A method, system and storage medium for determining the size of a burst disc

Abstract

The application discloses a method and system for determining the size of a rupture disc and a storage medium. The method comprises: separating condensable vapor and non-condensable gas generated by a small test reactor when an uncontrolled reaction occurs in the small test reactor; determining the generation rate of the condensable vapor according to the mass change rate of the condensable vapor and determining the generation rate of the non-condensable gas according to the pressure change rate of the non-condensable gas; determining the maximum gas phase discharge rate of an industrial reactor according to the generation rate of the condensable vapor and the generation rate of the non-condensable gas of the small test reactor; and determining the design size of the rupture disc of the industrial reactor according to the maximum gas phase discharge rate of the industrial reactor under an uncontrolled reaction. The scheme provided by the application has the advantages that the generation rates of the condensable vapor and the non-condensable gas in the discharge material are separated, the generation rates of the condensable vapor and the non-condensable gas are calculated respectively, the calculation accuracy of the maximum gas phase discharge rate is improved, and the rationality of the size design of the rupture disc is improved.

Description

Technical Field

[0001] This application relates to the field of chemical technology, and in particular to a method, system and storage medium for determining the size of a rupture disc. Background Technology

[0002] In chemical production, runaway chemical reactions are a major cause of accidents. To ensure safe production, rupture discs are often installed on reactors for protection. The calculation of the rupture disc size requires precise calculation of the runaway reaction release rate in the reactor.

[0003] For calculating the runaway reaction release rate, especially for non-adjustable complex reaction systems, the pressure generated by the runaway reaction is due to the superposition of non-condensable gases and condensable vapors. The current common method is to first obtain the release parameters such as temperature and pressure using an adiabatic calorimeter, and then calculate the runaway reaction release rate using the DIERS-recommended formula. However, for non-adjustable complex reaction systems, due to the complexity of the material decomposition products, the vaporization enthalpy of condensable vapors is often difficult to obtain using this method, leading to conservative calculations and an overestimation of the maximum gas-phase release rate. Furthermore, when calculating the reactor rupture disc size based on the maximum gas-phase release rate, the rupture disc size is also overestimated.

[0004] Therefore, how to rationally design the size of the rupture disc has become a technical problem that urgently needs to be solved. Summary of the Invention

[0005] This application provides a method, system, and storage medium for determining the size of a rupture disc, for the purpose of rationally designing the size of a rupture disc.

[0006] This application provides a method for determining the size of a rupture disc, including:

[0007] When a runaway reaction occurs in the pilot reactor, the condensable and non-condensable gases produced in the pilot reactor are separated.

[0008] The generation rate of condensable steam is determined based on the mass change rate of condensable steam, and the generation rate of non-condensable gas is determined based on the pressure change rate of non-condensable gas.

[0009] The maximum gas phase venting rate of the industrial reactor is determined based on the generation rates of condensable and non-condensable gases in the pilot reactor.

[0010] The design dimensions of the rupture disc of the industrial reactor are determined based on the maximum gas-phase venting rate under runaway reaction conditions.

[0011] The beneficial effects of this application are as follows: When a runaway reaction occurs in a pilot-scale reactor, the condensable and non-condensable gases produced in the pilot-scale reactor are separated. The generation rate of the condensable gas is determined based on the mass change rate of the condensable gas, and the generation rate of the non-condensable gas is determined based on the pressure change rate of the non-condensable gas. Furthermore, the maximum gas-phase release rate of the industrial reactor is determined based on the generation rates of the condensable and non-condensable gases. Since the generation rates of the condensable and non-condensable gases can be determined separately, and the generation rate of the condensable gas is obtained by measuring the mass generation rate, it is not necessary to consider the vaporization enthalpy of the condensable gas, thus improving the calculation accuracy of the maximum gas-phase release rate of the industrial reactor. Finally, the design size of the rupture disc of the industrial reactor is determined based on the maximum gas-phase release rate under the runaway reaction of the industrial reactor, improving the rationality of the rupture disc size design.

[0012] In one embodiment, the separation of condensable steam and non-condensable gas generated by the pilot reactor includes:

[0013] The condensable and non-condensable gases generated in the reactor are cooled by a material venting cooling device.

[0014] The condensate after cooling is controlled to enter the condensate container in order to separate condensable vapors and non-condensable gases.

[0015] In one embodiment, determining the condensable steam generation rate based on the mass change rate of condensable steam includes:

[0016] The rate of change of condensate mass is obtained by a weighing device installed at the bottom of the condensate container.

[0017] The rate of condensable vapor generation is calculated based on the mass change rate of the condensate.

[0018] In one embodiment, determining the noncondensable gas generation rate based on the noncondensable gas pressure change rate includes:

[0019] Non-condensable gas is controlled to enter a release material tank, wherein the release material tank is connected to a non-condensable gas tank;

[0020] By controlling the exhaust valve of the venting material tank between the venting material tank and the non-condensable gas tank, all excess gas in the venting material tank is discharged into the non-condensable gas tank, so that the pressure of the venting material tank remains constant.

