A control method and device for organic phase circulation in spent fuel reprocessing

Abstract

The present application belongs to the technical field of spent fuel post-processing, and specifically relates to a control method and device for the organic phase circulation of spent fuel post-processing. The method includes: obtaining the organic phase supply and demand relationship between various systems in the post-processing process; based on the organic phase supply and demand relationship, obtaining the organic phase flow rate and organic phase usage of each extraction supply and demand; based on the total volume of the input and output organic phase of each extraction process being equal, and the total conservation relationship of TBP and KE, determining the input and output calculation formula of each organic phase between each extraction process and the contaminated solvent distillation process; according to the input and output calculation formula, controlling the organic phase flow rate between various systems in the post-processing process. The present application can be directly used for spent fuel post-processing commissioning and production operations, realizing the quantitative replacement of organic phase in the extraction process and the inventory monitoring of the process system, and ensuring the continuous and stable operation of the process system under the organic phase circulation system.

Description

Technical Field

[0001] The present application belongs to the technical field of spent fuel post-processing, and in particular relates to a control method and device for organic phase circulation in spent fuel post-processing. Background Art

[0002] In the field of spent fuel reprocessing, the aqueous tributyl phosphate (TBP) extraction process is commonly used. This process usually uses 30% TBP-kerosene (TK30) and the aqueous phase containing uranium and plutonium fragments to enter the extraction equipment in a certain proportion to extract and purify uranium and plutonium elements. The large-scale use of organic phase in the reprocessing process increases the cost of operation and treatment and disposal of radioactive organic waste liquid.

[0003] In response to the above problems, a post-processing plant designed and added a dirty solvent distillation process, and carried out two-stage vacuum distillation treatment on the used waste organic phase to obtain kerosene (KE) fraction, 80% TBP-KE (TK80) fraction, low-boiling point kerosene fraction and distillation residue. After alkali washing and acidification, the 80% TBP-KE fraction is returned to the extraction process as an extractant for reuse, the kerosene fraction is returned to the oil removal equipment for reuse, the low-boiling point kerosene fraction is sent to the combustible waste incineration process for incineration treatment, and the distillation residue is sent to the distillation residue pyrolysis incineration process for pyrolysis treatment. However, it is easy for material accumulation to occur when 80% TBP-KE and KE are returned to the system for reuse after distillation and regeneration. Summary of the invention

[0004] The purpose of the present application is to provide a control method and device for the organic phase circulation of spent fuel reprocessing, so as to solve the problem of easy accumulation of materials when 80% TBP-KE and KE are returned to the system for reuse after distillation and regeneration in the prior art, realize quantitative replacement of organic phase in the extraction process and inventory monitoring of the process system, and ensure continuous and stable operation of the process system under the organic phase circulation system.

[0005] Technical solution to achieve the purpose of this application:

[0006] A first aspect of an embodiment of the present application provides a control method for organic phase circulation in spent fuel reprocessing, the method comprising:

[0007] Obtain the organic phase supply and demand relationship between various systems in the post-processing process;

[0008] Based on the organic phase supply and demand relationship, obtaining the organic phase flow rate and organic phase usage of each extraction supply and demand;

[0009] Based on the equal total volume of the input and output organic phases of each extraction process and the conservation relationship between the total amount of TBP and KE, the calculation formulas for the input and output volume of each organic phase between each extraction process and the contaminated solvent distillation process are determined;

[0010] According to the input-output calculation formula, the organic phase flow rate between various systems in the post-processing process is controlled.

[0011] Optionally, the total volume of the input and output organic phases in each extraction step is equal, and the total amount of TBP and KE is conserved, specifically including:

[0012] The total volume of the input and output organic phases in the co-decontamination and plutonium purification extraction steps is equal;

[0013] The total volume of the input and output organic phases in the uranium purification and extraction process is equal;

[0014] The output TK30 from the uranium purification and extraction process is sent to co-decontamination and plutonium purification;

[0015] The total amount of TBP in the co-decontamination and plutonium purification extraction process is conserved;

[0016] The total amount of TBP in the uranium purification and extraction process is conserved;

[0017] The total amount of KE in the co-decontamination and plutonium purification process is conserved;

[0018] Also, the total amount of uranium purification KE process is conserved.

