Control method and device for industrial chain of producing acetylene from natural gas and computer equipment

Abstract

The invention relates to a control method and device of a natural gas-to-acetylene industry chain, computer equipment, a computer readable storage medium and a computer program product. The method comprises the following steps: in response to a cracking furnace bumping event of a natural gas-to-acetylene industry chain, determining respective operation states of a plurality of cracking furnaces in the natural gas-to-acetylene industry chain; determining the variable quantity of the cracking gas output by each cracking furnace according to the respective operation state of each cracking furnace and the gas quantity relation balance model corresponding to the cracking furnace; and based on the variation of the cracked gas, adjusting the working parameters of downstream processes of the acetylene cracking process to which each cracking furnace belongs in the industry chain of producing acetylene from natural gas. Wherein the operation state comprises a normal state and a bumping state; the cracking furnace bumping event is triggered under the condition that at least one cracking furnace is changed into a bumping state from a normal state; and the gas flow relation balance model is used for representing the relation between the input gas flow and the output gas flow of the cracking furnace. By adopting the method, the control effect can be improved.

Description

Technical Field

[0001] The present application relates to the field of automatic control technology, and in particular to a control method, device, computer equipment, computer-readable storage medium and computer program product for a natural gas to acetylene industry chain. Background Art

[0002] Acetylene is a very important product in the chemical industry. It is one of the raw materials for the preparation of BDO (1,4-butanediol). The natural gas partial oxidation process for acetylene is one of the more mature processes in recent years. The natural gas partial oxidation system for acetylene uses natural gas and oxygen as raw materials. The raw materials are first heated in a preheating furnace and then enter the cracking furnace. Oxidation and cracking reactions occur in the cracking furnace. The cracked gas enters the scrubbing tower for washing and cooling, and then enters the downstream process.

[0003] In actual applications, cracking furnace tripping incidents often occur, resulting in large changes in the gas supply volume of downstream processes. In traditional technologies, technicians manually adjust and control related parameters, and the control effect is subject to the personal experience of the staff. If the staff is inexperienced or the adjustment is not timely, it is easy to trigger the shutdown of the entire natural gas to acetylene industry chain, resulting in huge energy and material consumption losses. Therefore, the use of traditional technologies has the disadvantage of poor control effect. Summary of the invention

[0004] Based on this, it is necessary to provide a control method, device, computer equipment, computer-readable storage medium and computer program product for the natural gas to acetylene industry chain that can improve the control effect in response to the above technical problems.

[0005] In a first aspect, the present application provides a control method for a natural gas to acetylene industry chain. The method comprises:

[0006] In response to a cracking furnace tripping event in a natural gas-to-acetylene industry chain, determining the operating status of each of a plurality of cracking furnaces in the natural gas-to-acetylene industry chain; the operating status includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one of the cracking furnaces changes from a normal state to a tripping state;

[0007] Determine the change in the cracking gas outputted by each cracking furnace according to the respective operating states and input gas volumes of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace; the gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace;

[0008] Based on the change in the cracked gas, the operating parameters of the downstream process of the acetylene cracking process to which each cracking furnace in the natural gas to acetylene industry chain belongs are adjusted.

[0009] In a second aspect, the present application also provides a control device for the natural gas to acetylene industry chain. The device comprises:

[0010] An operation state determination module is used to determine the operation state of each of the plurality of cracking furnaces in the natural gas to acetylene industry chain in response to a cracking furnace tripping event in the natural gas to acetylene industry chain; the operation state includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one of the cracking furnaces changes from a normal state to a tripping state;

[0011] A cracking gas change amount determination module is used to determine the change amount of cracking gas outputted by each cracking furnace according to the respective operating states and input gas amounts of each cracking furnace and the gas amount relationship balance model corresponding to the cracking furnace; the gas amount relationship balance model is used to characterize the relationship between the input gas amount and the output gas amount of the cracking furnace;

[0012] The parameter adjustment module is used to adjust the working parameters of the downstream process of the acetylene cracking process of each cracking furnace in the natural gas to acetylene industry chain based on the change amount of the cracking gas.