[0021] Obtain the pressure change rate of the non-condensable gas tank;

[0022] The rate of noncondensable gas generation is determined based on the pressure change rate of the noncondensable gas tank.

[0023] In one embodiment, determining the design dimensions of the rupture disc of the industrial reactor based on the maximum gas-phase venting rate under runaway reaction includes:

[0024] The calculated values ​​of multiple flow capacities of the rupture disc are determined based on at least the set pressure of multiple venting tanks and the reaction vessel material temperature at the corresponding maximum gas phase venting rate point.

[0025] Multiple rupture disc sizes are determined based on the maximum gas phase release rate under runaway reaction at the set pressure of the different venting material tanks and the calculated value of the corresponding rupture disc flow capacity.

[0026] The minimum value among the multiple rupture disc dimensions is selected as the design dimension of the rupture disc.

[0027] In one embodiment, determining the flow capacity of the rupture disc based at least on the set pressure of multiple venting tanks and the reaction vessel material temperature corresponding to the maximum gas phase venting rate point includes:

[0028] Determine the outlet pressure and critical pressure of the rupture disc;

[0029] When the outlet pressure of the rupture disc is less than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0030]

[0031] Where G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, k is the average heat capacity ratio of non-condensable gas and condensable gas, M is the average molecular weight of non-condensable gas and condensable gas, R is the ideal gas constant, and T1 is the material temperature of the reaction vessel corresponding to the maximum rate point.

[0032] In one embodiment, the critical pressure of the rupture disc is determined by the following formula:

[0033]

[0034] Among them, P cf P1 is the critical pressure of the rupture disc, P1 is the set pressure of the venting material tank, and k is the average heat capacity ratio of the vented gas and condensable steam.

[0035] In one embodiment, the method further includes:

[0036] When the outlet pressure of the rupture disc is greater than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0037]

[0038] In the above formula, G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, and P ddenoted as rupture disc outlet pressure, k as the average heat capacity ratio of non-condensable gas and condensable gas, M as the average molecular weight of non-condensable gas and condensable gas, R as the ideal gas constant, and T1 as the material temperature of the reaction vessel corresponding to the maximum rate point.

[0039] This application also provides a system for determining the size of a rupture disc, comprising:

[0040] At least one processor; and,

[0041] A memory communicatively connected to the at least one processor; wherein,

[0042] The memory stores instructions that can be executed by the at least one processor to implement the method for determining the rupture disc size as described in any of the above embodiments.

[0043] This application also provides a computer-readable storage medium, which, when the instructions in the storage medium are executed by a processor corresponding to a rupture disc size determination system, enables the rupture disc size determination system to implement the rupture disc size determination method described in any of the above embodiments.

[0044] Other features and advantages of this application will be set forth in the description which follows, and will be apparent in part from the description, or may be learned by practicing the application. The objectives and other advantages of this application may be realized and obtained by means of the structures particularly pointed out in the written description, claims, and drawings.

[0045] The technical solution of this application will be further described in detail below with reference to the accompanying drawings and embodiments. Attached Figure Description

[0046] The accompanying drawings are provided to further illustrate the present application and form part of the specification. They are used together with the embodiments of the present application to explain the application and do not constitute a limitation thereof. In the drawings:

[0047] Figure 1 This is a flowchart illustrating a method for determining the size of a rupture disc in one embodiment of this application;

[0048] Figure 2 This is a structural diagram of a reaction simulation device in one embodiment of this application;

[0049] Figure 3 This is a schematic diagram of the hardware structure of a system with a rupture disc size according to an embodiment of this application;

[0050] Figure 2 The annotations in the attached figures are explained as follows:

[0051] 201—Reaction auxiliary equipment; 202—Small-scale reactor; 203—Cooling device; 204—Relief material tank; 205—Relief material distributor; 206—Condensate container; 207—Weighing device; 208—Relief material tank gas supply valve; 209—Relief material tank pressure sensor; 210—Relief material tank exhaust valve; 211—Non-condensable gas tank; 212—Non-condensable gas tank pressure sensor; 213—Non-condensable gas tank exhaust valve; 214—Controller; 215—Computer. Detailed Implementation

[0052] The preferred embodiments of this application are described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are for illustration and explanation only and are not intended to limit this application.

[0053] Figure 1 This is a flowchart of a method for determining the size of a rupture disc according to an embodiment of this application, as shown below. Figure 1 As shown, the method can be implemented as follows: S101-S104:

[0054] In step S101, when a runaway reaction occurs in the pilot reactor, the condensable steam and non-condensable gas generated in the pilot reactor are separated.

[0055] In step S102, the generation rate of condensable steam is determined based on the mass change rate of condensable steam, and the generation rate of non-condensable gas is determined based on the pressure change rate of non-condensable gas.

[0056] In step S103, the maximum gas phase venting rate of the industrial reactor is determined based on the generation rate of condensable gas and the generation rate of non-condensable gas in the pilot reactor.

[0057] In step S104, the design size of the rupture disc of the industrial reactor is determined based on the maximum gas phase release rate under runaway reaction conditions.