[0019] Optionally, the input and output calculation formula specifically includes:

[0020] The input amount of 80% TBP-kerosene in the co-decontamination and plutonium purification extraction process is 0.51c-0.09fm 3 / d, 30% TBP-kerosene input is 1.6f+gm 3 / d, the output of 30% TBP-kerosene is 1.51c+1.51f+gm 3 / d, the input amount of kerosene is cm 3 / d, the replacement ratio of 30% TBP-kerosene is (1.51c-0.09f) / ∑0.024X i m 3 / d, the replacement ratio of kerosene is c / ∑0.024Y i m 3 / d;

[0021] In the uranium purification and extraction process, the input amount of 80% TBP-kerosene is 0.6fm 3 / d, 30% TBP-kerosene output is 1.6fm 3 / d, the input amount of kerosene is fm 3 / d, the replacement ratio of 30% TBP-kerosene is 1.6f / ∑0.024Z i m 3 / d, the replacement ratio of kerosene is f / ∑0.024P i m3 / d;

[0022] In the dirty solvent distillation process, the output of 80% TBP-kerosene is 0.51 (c+f) m 3 / d, 30% TBP-kerosene input is 1.51c+1.51f+gm 3 / d, the output of 30% TBP-kerosene is nm 3 / d, the output of kerosene is c+fm 3 / d;

[0023] Wherein, c is the kerosene input amount of the co-decontamination and plutonium purification and extraction process, f is the kerosene input amount of the uranium purification and extraction process, g is the daily usage of fresh 30% TBP-kerosene in the 2BS column, n is the residual liquid output of the contaminated solvent distillation process, and X i The 30% TBP-kerosene operating flow rate of each extraction equipment in the co-decontamination and plutonium purification extraction process, Y i is the kerosene flow rate of each deoiling equipment in the co-decontamination and plutonium purification and extraction process, Z i The 30% TBP-kerosene operating flow rate of each extraction equipment in the uranium purification and extraction process, P i It is the kerosene operating flow rate of each deoiling equipment in the uranium purification process.

[0024] Optionally, the method further includes:

[0025] The consumption of the organic phase was obtained based on the operating days of each system and the organic phase storage tank data.

[0026] Optionally, the method of obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data specifically includes:

[0027] The net daily consumption of TBP is (X TK30 +m)×30%+n

[0028] KE daily net consumption = X KE +70%g

[0029] Among them, X TK30 is the daily loss of 30% TBP-kerosene in the organic phase storage tank, X KE It is the daily loss of kerosene in the organic phase storage tank.

[0030] Optionally, the step of obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data further includes:

[0031] The annual net consumption of TBP is calculated according to the formula [(X TK30 +g)×30%+n]×k;

[0032] The annual net consumption of KE is calculated according to the formula (X KE +70%g)×k;

[0033] Where k is the number of operating days.

[0034] Optionally, the organic phase flow rate between various systems in the post-processing process is controlled according to the input-output calculation formula, specifically including:

[0035] According to the input-output calculation formula, the organic stock of each sub-item is obtained;

[0036] When the organic stock of each sub-item exceeds 80% of the total stock of the system, it indicates that there is a risk of material accumulation in the organic phase in the system; when the organic stock of each sub-item is less than 20% of the total stock of the system, it indicates that there is a risk of material shortage in the organic phase in the system.

[0037] A second aspect of the embodiment of the present application provides a control device for organic phase circulation in spent fuel post-processing, the device comprising:

[0038] A relationship determination module is used to obtain the organic phase supply and demand relationship between various systems in the post-processing process;

[0039] A data acquisition module, for acquiring the organic phase flow rate and the organic phase usage of each extraction supply and demand based on the organic phase supply and demand relationship;

[0040] A formula determination module is used to determine the input and output volume calculation formula of each organic phase between each extraction process and the contaminated solvent distillation process based on the equality of the total volume of the input and output organic phases of each extraction process and the total conservation relationship of TBP and KE;

[0041] The flow control module is used to control the organic phase flow between various systems in the post-processing process according to the input and output calculation formula.

