer to Figure 6 , Figure 6 A comparative effect diagram of sulfur content control provided according to Example 2 of the present invention is shown.

[0173] like Figure 6 As shown, the actual flow rate of each feed stream to the 2# catalytic device 412 is adjusted less than the real-time flow rate of each feed stream before optimization. The total sulfur content ZAVG of each feed stream before optimization is higher than the total sulfur content ZAVG of each feed stream after optimization, and the total sulfur content ZAVG of each feed stream after optimization is equal to the feed sulfur content defense value MS of the 2# catalytic device 412.

[0174] Example 3 Based on Example 2, the heavy oil processing unit related to residual oil is mainly considered, and the sulfur content of the heavy oil processing unit related to residual oil is effectively controlled by optimizing the feed amount of the heavy oil processing unit related to residual oil.

[0175] Please refer to Figure 7 , Figure 7 A schematic diagram of a process model related to residual oil provided in accordance with the third embodiment of the present invention is shown.

[0176] like Figure 4 , Figure 7 As shown, the heavy oil processing unit can be a 1# residue oil hydrogenation unit 470, and the processing unit for the feed stream of the 1# residue oil hydrogenation unit 470 can be a G932 tank supply 462, a 2# catalytic cycle oil 471, a residue feeding tank 490, a residue oil line 711 of a 3# atmospheric and vacuum unit 710, a washing oil line 712 of a 3# atmospheric and vacuum unit 710, and a purified oil slurry 472.

[0177] The feed ratio optimization system can obtain the actual flow and sulfur content related data to the 1# residue oil hydrotreating unit 470 in the heavy oil processing unit during the operation of the refinery through the monitoring model. The real-time flow and sulfur content of the processing unit corresponding to each feed stream of the 1# residue oil hydrotreating unit 470 are shown in Table 5:

[0178]

[0179]

[0180] Table 5

[0181] The real-time flow rate of G932 tank supply 462 in the feed stream is 5.4 t / h, and the sulfur content is 1%; the real-time flow rate of 2# catalytic circulating oil 471 in the feed stream is 13.19 t / h, and the sulfur content is 1%; the real-time flow rate of slag adding tank 490 in the feed stream is 103.4 t / h, and the sulfur content is 9.23%; the real-time flow rate of residue oil line 711 of 3# atmospheric and vacuum unit 710 in the feed stream is 161.54 t / h, and the sulfur content is 5.28%; the real-time flow rate of washing oil line 712 of 3# atmospheric and vacuum unit 710 in the feed stream is 44.74 t / h, and the sulfur content is 3.96%; the real-time flow rate of purified oil slurry 472 in the feed stream is 10.23 t / h, and the sulfur content is 1.32%.

[0182] The feed ratio optimization system can determine that the total sulfur content ZAVG of the feed of the 1# residue oil hydrotreating unit 470 is 5.96 according to the real-time monitored feed status. When the feed sulfur content defense value MS of the 1# residue oil hydrotreating unit 470 is 5.5, the total sulfur content ZAVG of the feed of the 1# residue oil hydrotreating unit 470 is higher than the feed sulfur content defense value MS. Therefore, the feed ratio optimization system can gradually optimize the feed flow rate according to the sulfur transfer optimization model. The goal of the sulfur transfer optimization model is to minimize the change in the total sulfur content of the feed of the heavy oil processing unit, and at the same time adjust the feed flow rate of the heavy oil processing unit related to wax oil to achieve effective control of the sulfur content.

[0183] According to the actual production process, the feed ratio optimization system can add constraints to ensure that the stability and sulfur content of the oil refining system meet the requirements. In the third embodiment, the constraints can include sulfur balance constraints in the oil refining process, material balance constraints in the oil refining process, feed sulfur content defense value constraints, flow constraints, processing volume constraints, and tank capacity constraints.

[0184] Based on the constraints and the optimization objective function, the sulfur transfer optimization model is determined. According to the real-time monitoring value, the optimized feed flow rate of each feed stream is solved by the linear programming interior point method. The optimized feed flow rate of each feed stream determined by the sulfur transfer optimization model is shown in Table 6:

[0185]

[0186]