[0013] In a third aspect, the present application further provides a computer device, wherein the computer device comprises a memory and a processor, wherein the memory stores a computer program, and the processor implements the steps of the above method when executing the computer program.

[0014] In a fourth aspect, the present application further provides a computer-readable storage medium having a computer program stored thereon, wherein the computer program implements the steps of the above method when executed by a processor.

[0015] In a fifth aspect, the present application further provides a computer program product, wherein the computer program product comprises a computer program, and when the computer program is executed by a processor, the steps of the above method are implemented.

[0016] The control method, device, computer equipment, computer-readable storage medium and computer program product of the natural gas to acetylene industry chain are responsive to the cracking furnace tripping event of the natural gas to acetylene industry chain, and determine the operating status of each of the multiple cracking furnaces in the natural gas to acetylene industry chain; determine the change in the cracking gas output by each cracking furnace according to the operating status of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace; and adjust the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain based on the change in the cracking gas. Among them, the operating status includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one cracking furnace changes from a normal state to a tripping state; the gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace. By adopting the above method, on the one hand, by real-time monitoring of the cracking furnace jump event, it is possible to respond to abnormal conditions in a timely manner and realize timely adjustment of the working parameters; on the other hand, through the pre-set gas volume relationship balance model, it is possible to accurately predict the change in the amount of cracking gas delivered by the cracking furnace to the downstream process when the jump event is triggered, and then adjust the working parameters of the downstream process based on the change, which can ensure that the adjusted working parameters match the amount of cracking gas delivered under the jump condition, which is conducive to improving the control effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] FIG1 is an application environment diagram of a control method for a natural gas to acetylene industry chain in one embodiment;

[0018] FIG2 is a schematic diagram of material flow in a natural gas to acetylene industry chain according to an embodiment;

[0019] FIG3 is a schematic flow diagram of a control method for a natural gas to acetylene industry chain in one embodiment;

[0020] FIG4 is a schematic diagram showing the yield gain of acetylene gas relative to natural gas at different oxygen ratios and preheating temperatures in one embodiment;

[0021] FIG5 is a schematic diagram showing the yield gain of synthesis gas relative to natural gas at different oxygen ratios and preheating temperatures in one embodiment;

[0022] FIG6 is a structural block diagram of a control device for a natural gas to acetylene industry chain in one embodiment;

[0023] FIG. 7 is a diagram showing the internal structure of a computer device in one embodiment.

[0024] Figure numerals: 1-cracking furnace; 2-cracking gas compressor; 3-cracking gas cabinet; 4-main scrubber; 5-methanol synthesis compressor; 6-conversion tower; 7-methanol synthesis tower; 8-acetylene product tower; 9-acetylene gas cabinet; 10-acetylene compressor; 11-BYD (1-4 butynediol) synthesis reactor; 12-BYD hydrogenation reactor; 13-main scrubber synthesis gas sent to methanol synthesis pressure control regulating valve; 14-synthesis gas sent to conversion process flow regulating valve; 15-formaldehyde flow regulating valve; FT1-synthesis gas sent to methanol synthesis in acetylene concentration process Flow meter; SIC1- frequency controller of cracking gas cabinet outlet compressor; LC1- liquid level monitor of cracking gas cabinet: PC1- outlet pressure monitor of main washing tower in acetylene concentration process; SIC2- frequency controller of methanol synthesis compressor; PC2- outlet pressure monitor of methanol synthesis compressor; PC3- outlet pressure monitor of acetylene compressor; AT1- hydrogen-carbon ratio monitor; SIC3- ​​frequency controller of acetylene compressor: SIC3- ​​pressure controller of acetylene gas sent to BYD synthesis; FC1- synthesis gas flow monitor; FC2- formaldehyde flow monitor. DETAILED DESCRIPTION

[0025] In order to make the purpose, technical solution and advantages of the present application more clearly understood, the present application is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present application and are not used to limit the present application.

[0026] The control method of the natural gas to acetylene industry chain provided in the embodiment of the present application can be applied in the application environment as shown in Figure 1. Among them, the terminal 102 communicates with the server 104 through a network. The communication network can be a wired network or a wireless network. Therefore, the terminal 102 and the server 104 can be directly or indirectly connected through a wired or wireless communication method. For example, the terminal 102 can be indirectly connected to the server 104 through a wireless access point, or the terminal 102 is directly connected to the server 104 through the Internet, and this application does not limit it here.