[0042] A third aspect of the embodiments of the present application provides a device for organic phase circulation in spent fuel post-processing, including a memory and a processor;

[0043] The memory is used to store programs;

[0044] The processor is used to execute the program to implement any one of the control methods for organic phase circulation in spent fuel post-processing provided in the first aspect of the embodiment of the present application.

[0045] A fourth aspect of an embodiment of the present application provides a computer-readable storage medium having a computer program stored thereon. When the computer program is executed by a processor, any one of the control methods for organic phase circulation in spent fuel reprocessing provided in the first aspect of the embodiment of the present application is implemented.

[0046] The beneficial technical effects of this application are:

[0047] The embodiment of the present application provides a control method and device for organic phase circulation in spent fuel post-processing, the method comprising: obtaining the organic phase supply and demand relationship between various systems in the post-processing process; based on the organic phase supply and demand relationship, obtaining the organic phase flow rate and organic phase usage of each extraction supply and demand; based on the total volume of the input and output organic phase of each extraction process being equal and the total conservation relationship of TBP and KE, determining the input and output calculation formula of each organic phase between each extraction process and the contaminated solvent distillation process; according to the input and output calculation formula, controlling the organic phase flow rate between various systems in the post-processing process. The embodiment of the present application is suitable for quantitative calculation of organic phase input and output under multiple working conditions. According to the actual consumption of KE in the co-decontamination and plutonium purification extraction process and uranium purification extraction process, the receiving amount of TK80 after distillation and the receiving amount and delivery amount of TK30 are calculated, and requirements are put forward for the distillation product amount of the contaminated solvent distillation process, which can be directly used for spent fuel post-processing commissioning and production operations, realize the quantitative replacement of organic phase in the extraction process and the inventory monitoring of the process system, and ensure the continuous and stable operation of the process system under the organic phase circulation system. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] Figure 1 A schematic flow chart of a control method for organic phase circulation in spent fuel reprocessing provided in an embodiment of the present application;

[0049] Figure 2 A schematic diagram of the organic phase circulation relationship in a control method for organic phase circulation in spent fuel reprocessing provided in an embodiment of the present application. DETAILED DESCRIPTION

[0050] In order to make those skilled in the art better understand the present application, the technical scheme in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the embodiments described below are only a part of the embodiments of the present application, not all. Based on the embodiments recorded in the present application, all other embodiments obtained by those skilled in the art without paying creative work are within the scope of protection of the present application.

[0051] The inventors of this application have found in their research that the total amount of fresh 30% TBP-KE and KE entering the system can be controlled to avoid the accumulation of 30% TBP-KE and kerosene and solve the accumulation problem. However, how to establish the organic phase circulation balance relationship between the extraction process, the solvent regeneration process, and the dirty solvent distillation process has become an urgent problem to be solved.

[0052] To this end, the embodiment of the present application provides a quantitative calculation of organic phase input and output under multiple working conditions to ensure that the process system can operate normally under the organic phase recycling system. The receiving amount of TK80 after distillation and the receiving amount and delivery amount of TK30 are calculated according to the actual consumption of KE in the co-decontamination and plutonium purification extraction process and uranium purification extraction process, and requirements are put forward for the distillation product amount (TK80, KE) of the contaminated solvent distillation process.

[0053] Based on the above content, in order to clearly and in detail illustrate the above advantages of the present application, the specific implementation methods of the present application will be described below in conjunction with the accompanying drawings.

[0054] See also Figure 1 , which is a schematic flow chart of a control method for organic phase circulation in spent fuel post-processing provided in an embodiment of the present application.