[0058] In this application, a pilot-scale reactor is used to simulate an industrial reactor. Figure 2 This is a structural diagram of a reaction simulation device in one embodiment of this application. The method provided in this application can be achieved through, as shown in... Figure 2 The device shown is implemented as follows. (As...) Figure 2As shown, when the reactive materials in the pilot reactor 202 of the reaction simulation equipment undergo a secondary reaction, the reactive materials self-heat. The condensable vapors and non-condensable gases generated during the reaction process enter the venting material cooling device 203 through the venting pipeline. The venting material is cooled in the venting material cooling device 203, and the condensable vapors in the venting material become condensate, which enters the venting material distributor 205 in the venting material tank 204 together with the non-condensable gases. The venting material tank 204 is connected to the non-condensable gas tank 211 through a pipeline. A weighing device 207 is installed at the bottom of the venting material tank 204, and a condensate container 206 is installed on the weighing device 207. The venting material undergoes gas-liquid separation in the venting material distributor 205, where the condensate enters the condensate container 206, and the non-condensable gases accumulate in the venting material tank 204. A nitrogen purging valve 208 for the venting tank is connected to the venting tank via a pipeline and is used to purge and pressurize the system with nitrogen before the experiment begins. An exhaust valve 210 for the venting tank has its inlet connected to the venting tank via a pipeline. Adjusting the opening of the exhaust valve 210 helps maintain a constant pressure in both the reaction vessel and the venting tank. Excess non-condensable gas in the venting tank 204 enters the non-condensable gas tank 211 through the venting exhaust pipeline. During the test, the weighing device 207, the venting tank pressure sensor 209, the venting tank exhaust valve 210, and the non-condensable gas tank pressure sensor 212 are controlled by a controller 214. Simultaneously, the controller 214 is connected to a computer 215 to record, process, and analyze the collected data and output control commands.

[0059] In this application, when a runaway reaction occurs in the pilot-scale reactor, the condensable and non-condensable gases produced in the reactor are separated. Condensable gas is steam generated during the venting process; steam can transfer heat through liquid-phase evaporation and condense into a liquid at room temperature, such as water vapor. Non-condensable gas refers to gases that are in the gaseous phase at room temperature, such as carbon monoxide, carbon dioxide, and methane. Figure 2 In the illustrated device, a material venting cooling device cools the condensable and non-condensable gases generated in the pilot reactor. After a runaway reaction occurs in the pilot reactor, the vented material enters the cooling device through a pipeline. The condensable gas condenses into a liquid after passing through the cooling device, while the non-condensable gas remains a gas, thus achieving separation of the condensable and non-condensable gases. The cooled condensate is then controlled to enter a condensate container to further separate the condensable and non-condensable gases. After cooling the condensable gas to form condensate, the condensate can be collected in the condensate container, while the non-condensable gas remains a gas, thus achieving separation of the condensable and non-condensable gases. Of course, the separation of condensable and non-condensable gases can also be achieved using other methods for condensable gas, and this application does not limit this approach.

[0060] The generation rate of condensable vapors is determined based on the mass change rate of condensable vapors, and the generation rate of non-condensable gases is determined based on the pressure change rate of non-condensable gases. Due to the properties of different gases, and since condensable vapors can condense into liquids, the mass of condensable vapors produced in the reactor can be determined by weighing, and thus the generation rate of condensable vapors can be determined based on their mass. Specifically, since the condensate is collected in a condensate container in liquid form, the mass of condensable vapors can be obtained by weighing the condensate. In cases such as... Figure 2 In the illustrated apparatus, the condensate container 206 is weighed using the weighing device 207, and the mass of the condensable vapor is obtained by measuring the change in the weighing value. After obtaining the mass of the condensable vapor, the rate of change of the condensate mass can be determined using the following formula:

[0061]

[0062] Among them, w 液 Let m be the rate of mass change of the condensate. 液 t represents the mass of the condensate, and t represents the time during which the reaction proceeds.

[0063] Finally, the condensable steam generation rate of the industrial reactor is calculated based on the condensate mass change rate. Specifically, the condensable steam generation rate is determined using the following formula:

[0064]

[0065] Among them, w 可 The rate of condensable steam generation; m e denoted as , where m is the mass of material in the pilot reactor at the initial moment; m is the mass of material in the industrial reactor.

[0066] For non-condensable gases, the generation rate of the non-condensable gases can be determined by the pressure change rate of the generated non-condensable gases. In this embodiment, the non-condensable gases are controlled to enter a venting tank, which is connected to a non-condensable gas tank. Figure 2As shown, before the experiment, the system was purged and pressurized with nitrogen. The condensable vapors in the released material were converted into condensate and entered the released material tank 204 along with the non-condensable gases. The released material tank 204 was connected to the non-condensable gas tank 211 via the released material tank exhaust valve 210. During the experiment, the pressure in the released material tank was kept constant by controlling the exhaust valve between the released material tank and the non-condensable gas tank, thus venting all excess gas in the released material tank into the non-condensable gas tank to maintain a constant pressure. The pressure in the released material tank can be measured in real time using a pressure sensor. Simultaneously, the pressure in the non-condensable gas tank can be measured in real time using a pressure sensor, thereby obtaining the pressure change rate of the non-condensable gas tank. The generation rate of non-condensable gases is determined based on the pressure change rate of the non-condensable gas tank. Specifically, the generation rate of non-condensable gases is determined using the following formula:

[0067]

[0068] Among them, w 不 The rate of noncondensable gas generation; V is the pressure change rate of the non-condensable gas tank; M is the volume of the non-condensable gas tank; 不 R is the average molecular weight of the noncondensable gas; T is the gas constant; m is the room temperature. e denoted as , where m is the mass of material in the pilot reactor at the initial moment; m is the mass of material in the industrial reactor.