[0027] Among them, the terminal 102 can be, but is not limited to, various desktop computers, laptops, smart phones, tablet computers, Internet of Things devices and portable wearable devices. The Internet of Things devices can be smart speakers, smart TVs, smart air conditioners, smart car-mounted devices, etc. Portable wearable devices can be smart watches, smart bracelets, head-mounted devices, etc. The server 104 can be an independent physical server, or a server cluster or distributed system composed of multiple physical servers, or a cloud server that provides basic cloud computing services such as cloud services, cloud databases, cloud computing, cloud functions, cloud storage, network services, cloud communications, middleware services, domain name services, security services, CDN (Content Delivery Network), and big data and artificial intelligence platforms. The data storage system can store data that the server 104 needs to process. The data storage system can be set up separately, integrated on the server 104, or placed on the cloud or other servers.

[0028] It should be noted that the control method of the natural gas to acetylene industry chain in the embodiment of the present application can be executed by the terminal 102 or the server 104 alone, or by the terminal 102 and the server 104 together. Taking the case where the terminal 102 is executed alone as an example, in the process of controlling the natural gas to acetylene industry chain, the terminal 102: responds to the cracking furnace tripping event of the natural gas to acetylene industry chain, determines the operating status of each of the multiple cracking furnaces in the natural gas to acetylene industry chain; determines the change in the cracking gas output by each cracking furnace according to the operating status of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace; based on the change in the cracking gas, adjusts the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain. Among them, the operating state includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one cracking furnace changes from a normal state to a tripping state; the gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace.

[0029] The following is an introduction to the natural gas to acetylene industry chain.

[0030] In one embodiment, the natural gas to acetylene industry chain may specifically include an acetylene cracking process, an acetylene concentration process, a methanol synthesis process, a synthesis gas conversion process and a BYD reaction process. As shown in FIG2 , the acetylene cracking process is deployed with multiple cracking furnaces 1. The natural gas and oxygen preheated by the preheating furnace enter the cracking furnace 1 to undergo a cracking reaction to produce cracked gas. The cracked gas includes acetylene gas, synthesis gas and high-grade alkynes. Among them, the synthesis gas includes hydrogen, carbon monoxide, carbon dioxide and methane, and the purity of acetylene gas is as high as 99% or more. After the natural gas and oxygen enter the cracking furnace 1, the product is cracked gas, part of which enters the cracking gas cabinet 2 for storage, and part directly enters the cracking gas compressor 3 for compression. After compression, part of the cracked gas enters the main washing tower 4 of the acetylene concentration process to obtain synthesis gas, which is sent to the downstream methanol synthesis process. Part of the synthesis gas sent to the methanol synthesis process directly enters the methanol synthesis tower 7, and the other part is sent to the conversion tower 6 of the synthesis gas conversion process to produce hydrogen, which is supplied to BYD hydrogenation and adjusts the hydrogen-carbon ratio of methanol synthesis. The remaining gas from the main scrubber 4 enters the acetylene product tower 8 to obtain acetylene gas, a part of which enters the acetylene gas tank 9 for storage, and the other part is directly pressurized by the acetylene compressor 10 and sent to the BYD synthesis reactor 11 of the downstream BYD reaction process, where it reacts with formaldehyde in the BYD synthesis reactor 11 to produce BYD, and BYD reacts with hydrogen sent from the conversion tower 6 in the BYD hydrogenation reactor 12 to produce BDO. Among them, the liquid level LC1 of the cracking gas tank 2 can be controlled by the compressor frequency hand operator SIC1, and can be specifically controlled based on PID parameters.