[0055] A control method for organic phase circulation in spent fuel reprocessing provided in an embodiment of the present application includes:

[0056] Step S101: obtaining the organic phase supply and demand relationship between various systems in the post-processing process;

[0057] Step S102: based on the organic phase supply and demand relationship, obtaining the organic phase flow rate and organic phase usage of each extraction supply and demand;

[0058] Step S103: Based on the equal total volume of the input and output organic phases of each extraction process and the conservation relationship of the total amount of TBP and KE, the calculation formula for the input and output volume of each organic phase between each extraction process and the contaminated solvent distillation process is determined;

[0059] Step S104: According to the input-output calculation formula, the organic phase flow rate between various systems in the post-processing process is controlled.

[0060] In the embodiment of the present application, the extraction cycle, solvent regeneration system, and solvent distillation system organic phase circulation desktop deduction are carried out to determine the organic phase inventory of each system and the transfer volume of each material between interfaces to ensure the establishment of an organic phase circulation system. The supply and demand relationship of the organic phase between the systems is sorted out to obtain a preliminary circulation relationship; the flow rate and usage of the organic phase of each extraction process are counted, and the input and output of the organic phase between each process is set as an unknown number; the input and output calculation formula between each extraction process and the dirty solvent distillation process is derived by using the total volume of the input and output organic phase of each extraction process to be equal, and the total conservation relationship of TBP and KE. It is suitable for quantitative calculation of organic phase input and output under multiple working conditions. According to the actual consumption of KE in the co-decontamination and plutonium purification extraction process and uranium purification extraction process, the receiving amount of TK80 after distillation and the receiving amount and delivery amount of TK30 are calculated, and the distillation product amount (TK80, KE) of the dirty solvent distillation process is required. Early warning of the organic phase inventory of each process. When the organic inventory of each sub-item exceeds 80% of the total inventory of the system, it indicates that there is a risk of accumulation of organic phase in the system; when the system inventory is less than 20% of the total inventory, it indicates that there is a risk of material shortage in the organic phase in the system. It is necessary to adjust the distribution of the organic phase according to the inventory results of the organic phase or determine whether it is necessary to supplement fresh organic phase from the reagent preparation. It is applicable to the calculation of the replacement ratio of the organic phase in the extraction process under multiple working conditions.

[0061] In some possible implementations of the present application, in order to ensure that there is no accumulation of organic phase in the co-decontamination and plutonium purification, uranium purification, and contaminated solvent distillation processes, ignoring the influence of density difference on volume and the influence of organic phase entrainment loss in the process system, the total volume of the input and output organic phases of each extraction process is equal, and the total amount of TBP and KE is conserved, which may specifically include:

[0062] The total volume of the input and output organic phases in the co-decontamination and plutonium purification extraction steps is equal;

[0063] The total volume of the input and output organic phases in the uranium purification and extraction process is equal;

[0064] The output TK30 from the uranium purification and extraction process is sent to co-decontamination and plutonium purification;

[0065] The total amount of TBP in the co-decontamination and plutonium purification extraction process is conserved;

[0066] The total amount of TBP in the uranium purification and extraction process is conserved;

[0067] The total amount of KE in the co-decontamination and plutonium purification process is conserved;

[0068] Also, the total amount of uranium purification KE process is conserved.

[0069] In one example, the input-output calculation formula may specifically include:

[0070] The input amount of 80% TBP-kerosene in the co-decontamination and plutonium purification extraction process is 0.51c-0.09fm 3 / d, 30% TBP-kerosene input is 1.6f+gm 3 / d, the output of 30% TBP-kerosene is 1.51c+1.51f+gm 3 / d, the input amount of kerosene is cm 3 / d, the replacement ratio of 30% TBP-kerosene is (1.51c-0.09f) / ∑0.024X i m 3 / d, the replacement ratio of kerosene is c / ∑0.024Y i m 3 / d;