[0069] After obtaining the generation rates of condensable steam and non-condensable gas respectively, the maximum gas phase venting rate of the industrial reactor can be determined based on the generation rates of condensable steam and non-condensable gas.

[0070]

[0071] Among them, w 可 The rate of condensable steam generation; w 不 m is the rate of noncondensable gas production. 液 The mass of the condensate is given by t, the reaction time is given by P, the pressure of the non-condensable gas tank is given by V, and the volume of the non-condensable gas tank is given by M. 不 R is the average molecular weight of the noncondensable gas; T is the gas constant; m is the room temperature. e denoted as , where m is the mass of material in the pilot reactor at the initial moment; m is the mass of material in the industrial reactor.

[0072] The design size of the reactor's rupture disc is determined based on the maximum gas-phase venting rate under runaway reaction conditions in the industrial reactor. Since the set pressure of the rupture disc should be less than or equal to the reactor's design pressure, multiple pressure values ​​can be selected within the design pressure of the industrial reactor and the back pressure range of the venting pipeline as the control pressure of the venting material tanks. Multiple tests are conducted, and the corresponding design size of the rupture disc is calculated sequentially. Then, the rupture disc sizes corresponding to different control pressures of the venting material tanks are compared, and the smallest rupture disc size is selected as the rupture disc of the industrial reactor. The corresponding maximum gas-phase venting rate is the maximum gas-phase venting rate of the industrial reactor. Specifically, firstly, at least based on the set pressure of multiple venting material tanks and the reaction vessel material temperature at the corresponding maximum gas-phase venting rate point, multiple flow capacity calculations for the rupture disc are determined. First, the outlet pressure and critical pressure of the rupture disc are determined. The critical pressure of the rupture disc is determined using the following formula:

[0073]

[0074] Among them, P cf P1 is the critical pressure of the rupture disc, P1 is the set pressure of the venting tank, and k is the average heat capacity ratio of non-condensable gas and condensable gas.

[0075] Simultaneously, based on the corresponding maximum gas phase venting rate and the venting pipeline resistance, the outlet pressure P of the rupture disc is calculated. d The resistance of the venting pipeline is an inherent property of the pipeline and can be obtained in advance. The rupture disc outlet pressure can be calculated iteratively based on the post-venting treatment pipeline and the venting rate. Alternatively, it can be calculated by obtaining the rupture disc outlet pressure under different maximum gas phase venting rates and venting pipeline resistances through prior experiments, forming a corresponding relationship table, and obtaining the corresponding outlet pressure value by looking up the table.

[0076] When the outlet pressure of the rupture disc is less than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0077]

[0078] Where G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, k is the average heat capacity ratio of non-condensable gas and condensable gas, M is the average molecular weight of non-condensable gas and condensable gas, R is the ideal gas constant, and T1 is the material temperature of the reaction vessel corresponding to the maximum rate point.

[0079] When the outlet pressure of the rupture disc is greater than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0080]

[0081] In the above formula, G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, and P d denoted as rupture disc outlet pressure, k as the average heat capacity ratio of non-condensable gas and condensable gas, M as the average molecular weight of non-condensable gas and condensable gas, R as the ideal gas constant, and T1 as the material temperature of the reaction vessel corresponding to the maximum rate point.

[0082] Then, multiple rupture disc sizes are determined based on the maximum gas-phase release rate under runaway reactions at different set pressures and the calculated flow capacity of the corresponding rupture discs. Specifically, the rupture disc area is calculated using the following formula:

[0083]

[0084] Where A is the rupture disc venting area, W is the maximum gas phase venting rate of the reactor, and G is the flow capacity of the rupture disc.

[0085] Finally, the minimum value among the multiple rupture disc dimensions is selected as the design size of the rupture disc. Using this rupture disc ensures that the reactor pressure will not exceed its design pressure during the venting process.

[0086] The beneficial effects of this application are as follows: When a runaway reaction occurs in a pilot-scale reactor, the condensable and non-condensable gases generated in the pilot-scale reactor are separated. The generation rate of the condensable gas is determined based on the mass change rate of the condensable gas, and the generation rate of the non-condensable gas is determined based on the pressure change rate of the non-condensable gas. Furthermore, the maximum gas-phase release rate of the reactor is determined based on the generation rates of the condensable and non-condensable gases. Since the generation rates of the condensable and non-condensable gases can be determined separately, and the generation rate of the condensable gas is obtained by measuring the mass generation rate, it is not necessary to consider the vaporization enthalpy of the condensable gas, thus improving the measurement accuracy of the maximum gas-phase release rate of the reactor. Finally, the design dimensions of the reactor's rupture disc are determined based on the maximum gas-phase release rate under the runaway reaction of the reactor.