[0031] By adopting the control method provided by the present application, the natural gas cracking furnace produces acetylene gas and synthesis gas for use in the downstream process. When the cracking furnace trips, the acetylene gas and synthesis gas required by the downstream process will suddenly change. The downstream load and the compressor speed are automatically matched according to the load after the acetylene gas and synthesis gas trip, so as to maintain the stability of the upstream and downstream. That is to say, based on the technical solution of the present application, when the natural gas to acetylene industry chain triggers the cracking furnace trip event, the working parameters of the downstream process of the acetylene cracking process can be adaptively adjusted without relying on human control and human experience, which is conducive to improving the working efficiency and control effect of the control process of the acetylene industry chain.

[0032] In one embodiment, as shown in FIG3 , a control method for a natural gas to acetylene industry chain is provided. The method may be executed by a computer device, and the computer device may be a terminal or a server as shown in FIG1 . In this embodiment, the method is applied to the terminal in FIG1 as an example for description, and the method includes the following steps:

[0033] Step S302, in response to a cracking furnace trip event in the natural gas to acetylene industry chain, determining the operating status of each of the plurality of cracking furnaces in the natural gas to acetylene industry chain.

[0034] The natural gas to acetylene industry chain refers to a series of process flows and industrial links for producing acetylene using natural gas as raw material. As mentioned above, the natural gas to acetylene industry chain can specifically include acetylene cracking process, acetylene concentration process, methanol synthesis process, synthesis gas conversion process and BYD reaction process.

[0035] A cracking furnace is a device used for hydrocarbon cracking reactions. Cracking furnace tripping refers to the phenomenon that the cracking furnace automatically stops running due to certain abnormal conditions during the production process. The reasons for the natural gas cracking furnace tripping may involve pressure overlimit, insufficient air volume or air pressure, solenoid valve power failure or oil pressure fluctuation, valve switching failure, early ignition, flameout and flame detection failure, and interlock confirmation. In practical applications, the cracking furnace tripping under abnormal conditions can prevent greater equipment damage or safety accidents. Furthermore, the operating status of the cracking furnace can include normal state and tripping state.

[0036] Specifically, the acetylene cracking process of the natural gas to acetylene industry chain can deploy multiple cracking furnaces, and when at least one cracking furnace changes from a normal state to a tripped state, a cracking furnace tripping event is triggered. Furthermore, the terminal can determine the operating status of each of the multiple cracking furnaces in the natural gas to acetylene industry chain in response to the cracking furnace tripping event.

[0037] Optionally, the terminal can use the interlocking signal of the acetylene cracking furnace, the valve state of the tail gas from the top of the acetylene cracking cooling tower to the cracking gas holder, and the valve state of the tail gas from the top of the acetylene cracking cooling tower to the flare to determine the tripping of the cracking furnace. The terminal can specifically deploy a distributed control system (DCS) to obtain the operating status of each cracking furnace. Exemplarily, a signal Ri, i.e., a tripping signal of the i-th column cracking furnace, can be established on the DCS side. The tripping signal can be determined based on the triggering situation and valve state of the interlocking signal of the i-th column. If the interlocking signal of the i-th column cracking furnace is triggered, and the valve to the cracking gas holder is closed and the valve to the flare is opened, then Ri=1, indicating that the i-th column cracking furnace is in a tripping state. Otherwise, Ri=0, indicating that the i-th column cracking furnace is in a normal operating state. The above signal can be used to monitor the operating state of each cracking furnace in real time, and when at least one cracking furnace changes from a normal state to a tripping state, the operating state of each cracking furnace can be determined in real time, so that the process parameters of the downstream process can be adjusted according to each operating state later.

[0038] Step S304, determining the change in the cracking gas outputted by each cracking furnace according to the operating status and input gas volume of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace.

[0039] Among them, the gas volume can be characterized by gas volume or gas flow rate. The gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace. The input gas volume can refer to the gas volume of the input natural gas; it can also refer to the gas volume of the input natural gas and oxygen respectively; it can also refer to the gas volume of the mixed gas of the input natural gas and oxygen. The output gas volume can include at least a part of the gas volume of cracking gas, acetylene gas, synthesis gas, etc. The cracking gas output by the cracking furnace includes acetylene gas, synthesis gas and higher alkynes. The change in the cracking gas output by the cracking furnace refers to the change in the cracking gas output by the acetylene cracking process of each cracking furnace to the downstream process. The change in the cracking gas can include the change in the acetylene gas in the cracking gas, the change in the synthesis gas in the cracking gas, or at least a part of the change in the cracking gas.