[0071] In the uranium purification and extraction process, the input amount of 80% TBP-kerosene is 0.6fm 3 / d, 30% TBP-kerosene output is 1.6fm 3 / d, the input amount of kerosene is fm 3 / d, the replacement ratio of 30% TBP-kerosene is 1.6f / ∑0.024Z i m 3 / d, the replacement ratio of kerosene is f / ∑0.024P i m 3 / d;

[0072] In the dirty solvent distillation process, the output of 80% TBP-kerosene is 0.51 (c+f) m 3 / d, 30% TBP-kerosene input is 1.51c+1.51f+gm 3 / d, the output of 30% TBP-kerosene is nm 3 / d, the output of kerosene is c+fm 3 / d;

[0073] Wherein, c is the kerosene input amount of the co-decontamination and plutonium purification and extraction process, f is the kerosene input amount of the uranium purification and extraction process, g is the daily usage of fresh 30% TBP-kerosene in the 2BS column, n is the residual liquid output of the contaminated solvent distillation process, and X i The 30% TBP-kerosene operating flow rate of each extraction equipment in the co-decontamination and plutonium purification extraction process, Y i is the kerosene flow rate of each deoiling equipment in the co-decontamination and plutonium purification and extraction process, Z i The 30% TBP-kerosene operating flow rate of each extraction equipment in the uranium purification and extraction process, P i It is the kerosene operating flow rate of each deoiling equipment in the uranium purification process.

[0074] A desktop simulation of the organic phase supply and demand relationship between the systems was performed to obtain a preliminary circulation relationship. Figure 2 An example schematic diagram of an organic phase circulation relationship is shown.

[0075] Among them, the reagent preparation system: the preparation and transportation of fresh TBP-kerosene and kerosene is the input point of the organic phase circulation. Co-decontamination separation system: use TK30 to extract-wash-separate the uranium and plutonium in the feed liquid to obtain uranium-containing feed liquid and plutonium-containing feed liquid, and use kerosene to remove TBP in the aqueous phase feed liquid after extraction. Uranium purification system: use TK30 to evaporate-extract-wash-strip the uranium-containing feed liquid from the co-decontamination separation system to further purify and concentrate the uranium-containing feed liquid, and use kerosene to remove TBP in the aqueous phase feed liquid after extraction. Plutonium purification system: use TK30 to extract-wash-strip the plutonium-containing feed liquid from the co-decontamination separation system to further purify and concentrate the plutonium-containing feed liquid, and use kerosene to remove TBP in the aqueous phase feed liquid after extraction. Solvent regeneration system: There are two systems, which respectively carry out alkali washing and acid washing on the organic phase after use in the co-decontamination separation system and the uranium purification system. Part of the washed organic phase is reused for seasoning, and part is sent to the solvent distillation system. Solvent distillation system: The organic phase after alkali washing in the solvent regeneration system is distilled to obtain distillation TK80 and distillation KE for reuse in the co-decontamination separation system, uranium purification system, plutonium purification system and solvent regeneration system. The distillation residue is incinerated and is the output point of the organic phase circulation. The purple line in the figure is the input and output path of the organic phase, the yellow line is the circulation path of TK30, the blue line is the reuse path of distillation KE, the red line is the reuse path of distillation TK80, and the green line is the backup path for the introduction of the organic phase. KE: kerosene, TBP: tributyl phosphate, TK30: 30% TBP-kerosene, TK80: 80% TBP-kerosene.

[0076] The flow rate and usage of the organic phase in the extraction process are statistically analyzed, and the statistics are shown in Table 1. The input and output relationship of the organic phase between the extraction process and the dirty solvent distillation process is sorted out, and the unknown variables are set. The specific parameter settings are shown in Table 2.