[0087] In one embodiment, step S101 above can be implemented as steps A1-A2 as follows:

[0088] In step A1, the condensable and non-condensable gases generated in the reactor are cooled by a material venting cooling device.

[0089] In step A2, the cooled condensate is controlled to enter the condensate container to achieve the separation of condensable vapors and non-condensable gases.

[0090] In this embodiment, the condensable and non-condensable gases generated in the pilot reactor are cooled by a material venting cooling device. After a runaway reaction occurs in the pilot reactor, the vented material enters the cooling device through a pipeline. The condensable gas condenses into a liquid after passing through the cooling device, while the non-condensable gas remains a gas, thus achieving the separation of condensable and non-condensable gases. Of course, other methods can also be used to separate condensable and non-condensable gases, and this application is not limited to this. Then, the cooled condensate is controlled to enter a condensate container to achieve the separation of condensable and non-condensable gases. After the condensable gas is cooled to form condensate, the condensate can be collected in the condensate container, while the non-condensable gas remains a gas, thus achieving the separation of condensable and non-condensable gases.

[0091] In one embodiment, determining the condensable steam generation rate based on the mass change rate of the condensable steam in step S102 above can be implemented as follows: steps B1-B2:

[0092] In step B1, the mass of the condensate is obtained by a weighing device installed at the bottom of the condensate container;

[0093] In step B2, the rate of condensable vapor generation is calculated based on the rate of change of condensate mass.

[0094] In this embodiment, the mass of condensable vapor is obtained using a weighing device installed at the bottom of the condensate container. Since the condensate is collected in liquid form within the condensate container, the mass of condensable vapor can be obtained by weighing the condensate. Figure 2 In the device shown, the condensate container 206 is weighed by the weighing device 207, and the mass of condensable vapor is obtained by the change of the weighing value.

[0095] After obtaining the mass of the condensable vapor, the rate of change of the condensate mass can be determined using the following formula:

[0096]

[0097] Among them, w 液 Let m be the rate of mass change of the condensate. 液 t represents the mass of the condensate, and t represents the time during which the reaction proceeds.

[0098] Finally, the condensable steam generation rate of the industrial reactor is calculated based on the condensate mass change rate. Specifically, the condensable steam generation rate of the industrial reactor is determined using the following formula:

[0099]

[0100] Among them, w 可 The rate of condensable steam generation in an industrial reactor; m edenoted as , where m is the mass of material in the pilot reactor at the initial moment; m is the mass of material in the industrial reactor.

[0101] In one embodiment, determining the non-condensable gas generation rate based on the non-condensable gas pressure change rate in step S102 above can be implemented as the following steps C1-C4:

[0102] In step C1, non-condensable gas is controlled to enter the venting material tank, wherein the venting material tank is connected to the non-condensable gas tank;

[0103] In step C2, the excess gas in the venting tank is discharged into the non-condensable gas tank by controlling the venting tank exhaust valve between the venting tank and the non-condensable gas tank, so that the pressure of the venting tank remains constant.

[0104] In step C3, the pressure change rate of the non-condensable gas tank is obtained;

[0105] In step C4, the noncondensable gas generation rate is determined based on the pressure change rate of the noncondensable gas tank.

[0106] In this embodiment, non-condensable gas is controlled to enter a venting material tank, wherein the venting material tank is connected to a non-condensable gas tank. Figure 2 As shown, the system is purged and pressurized with nitrogen before the experiment begins; the condensable vapor in the vented material is converted into condensate and enters the vented material tank 204 together with the non-condensable gas. The vented material tank 204 is connected to the non-condensable gas tank 211 through the vented material tank exhaust valve 210.

[0107] During the experiment, the pressure in the venting material tank was kept constant by controlling the exhaust valve of the venting material tank between the venting material tank and the non-condensable gas tank. Excess gas in the venting material tank was completely discharged into the non-condensable gas tank, thus maintaining a constant pressure in the venting material tank. The pressure in the venting material tank was measured in real time using a pressure sensor. Simultaneously, the pressure in the non-condensable gas tank was also measured in real time using a pressure sensor, allowing the acquisition of the pressure change rate in the non-condensable gas tank.

[0108] The noncondensable gas generation rate in an industrial reactor is determined based on the pressure change rate of the noncondensable gas tank. Specifically, the noncondensable gas generation rate is determined using the following formula:

[0109]

[0110] Among them, w 不 t is the rate of noncondensable gas generation; P is the pressure of the noncondensable gas container; t is the reaction time; V is the volume of the noncondensable gas container; M 不 R is the average molecular weight of the noncondensable gas; T is the gas constant; m is the room temperature. edenoted as , where m is the mass of material in the pilot reactor at the initial moment; m is the mass of material in the industrial reactor.