[0040] Optionally, the terminal can construct corresponding gas volume relationship balance models for the cracking gas or a type of gas contained in the cracking gas. Furthermore, the gas volume relationship balance models corresponding to each cracking furnace can be the same or different.

[0041] Specifically, for each cracking furnace, the terminal can construct a gas volume relationship balance model that can characterize the relationship between the input gas volume and the output gas volume of the cracking furnace. Furthermore, in the case of triggering a cracking furnace trip event, the terminal can determine the current gas volume of the cracking gas output by each cracking furnace according to the respective operating states and input gas volumes of each cracking furnace, and the gas volume relationship balance model corresponding to the cracking furnace. Then, the terminal can determine the change in the cracking gas output by each cracking furnace according to the current gas volume and the historical gas volume of the cracking gas output by each cracking furnace before the cracking furnace trip event is triggered.

[0042] In an optional embodiment, the operation status of each of the plurality of cracking furnaces includes the historical operation status before the cracking furnace car jump event is triggered, and the current operation status after the cracking furnace car jump event is triggered. In the case of this embodiment, the terminal can identify the target cracking furnace where the car jump event occurs from each cracking furnace according to the current operation status and historical operation status of each cracking furnace, and then determine the change amount of the cracking gas output by each cracking furnace according to the input gas volume and gas volume relationship balance model of the target cracking furnace.

[0043] In an optional embodiment, the gas volume balance model can be expressed as:

[0044] F1i=kij×Fi+△F1i

[0045] F2i=Kij×Fi+△F2i

[0046] F3i=F1i+F2i+△F3i

[0047] F1=

[0048] F2=

[0049] F3=

[0050] Among them, Fi represents the amount of natural gas input to the i-th cracking furnace; F1i represents the amount of acetylene gas produced by the i-th cracking furnace; F2i represents the amount of synthesis gas produced by the i-th cracking furnace; F3i represents the amount of cracking gas produced by the i-th cracking furnace; kij represents the yield gain of acetylene gas in the i-th cracking furnace relative to natural gas; Kij represents the yield gain of synthesis gas in the i-th cracking furnace relative to natural gas; △F1i, △F2i and △F3i ​​are correction coefficients respectively, among which △F3i ​​is the correction coefficient for advanced acetylene. n is the number of cracking furnaces in the natural gas to acetylene industry chain. F1 is the total amount of acetylene gas produced by the acetylene cracking process; F2 is the total amount of synthesis gas produced by the acetylene cracking process; F3 is the total amount of cracking gas produced by the acetylene cracking process. After calculation, the deviation of the above model is within ±500m 3 / h range to meet actual application needs.

[0051] Taking the case where all the cracking furnaces are in normal state before the cracking furnace trip event is triggered as an example, the change in acetylene gas corresponding to each cracking furnace can be expressed as: △F1= ; The change in synthesis gas corresponding to each cracking furnace can be expressed as: △F2= ×F2i; the change in the cracking gas corresponding to each cracking furnace can be expressed as: △F3= ×F3i.

[0052] Step S306, based on the change in the cracked gas, adjusting the working parameters of the downstream process of the acetylene cracking process of each cracking furnace in the natural gas to acetylene industry chain.

[0053] Among them, the downstream process of the acetylene cracking process may include the acetylene concentration process, the methanol synthesis process, the synthesis gas conversion process and the BYD reaction process. Specifically, the change in the gas volume output of the upstream acetylene cracking process will cause the gas volume load of the downstream process to change. Based on this, the terminal can predict the change in the gas volume load of the downstream process caused by the change in cracking gas according to the material flow between the various processes in the natural gas to acetylene industry chain, and then configure the corresponding downstream process with working parameters that match the predicted value of the gas volume load change, so as to avoid the interlocking shutdown of the industrial chain caused by the cracking furnace jumping.