[0077] Table 1 Statistics of organic phase flow and usage in extraction process

[0078]

[0079]

[0080]

[0081] Table 2 Relationship between organic phase input and output

[0082]

[0083] Among them, the TK30 input to the contaminated solvent distillation process comes from the co-decontamination and plutonium purification extraction process, so the TK30 input value of the contaminated solvent distillation process = the TK30 output value of the co-decontamination and plutonium purification extraction process. The TK80 and KE output from the contaminated solvent distillation process are sent to the co-decontamination and plutonium purification extraction process and the uranium purification extraction process for reuse, so the TK80 output value of the contaminated solvent distillation process = the TK80 input value of the co-decontamination and plutonium purification extraction process + the TK80 input value of the uranium purification extraction process; the KE output value of the contaminated solvent distillation process = the KE input value of the co-decontamination and plutonium purification extraction process + the KE input value of the uranium purification extraction process. All 2BS columns use fresh TK30 prepared from reagents, and the daily input amount is m. The residual liquid output of the contaminated solvent distillation process is n. The unknown variables were calculated by using the equal total volume of the input and output organic phases of each extraction process and the conservation relationship of the total amount of TBP and KE, and the input and output calculation formulas between each extraction process and the contaminated solvent distillation process were derived.

[0084] In order to ensure that there is no accumulation of organic phase in the co-decontamination, plutonium purification, uranium purification, and contaminated solvent distillation processes, ignoring the effect of density difference on volume and the effect of organic phase entrainment losses in the process system, it can be obtained:

[0085] The total volume of the input and output organic phases of the co-decontamination and plutonium purification extraction process is equal: a+b+c=d The total volume of the input and output organic phases of the uranium purification extraction process is equal: e+f=j

[0086] The output TK30 from the uranium purification and extraction process is sent to co-decontamination and plutonium purification: b = j

[0087] Total TBP conservation in the co-decontamination and plutonium purification extraction process: 0.8*a+0.3*b=0.27*d

[0088] Conservation of total TBP in uranium purification and extraction process: 0.8*e=0.3b

[0089] Total KE conservation in the co-decontamination and plutonium purification process: c+0.7*b+0.2*a=0.73*d

[0090] Conservation of total amount of uranium purification KE process: f+0.2e=0.7*j

[0091] Taking the KE input of the co-decontamination and plutonium purification extraction process and the uranium purification extraction process as input values ​​and combining the above equation relationship, the following model relationship can be obtained:

[0092] Table 3 Organic phase circulation model

[0093]

[0094]

[0095] Wherein, Xi is the TK30 operating flow rate of each extraction equipment in the co-decontamination and plutonium purification extraction process, in L / h; Yi is the KE operating flow rate of each oil removal equipment in the co-decontamination and plutonium purification extraction process, in L / h; m is the daily usage of fresh TK30 of 2BS column, in m 3 ; Zi is the TK30 operating flow rate of each extraction equipment in the uranium purification and extraction process, in L / h; Pi is the KE operating flow rate of each oil removal equipment in the uranium purification process, in L / h.

[0096] In some possible implementations of the embodiments of the present application, the method may further include a method for calculating the net organic phase consumption based on the number of operating days and the organic phase loss data. Specifically, it includes:

[0097] The consumption of the organic phase was obtained based on the operating days of each system and the organic phase storage tank data.

[0098] In one example, obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data may specifically include:

[0099] The net daily consumption of TBP is (X TK30 +m)×30%+n

[0100] KE daily net consumption = X KE +70%g

[0101] Among them, X TK30 is the daily loss of 30% TBP-kerosene in the organic phase storage tank, X KE It is the daily loss of kerosene in the organic phase storage tank.

[0102] In another example, obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data may further include:

[0103] The annual net consumption of TBP is calculated according to the formula [(X TK30 +g)×30%+n]×k;

[0104] The annual net consumption of KE is calculated according to the formula (X KE +70%g)×k;

[0105] Where k is the number of operating days.

[0106] In some possible implementations of the embodiments of the present application, step S104 may specifically include:

[0107] According to the input-output calculation formula, the organic stock of each sub-item is obtained;

[0108] When the organic stock of each sub-item exceeds 80% of the total stock of the system, it indicates that there is a risk of material accumulation in the organic phase in the system; when the organic stock of each sub-item is less than 20% of the total stock of the system, it indicates that there is a risk of material shortage in the organic phase in the system.