[0187] Table 6

[0188] As shown in Table 6, through the sulfur transfer optimization model, the feed ratio optimization system can determine that the real-time flow rate of G932 tank supply 462 is 5.4 t / h, and the sulfur content is 1%. After optimization, the actual flow rate of G932 tank supply 462 to 1# residue oil hydrogenation unit 470 is 17.39 t / h; the real-time flow rate of 2# catalytic cycle oil 471 is 13.19 t / h, and the sulfur content is 1%. After optimization, the actual flow rate of 2# catalytic cycle oil 471 to 1# residue oil hydrogenation unit 470 is 24.21 t / h; the real-time flow rate of slag feeding tank 490 is 103.4 t / h, and the sulfur content is 9.23%. After optimization, the actual flow rate of slag feeding tank 490 to 1# residue oil hydrogenation unit 470 is 94.98 t / h; 3# atmospheric and vacuum unit The real-time flow rate of the residue oil line 711 of 710 is 161.54 t / h, and the sulfur content is 5.28%. After optimization, the actual flow rate of the residue oil line 711 of the 3# atmospheric and vacuum unit 710 to the 1# residue oil hydrogenation unit 470 is 148.50 t / h; the real-time flow rate of the washing oil line 712 of the 3# atmospheric and vacuum unit 710 is 44.74 t / h, and the sulfur content is 3.96%. After optimization, the actual flow rate of the washing oil line 712 of the 3# atmospheric and vacuum unit 710 to the 1# residue oil hydrogenation unit 470 is 29.74 t / h; the real-time flow rate of the purified oil slurry 472 is 10.23 t / h, and the sulfur content is 1.32%. After optimization, the actual flow rate of the purified oil slurry 472 to the 1# residue oil hydrogenation unit 470 is 21.21 t / h.

[0189] The value of the optimized total sulfur content ZAVG of the feed of the 1# residue oil hydrotreating unit 470 is adjusted from 5.96 to 5.499. After the adjustment, when the feed sulfur content defense value MS of the 1# residue oil hydrotreating unit 470 is 5.5, the total sulfur content ZAVG of the feed of the 1# residue oil hydrotreating unit 470 is less than the feed sulfur content defense value MS.

[0190] In summary, according to the feed ratio optimization method for a heavy oil processing device provided by the present invention, when the total sulfur content of the feed of the heavy oil processing device exceeds the standard due to changes in the raw materials, by adjusting the ratio of the actual feed flow rates of different feed streams, the high-sulfur raw materials can be utilized to the maximum extent under the premise of meeting the sulfur content limit requirement. In addition, the feed ratio optimization method for a heavy oil processing device provided by the present invention is simple and convenient to calculate, and has strong practicality. It is suitable for guiding the setting of the feed amount operating parameters of the heavy oil processing device in the oil refining process, and can effectively adjust and control the total sulfur content of the feed of the heavy oil processing device within a reasonable range.

[0191] Although the above methods are illustrated and described as a series of actions for simplicity of explanation, it should be understood and appreciated that these methods are not limited by the order of the actions, because according to one or more embodiments, some actions may occur in a different order and / or concurrently with other actions from those illustrated and described herein or not illustrated and described herein but understandable to those skilled in the art.

[0192] Those skilled in the art will appreciate that information, signals, and data may be represented using any of a variety of different technologies and techniques. For example, data, instructions, commands, information, signals, bits, symbols, and chips cited throughout the above description may be represented by voltage, current, electromagnetic waves, magnetic fields or magnetic particles, optical fields or optical particles, or any combination thereof.

[0193] Those skilled in the art will further appreciate that the various illustrative logic blocks, modules, circuits, and algorithm steps described in conjunction with the embodiments disclosed herein may be implemented as electronic hardware, computer software, or a combination of the two. To clearly illustrate this interchangeability of hardware and software, various illustrative components, blocks, modules, circuits, and steps are generally described above in terms of their functionality. Whether such functionality is implemented as hardware or software depends on the specific application and the design constraints imposed on the overall system. The technician may implement the described functionality in different ways for each specific application, but such implementation decisions should not be interpreted as resulting in a departure from the scope of the present invention.

[0194] The various illustrative logic modules and circuits described in conjunction with the embodiments disclosed herein may be implemented or executed with a general purpose processor, a digital signal processor (DSP), an application specific integrated circuit (ASIC), a field programmable gate array (FPGA) or other programmable logic device, discrete gate or transistor logic, discrete hardware components, or any combination thereof designed to perform the functions described herein. A general purpose processor may be a microprocessor, but in the alternative, the processor may be any conventional processor, controller, microcontroller, or state machine. The processor may also be implemented as a combination of computing devices, such as a combination of a DSP and a microprocessor, a plurality of microprocessors, one or more microprocessors in cooperation with a DSP core, or any other such configuration.

[0195] The steps of the method or algorithm described in conjunction with the embodiments disclosed herein may be embodied directly in hardware, in a software module executed by a processor, or in a combination of the two. The software module may reside in a RAM memory, a flash memory, a ROM memory, an EPROM memory, an EEPROM memory, a register, a hard disk, a removable disk, a CD-ROM, or any other form of storage medium known in the art. An exemplary storage medium is coupled to a processor so that the processor can read and write information from / to the storage medium. In an alternative, a storage medium may be integrated into a processor. The processor and the storage medium may reside in an ASIC. The ASIC may reside in a user terminal. In an alternative, the processor and the storage medium may reside in a user terminal as discrete components.