[0111] In one embodiment, step S104 above can be implemented as steps D1-D3 as follows:

[0112] In step D1, the calculated values ​​of multiple flow capacities of the rupture disc are determined based on at least the set pressure of multiple venting tanks and the material temperature of the pilot reactor at the corresponding maximum gas phase venting rate point.

[0113] In step D2, multiple rupture disc sizes are determined based on the maximum gas phase release rate under the runaway reaction at the set pressure of the different release material tanks and the calculated value of the corresponding rupture disc flow capacity.

[0114] In step D3, the minimum value among the multiple rupture disc sizes is selected as the design size of the rupture disc.

[0115] In this embodiment, since the set pressure of the rupture disc should be less than or equal to the design pressure of the reactor, multiple pressure values ​​can be selected within the design pressure of the industrial reactor and the back pressure range of the venting pipeline as the control pressure of the venting material tank. Multiple tests are conducted, and the corresponding design size of the rupture disc is calculated sequentially. Then, the rupture disc sizes corresponding to different control pressures of the venting material tanks are compared, and the smallest rupture disc size is selected as the rupture disc for the industrial reactor. The corresponding maximum gas phase venting rate is the maximum gas phase venting rate of the industrial reactor. Using this rupture disc ensures that the reactor pressure will not exceed its design pressure during the venting process. The specific determination process is as follows:

[0116] The calculated values ​​of multiple flow capacities of the rupture disc are determined based on at least the set pressures of multiple venting tanks and the corresponding reaction vessel material temperatures at the maximum gas phase venting rate points. First, the outlet pressure and critical pressure of the rupture disc are determined. The critical pressure of the rupture disc is determined using the following formula:

[0117]

[0118] Among them, P cf P1 is the critical pressure of the rupture disc, P1 is the set pressure of the venting tank, and k is the average heat capacity ratio of non-condensable gas and condensable gas.

[0119] Simultaneously, based on the corresponding maximum gas phase venting rate and the venting pipeline resistance, the outlet pressure P of the rupture disc is calculated. d .

[0120] When the outlet pressure of the rupture disc is less than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0121]

[0122] Where G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, k is the average heat capacity ratio of non-condensable gas and condensable gas, M is the average molecular weight of non-condensable gas and condensable gas, R is the ideal gas constant, and T1 is the material temperature of the reaction vessel corresponding to the maximum rate point.

[0123] When the outlet pressure of the rupture disc is greater than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula:

[0124]

[0125] In the above formula, G is the flow capacity of the rupture disc, C0 is the correction coefficient, P1 is the set pressure of the venting tank, and P d denoted as rupture disc outlet pressure, k as the average heat capacity ratio of non-condensable gas and condensable gas, M as the average molecular weight of non-condensable gas and condensable gas, R as the ideal gas constant, and T1 as the material temperature of the reaction vessel corresponding to the maximum rate point.

[0126] Then, multiple rupture disc sizes are determined based on the maximum gas-phase release rate under runaway reactions at different set pressures and the calculated flow capacity of the corresponding rupture discs. Specifically, the rupture disc area is calculated using the following formula:

[0127]

[0128] Where A is the rupture disc venting area, W is the maximum gas phase venting rate of the reactor, and G is the flow capacity of the rupture disc.

[0129] Finally, the minimum value among the multiple rupture disc dimensions is selected as the design size of the rupture disc.

[0130] Figure 3 This is a schematic diagram of the hardware structure of a system for determining the size of a rupture disc according to an embodiment of this application, as shown below. Figure 3 As shown, the system for this rupture disc size includes:

[0131] At least one processor 320; and,

[0132] Memory 304 communicatively connected to the at least one processor 320; wherein,

[0133] The memory 304 stores instructions that can be executed by the at least one processor 320 to implement the method for rupture disc size as described in any of the above embodiments.

[0134] Reference Figure 3The system 300 of the rupture disc size may include one or more of the following components: processing component 302, memory 304, power supply component 306, multimedia component 308, audio component 310, input / output (I / O) interface 312, sensor component 314, and communication component 316.

[0135] Processing component 302 typically controls the overall operation of system 300, which controls the size of the rupture disc. Processing component 302 may include one or more processors 320 to execute instructions to complete all or part of the steps of the method described above. Furthermore, processing component 302 may include one or more modules to facilitate interaction between processing component 302 and other components. For example, processing component 302 may include a multimedia module to facilitate interaction between multimedia component 308 and processing component 302.

[0136] Memory 304 is configured to store various types of data to support the operation of the rupture disc-sized system 300. Examples of this data include instructions for any application or method operating on the rupture disc-sized system 300, such as text, images, videos, etc. Memory 304 can be implemented by any type of volatile or non-volatile storage device or a combination thereof, such as static random access memory (SRAM), electrically erasable programmable read-only memory (EEPROM), erasable programmable read-only memory (EPROM), programmable read-only memory (PROM), read-only memory (ROM), magnetic storage, flash memory, magnetic disk, or optical disk.

[0137] Power supply assembly 306 provides power to various components of the rupture disc-sized system 300. Power supply assembly 306 may include a power management system, one or more power supplies, and other components associated with generating, managing, and distributing power to the vehicle control system 300.