[0109] Based on the control method for organic phase circulation in spent fuel reprocessing provided in the above embodiment, the embodiment of the present application further provides a control device for organic phase circulation in spent fuel reprocessing.

[0110] A control device for organic phase circulation in spent fuel post-processing provided in an embodiment of the present application includes:

[0111] A relationship determination module is used to obtain the organic phase supply and demand relationship between various systems in the post-processing process;

[0112] A data acquisition module, for acquiring the organic phase flow rate and the organic phase usage of each extraction supply and demand based on the organic phase supply and demand relationship;

[0113] A formula determination module is used to determine the input and output volume calculation formula of each organic phase between each extraction process and the contaminated solvent distillation process based on the equality of the total volume of the input and output organic phases of each extraction process and the total conservation relationship of TBP and KE;

[0114] The flow control module is used to control the organic phase flow between various systems in the post-processing process according to the input and output calculation formula.

[0115] Based on the control method and device for organic phase circulation in spent fuel post-processing provided in the above embodiment, the embodiment of the present application further provides a device for organic phase circulation in spent fuel post-processing, including a memory and a processor;

[0116] The memory is used to store programs;

[0117] The processor is used to execute the program to implement any one of the control methods for organic phase circulation in spent fuel post-processing provided in the above embodiments.

[0118] Based on the control method and device for organic phase circulation of spent fuel reprocessing provided in the above embodiment, the embodiment of the present application further provides a computer-readable storage medium having a computer program stored thereon. When the computer program is executed by a processor, any one of the control methods for organic phase circulation of spent fuel reprocessing provided in the above embodiment is implemented.

[0119] The present application is described in detail above in conjunction with the accompanying drawings and embodiments, but the present application is not limited to the above embodiments, and various changes can be made within the knowledge of ordinary technicians in the field without departing from the purpose of the present application. Any content not described in detail in the present application can adopt the existing technology.

Claims

1. A control method for organic phase circulation in spent fuel reprocessing, characterized in that: The method comprises: Obtain the organic phase supply and demand relationship between various systems in the post-processing process; Based on the organic phase supply and demand relationship, obtaining the organic phase flow rate and organic phase usage of each extraction supply and demand; Based on the equal total volume of the input and output organic phases of each extraction process and the conservation relationship between the total amount of TBP and KE, the calculation formulas for the input and output volume of each organic phase between each extraction process and the contaminated solvent distillation process are determined; According to the input-output calculation formula, the organic phase flow rate between various systems in the post-processing process is controlled.

2. The control method for organic phase circulation in spent fuel reprocessing according to claim 1, characterized in that: The total volume of the input and output organic phases of each extraction step is equal, and the total amount of TBP and KE is conserved, specifically including: The total volume of the input and output organic phases in the co-decontamination and plutonium purification extraction steps is equal; The total volume of the input and output organic phases in the uranium purification and extraction process is equal; The output TK30 from the uranium purification and extraction process is sent to co-decontamination and plutonium purification; The total amount of TBP in the co-decontamination and plutonium purification extraction process is conserved; The total amount of TBP in the uranium purification and extraction process is conserved; The total amount of KE in the co-decontamination and plutonium purification process is conserved; Also, the total amount of uranium purification KE process is conserved.