[0196] In one or more exemplary embodiments, the functions described may be implemented in hardware, software, firmware, or any combination thereof. If implemented as a computer program product in software, each function may be stored on or transmitted by a computer-readable medium as one or more instructions or codes. Computer-readable media include both computer storage media and communication media, including any medium that facilitates the transfer of a computer program from one place to another. Storage media may be any available medium that can be accessed by a computer. As an example and not limitation, such a computer-readable medium may include RAM, ROM, EEPROM, CD-ROM or other optical disk storage, disk storage or other magnetic storage device, or any other medium that can be used to carry or store the desired program code in the form of an instruction or data structure and can be accessed by a computer. Any connection is also properly referred to as a computer-readable medium. For example, if the software is transmitted from a website, a server, or other remote source using a coaxial cable, a fiber optic cable, a twisted pair, a digital subscriber line (DSL), or wireless technologies such as infrared, radio, and microwaves, the coaxial cable, fiber optic cable, twisted pair, DSL, or wireless technologies such as infrared, radio, and microwaves are included in the definition of the medium. Disk and disc as used herein include compact disc (CD), laser disc, optical disc, digital versatile disc (DVD), floppy disk and Blu-ray disc, wherein disk often reproduces data magnetically, while disc reproduces data optically with lasers. Combinations of the above should also be included within the scope of computer-readable media.

[0197] The previous description of the disclosure is provided to enable any person skilled in the art to make or use the disclosure. Various modifications to the disclosure will be apparent to those skilled in the art, and the general principles defined herein may be applied to other variations without departing from the spirit or scope of the disclosure. Thus, the disclosure is not intended to be limited to the examples and designs described herein, but should be granted the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A feed ratio optimization method for a heavy oil processing device, characterized in that: Includes steps: Determining a sulfur transfer model based on a linear model of a plurality of processing units, the plurality of processing units including a vacuum unit, a heavy oil processing unit, and a tank farm unit; Establishing a monitoring model related to the sulfur transfer model to monitor the feed status of the heavy oil processing unit in real time; In response to the total sulfur content of the feed of the heavy oil processing unit being higher than the defense value of the feed sulfur content of the heavy oil processing unit, according to the real-time monitoring value of the monitoring model, the linear programming interior point method is used to solve the sulfur transfer optimization model to determine the optimized feed flow rate of the heavy oil processing unit. The sulfur transfer optimization model is established according to the optimization objective function and the constraints determined based on the actual process conditions.

2. The feed ratio optimization method according to claim 1, characterized in that: The optimization objective function is to minimize the difference between the total sulfur content of the feed of the heavy oil processing unit and the sulfur content defense value of the feed of the heavy oil processing unit.

3. The feed ratio optimization method according to claim 2, characterized in that: The optimization objective function Z is: Z=|MS(k)-∑ i，j ((Q act i*Si+TQ act j*TSj) / (Q act i+TQ act j))|min, Among them, Q act i is the actual flow rate of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit, Si is the sulfur content of the i-th side line of the atmospheric and vacuum unit to the heavy oil processing unit, TQ act j is the actual flow rate of the j-th side line of the direct supply tank of the tank area device to the heavy oil processing device, TSj is the sulfur content of the j-th side line of the direct supply tank to the heavy oil processing device, and MS(k) is the defense value of the feed sulfur content of the k-th heavy oil processing device.

4. The feed ratio optimization method according to claim 1, characterized in that: The step of solving the sulfur transfer optimization model using a linear programming interior point method according to the real-time monitoring value of the monitoring model to determine the optimized feed flow rate of the heavy oil processing unit comprises: In response to the optimization objective function being in a nonlinear form, converting the optimization objective function into a linear form; and The optimization objective function is solved by a linear programming interior point method to determine the optimized feed flow rate of the heavy oil processing unit.

5. The feed ratio optimization method according to claim 1, characterized in that: The heavy oil processing device includes a delayed coking device, a hydrocracking device, a catalytic cracking device, and a residual oil hydrogenation device, and the tank area device includes a direct supply tank and a temporary storage tank.

6. The feed ratio optimization method according to claim 1, characterized in that: The constraints include sulfur balance constraints in the oil refining process, material balance constraints in the oil refining process, feed sulfur content defense value constraints, flow constraints, processing volume constraints, and tank capacity constraints.

7. The feed ratio optimization method according to claim 1, characterized in that: The real-time monitoring values ​​of the monitoring model include the real-time flow and sulfur content of each side line of the atmospheric and vacuum device, the real-time flow and sulfur content of each side line of the direct supply tank of the tank area device, and the defense value of the feed sulfur content of the heavy oil processing device.

8. The feed ratio optimization method according to claim 1, characterized in that: Determining the optimized feed flow rate of the heavy oil processing device includes determining the optimized feed flow rate of each side line of the atmospheric and vacuum device to the heavy oil processing device and the optimized feed flow rate of the direct supply tank of the tank area device to the heavy oil processing device.

9. A feed ratio optimization system for a heavy oil processing device, characterized in that: include: a memory having computer instructions stored thereon; as well as A processor is connected to the memory and is configured to execute computer instructions stored in the memory to implement the feed ratio optimization method for a heavy oil processing device according to any one of claims 1 to 8.

10. A computer-readable storage medium having computer instructions stored thereon, characterized in that: When the computer instructions are executed by the processor, the feed ratio optimization method for a heavy oil processing device according to any one of claims 1 to 8 is implemented.

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