[0138] Multimedia component 308 includes a screen that provides an output interface between the rupture-sized system 300 and the user. In some embodiments, the screen may include a liquid crystal display (LCD) and a touch panel (TP). If the screen includes a touch panel, the screen may be implemented as a touchscreen to receive input signals from the user. The touch panel includes one or more touch sensors to sense touches, swipes, and gestures on the touch panel. The touch sensors may sense not only the boundaries of touch or swipe actions but also the duration and pressure associated with the touch or swipe operation. In some embodiments, multimedia component 308 may also include a front-facing camera and / or a rear-facing camera. When the rupture-sized system 300 is in an operating mode, such as a shooting mode or a video mode, the front-facing camera and / or rear-facing camera may receive external multimedia data. Each front-facing camera and rear-facing camera may be a fixed optical lens system or have focal length and optical zoom capabilities.

[0139] Audio component 310 is configured to output and / or input audio signals. For example, audio component 310 includes a microphone (MIC) configured to receive external audio signals when the rupture scale system 300 is in an operating mode, such as alarm mode, recording mode, voice recognition mode, and voice output mode. The received audio signals may be further stored in memory 304 or transmitted via communication component 316. In some embodiments, audio component 310 also includes a speaker for outputting audio signals.

[0140] I / O interface 312 provides an interface between processing component 302 and peripheral interface modules, such as keyboards, click wheels, buttons, etc. These buttons may include, but are not limited to, home buttons, volume buttons, power buttons, and lock buttons.

[0141] Sensor assembly 314 includes one or more sensors for providing status assessments of various aspects of the rupture disc size system 300. For example, sensor assembly 314 may include a sound sensor. Additionally, sensor assembly 314 may detect the on / off state of the rupture disc size system 300, the relative positioning of components (e.g., the display and keypad of the rupture disc size system 300), and the operational state of the rupture disc size system 300 or a component thereof (e.g., the operational state of the air distribution plate, structural state, discharge scraper, etc.), the orientation or acceleration / deceleration of the rupture disc size system 300, and temperature changes of the rupture disc size system 300. Sensor assembly 314 may include a proximity sensor configured to detect the presence of nearby objects without any physical contact. Sensor assembly 314 may also include an optical sensor, such as a CMOS or CCD image sensor, for use in imaging applications. In some embodiments, sensor assembly 314 may also include an accelerometer, a gyroscope, a magnetometer, a pressure sensor, a material buildup thickness sensor, or a temperature sensor.

[0142] Communication component 316 is configured to enable the rupture disc-sized system 300 to provide wired or wireless communication capabilities with other devices and cloud platforms. The rupture disc-sized system 300 can access wireless networks based on communication standards, such as WiFi, 2G, or 3G, or combinations thereof. In one exemplary embodiment, communication component 316 receives broadcast signals or broadcast-related information from an external broadcast management system via a broadcast channel. In one exemplary embodiment, communication component 316 also includes a near-field communication (NFC) module to facilitate short-range communication. For example, the NFC module may be implemented based on radio frequency identification (RFID) technology, Infrared Data Association (IrDA) technology, ultra-wideband (UWB) technology, Bluetooth (BT) technology, and other technologies.

[0143] In an exemplary embodiment, the fragmentation dimensional system 300 may be implemented by one or more application-specific integrated circuits (ASICs), digital signal processors (DSPs), digital signal processing devices (DSPDs), programmable logic devices (PLDs), field-programmable gate arrays (FPGAs), controllers, microcontrollers, microprocessors, or other electronic components to perform the fragmentation dimensional method described in any of the above embodiments.

[0144] This application also provides a computer-readable storage medium, which, when the instructions in the storage medium are executed by a processor corresponding to a rupture disc size determination system, enables the rupture disc size determination system to implement the rupture disc size determination method described in any of the above embodiments.

[0145] Those skilled in the art will understand that embodiments of this application can be provided as methods, systems, or computer program products. Therefore, this application can take the form of a completely hardware embodiment, a completely software embodiment, or an embodiment combining software and hardware aspects. Furthermore, this application can take the form of a computer program product implemented on one or more computer-usable storage media (including, but not limited to, disk storage and optical storage) containing computer-usable program code.

[0146] This application is described with reference to flowchart illustrations and / or block diagrams of methods, apparatus (systems), and computer program products according to embodiments of this application. It will be understood that each block of the flowchart illustrations and / or block diagrams, and combinations of blocks in the flowchart illustrations and / or block diagrams, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, special-purpose computer, embedded processor, or other programmable data processing apparatus to produce a machine, such that the instructions, which execute via the processor of the computer or other programmable data processing apparatus, generate instructions for implementing the flowchart... Figure 1 One or more processes and / or boxes Figure 1A device that provides the functions specified in one or more boxes.

[0147] These computer program instructions may also be stored in a computer-readable storage medium that can direct a computer or other programmable data processing device to function in a particular manner, such that the instructions stored in the computer-readable storage medium produce an article of manufacture including instruction means, which are implemented in a process Figure 1 One or more processes and / or boxes Figure 1 The function specified in one or more boxes.