3. The control method for organic phase circulation in spent fuel reprocessing according to claim 2, characterized in that: The input and output calculation formula specifically includes: The input amount of 80% TBP-kerosene in the co-decontamination and plutonium purification extraction process is 0.51c-0.09fm 3 / d, 30% TBP-kerosene input is 1.6f+gm 3 / d, the output of 30% TBP-kerosene is 1.51c+1.51f+gm 3 / d, the input amount of kerosene is cm 3 / d, the replacement ratio of 30% TBP-kerosene is (1.51c-0.09f) / ∑0.024X i m 3 / d, the replacement ratio of kerosene is c / ∑0.024Y i m 3 / d; In the uranium purification and extraction process, the input amount of 80% TBP-kerosene is 0.6fm 3 / d, 30% TBP-kerosene output is 1.6fm 3 / d, the input amount of kerosene is fm 3 / d, the replacement ratio of 30% TBP-kerosene is 1.6f / ∑0.024Z i m 3 / d, the replacement ratio of kerosene is f / ∑0.024P i m 3 / d; In the dirty solvent distillation process, the output of 80% TBP-kerosene is 0.51 (c+f) m 3 / d, 30% TBP-kerosene input is 1.51c+1.51f+gm 3 / d, the output of 30% TBP-kerosene is nm 3 / d, the output of kerosene is c+fm 3 / d; Wherein, c is the kerosene input amount of the co-decontamination and plutonium purification and extraction process, f is the kerosene input amount of the uranium purification and extraction process, g is the daily usage of fresh 30% TBP-kerosene in the 2BS column, n is the residual liquid output of the contaminated solvent distillation process, and X i The 30% TBP-kerosene operating flow rate of each extraction equipment in the co-decontamination and plutonium purification extraction process, Y i is the kerosene flow rate of each deoiling equipment in the co-decontamination and plutonium purification and extraction process, Z i The 30% TBP-kerosene operating flow rate of each extraction equipment in the uranium purification and extraction process, P i It is the kerosene operating flow rate of each deoiling equipment in the uranium purification process.

4. The control method for organic phase circulation in spent fuel reprocessing according to claim 3, characterized in that: The method further comprises: The consumption of the organic phase was obtained based on the operating days of each system and the organic phase storage tank data.

5. The control method for organic phase circulation in spent fuel reprocessing according to claim 4, characterized in that: The method of obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data specifically includes: The net daily consumption of TBP is (X TK30 +m)×30%+n KE daily net consumption = X KE +70%g Among them, X TK30 is the daily loss of 30% TBP-kerosene in the organic phase storage tank, X KE It is the daily loss of kerosene in the organic phase storage tank.

6. The control method for organic phase circulation in spent fuel reprocessing according to claim 5, characterized in that: The method of obtaining the consumption of the organic phase according to the operating days of each system and the organic phase storage tank data specifically includes: The annual net consumption of TBP is calculated according to the formula [(X TK30 +g)×30%+n]×k; The annual net consumption of KE is calculated according to the formula (X KE +70%g)×k; Where k is the number of running days.

7. The control method for organic phase circulation in spent fuel reprocessing according to any one of claims 1 to 6, characterized in that: The control of the organic phase flow rate between various systems in the post-processing process according to the input-output calculation formula specifically includes: According to the input-output calculation formula, the organic stock of each sub-item is obtained; When the organic stock of each sub-item exceeds 80% of the total stock of the system, it indicates that there is a risk of material accumulation in the organic phase in the system; when the organic stock of each sub-item is less than 20% of the total stock of the system, it indicates that there is a risk of material shortage in the organic phase in the system.

8. A control device for organic phase circulation in spent fuel reprocessing, characterized in that: The device comprises: A relationship determination module is used to obtain the organic phase supply and demand relationship between various systems in the post-processing process; A data acquisition module, for acquiring the organic phase flow rate and the organic phase usage of each extraction supply and demand based on the organic phase supply and demand relationship; A formula determination module is used to determine the input and output volume calculation formula of each organic phase between each extraction process and the contaminated solvent distillation process based on the equality of the total volume of the input and output organic phases of each extraction process and the total conservation relationship of TBP and KE; The flow control module is used to control the organic phase flow between various systems in the post-processing process according to the input and output calculation formula.

9. A device for organic phase circulation in spent fuel reprocessing, characterized in that: including memory and processor; The memory is used to store programs; The processor is used to execute the program to implement the control method for organic phase circulation in spent fuel reprocessing according to any one of claims 1 to 7.

10. A computer-readable storage medium having a computer program stored thereon, characterized in that: When the computer program is executed by a processor, the control method for organic phase circulation in spent fuel reprocessing according to any one of claims 1 to 7 is implemented.

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