[0148] These computer program instructions may also be loaded onto a computer or other programmable data processing equipment to cause a series of operational steps to be performed on the computer or other programmable equipment to produce a computer-implemented process, thereby providing instructions that execute on the computer or other programmable equipment for implementing the process. Figure 1 One or more processes and / or boxes Figure 1 The steps of the function specified in one or more boxes.

[0149] Obviously, those skilled in the art can make various modifications and variations to this application without departing from the spirit and scope of this application. Therefore, if such modifications and variations fall within the scope of the claims of this application and their equivalents, this application also intends to include such modifications and variations.

Claims

1. A method for determining the size of a rupture disc, characterized in that, include: When a runaway reaction occurs in the pilot reactor, the condensable and non-condensable gases produced in the pilot reactor are separated. The generation rate of condensable steam is determined based on the mass change rate of condensable steam, and the generation rate of non-condensable gas is determined based on the pressure change rate of non-condensable gas. The maximum gas phase venting rate of the industrial reactor is determined based on the generation rates of condensable and non-condensable gases in the pilot reactor. The design dimensions of the rupture disc of the industrial reactor are determined based on the maximum gas-phase venting rate under runaway reaction conditions.

2. The method as described in claim 1, characterized in that, The separation of condensable and non-condensable gases generated in the pilot reactor includes: The condensable and non-condensable gases generated in the reactor are cooled by a material venting cooling device. The condensate after cooling is controlled to enter the condensate container in order to separate condensable vapors and non-condensable gases.

3. The method as described in claim 2, characterized in that, The determination of the condensable steam generation rate based on the mass change rate of condensable steam includes: The rate of change of condensate mass is obtained by a weighing device installed at the bottom of the condensate container. The rate of condensable vapor generation is calculated based on the mass change rate of the condensate.

4. The method as described in claim 1, characterized in that, The determination of the noncondensable gas generation rate based on the pressure change rate of the noncondensable gas includes: Non-condensable gas is controlled to enter a release material tank, wherein the release material tank is connected to a non-condensable gas tank; By controlling the exhaust valve of the venting material tank between the venting material tank and the non-condensable gas tank, all excess gas in the venting material tank is discharged into the non-condensable gas tank, so that the pressure of the venting material tank remains constant. Obtain the pressure change rate of the non-condensable gas tank; The rate of noncondensable gas generation is determined based on the pressure change rate of the noncondensable gas tank.

5. The method as described in claim 1, characterized in that, The process of determining the design dimensions of the rupture disc of the industrial reactor based on the maximum gas-phase release rate under runaway reaction includes: The calculated values ​​of multiple flow capacities of the rupture disc are determined based on at least the set pressure of multiple venting tanks and the reaction vessel material temperature at the corresponding maximum gas phase venting rate point. The dimensions of multiple rupture discs are determined based on the maximum gas phase release rate under the set pressure of the multiple release material tanks and the calculated value of the corresponding flow capacity of the rupture discs. The minimum value among the multiple rupture disc dimensions is selected as the design dimension of the rupture disc.

6. The method as described in claim 5, characterized in that, The determination of the rupture disc's flow capacity based at least on the set pressure of multiple venting tanks and the reaction vessel material temperature corresponding to the maximum gas phase venting rate point includes: Determine the outlet pressure and critical pressure of the rupture disc; When the outlet pressure of the rupture disc is less than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula: ； in, To improve the circulation capacity of blasting fragments, For correction factor, To release the set pressure of the material tank, The ratio of the average heat capacity of non-condensable gases to condensable gases. The average molecular weight of non-condensable and condensable gases. Let be the ideal gas constant. This represents the temperature of the material in the reaction vessel corresponding to the point of maximum rate.

7. The method as described in claim 6, characterized in that, The critical pressure of the rupture disc is determined by the following formula: ； in, The critical pressure of the rupture disc. To release the set pressure of the material tank, This represents the average heat capacity ratio of non-condensable gas and condensable gas.

8. The method as described in claim 6, characterized in that, The method further includes: When the outlet pressure of the rupture disc is greater than the critical pressure, the flow capacity of the rupture disc is calculated according to the following formula: ； In the above formula, To improve the circulation capacity of blasting fragments, For correction factor, To release the set pressure of the material tank, To alleviate export pressure on rupture fragments, The ratio of the average heat capacity of non-condensable gases to condensable gases. The average molecular weight of non-condensable and condensable gases. Let be the ideal gas constant. This represents the temperature of the material in the reaction vessel corresponding to the point of maximum rate.

9. A system for determining the size of a rupture disc, characterized in that, include: At least one processor; as well as, A memory communicatively connected to the at least one processor; wherein, The memory stores instructions executable by the at least one processor to implement the method for determining the size of a rupture disc as described in any one of claims 1-8.

10. A computer-readable storage medium, characterized in that, When the instructions in the storage medium are executed by the processor corresponding to the rupture disc size determination system, the rupture disc size determination system is able to implement the rupture disc size determination method as described in any one of claims 1-8.

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