[0054] Optionally, the terminal can determine the theoretical load value of the synthesis gas to the methanol synthesis process and the theoretical load value of the acetylene gas to the BYD synthesis process according to the relationship between the cracking gas volume, the cracking gas tank liquid level, the acetylene gas tank liquid level, the acetylene gas volume and the downstream synthesis gas material model under the cracking furnace tripping condition. Then, according to the theoretical load value of the synthesis gas to the methanol synthesis process, the outlet pressure of the methanol synthesis compressor is calculated to achieve automatic matching and adjustment of the compressor pressure and speed, and then the compressor anti-surge formula is used to predict the operating state of the working point after the tripping, which is used as the anti-surge feedforward signal of the methanol synthesis compressor to adjust the anti-surge in advance.

[0055] Optionally, the terminal may also calculate the amount of formaldehyde added that matches the theoretical load value of the acetylene gas to the BYD synthesis process, thereby achieving automatic matching and adjustment of the formaldehyde load.

[0056] Optionally, the terminal can also automatically match the load of the synthesis gas conversion process according to the relationship between the amount of hydrogen produced by the synthesis gas conversion process, the amount of hydrogen required for BYD hydrogenation and the hydrogen-to-carbon ratio of methanol synthesis; according to the changes in acetylene cracking tail gas and fresh synthesis gas, design variable PID control parameters, adaptively adjust the cracking gas cabinet liquid level and automatically adjust the acetylene concentration process main washing tower outlet pressure set value.

[0057] In short, the terminal can use the pre-built gas volume relationship balance model according to the abnormal operating conditions of the industrial chain to achieve adaptive adjustment of the load of each process after the acetylene cracking furnace jumps, minimize the impact of the jump on each process, reduce the risk of interlocking shutdown of the entire industrial chain due to acetylene cracking jumps, improve the level of automation, shorten the abnormal operating time, and reduce the economic losses from the jump and the intensity of internal operations.

[0058] In the control method of the above-mentioned natural gas to acetylene industry chain, in response to the tripping event of the cracking furnace in the natural gas to acetylene industry chain, the operating status of each of the multiple cracking furnaces in the natural gas to acetylene industry chain is determined; according to the operating status of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace, the change in the cracking gas output by each cracking furnace is determined; based on the change in the cracking gas, the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain are adjusted. Among them, the operating status includes a normal state and a tripping state; the tripping event of the cracking furnace is triggered when at least one cracking furnace changes from a normal state to a tripping state; the gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace. By adopting the above method, on the one hand, by real-time monitoring of the cracking furnace jump event, it is possible to respond to abnormal conditions in a timely manner and realize timely adjustment of the working parameters; on the other hand, through the pre-set gas volume relationship balance model, it is possible to accurately predict the change in the amount of cracking gas delivered by the cracking furnace to the downstream process when the jump event is triggered, and then adjust the working parameters of the downstream process based on the change, which can ensure that the adjusted working parameters match the amount of cracking gas delivered under the jump condition, which is conducive to improving the control effect.

[0059] In one embodiment, the control method of the natural gas to acetylene industry chain also includes: obtaining the intake parameters of each cracking furnace under the current operating state; for each cracking furnace, based on the gas yield gain matching the intake parameters of the cracking furnace, constructing a gas volume relationship balance model corresponding to the cracking furnace.

[0060] The gas inlet parameters include the oxygen ratio and the preheating temperature of the preheating furnace; the gas yield gain includes the yield gain of acetylene gas relative to natural gas, and the yield gain of synthesis gas relative to natural gas.

[0061] Specifically, the terminal can obtain the intake parameters of each cracking furnace in the current operating state, and query the yield gain of each cracking furnace according to each intake parameter. Then, for each cracking furnace, a gas volume relationship balance model corresponding to the cracking furnace is constructed based on the gas yield gain matching the intake parameters of the cracking furnace. Exemplarily, the terminal can construct a gas volume relationship balance model of acetylene gas relative to natural gas based on the yield gain of acetylene gas relative to natural gas; the terminal can also construct a gas volume relationship balance model of synthesis gas relative to natural gas based on the yield gain of synthesis gas relative to natural gas.

[0062] In an optional embodiment, the gas volume relationship balance model may include an acetylene gas model, a synthesis gas model, and a cracking gas model. Specifically, the terminal can analyze the relationship between the intake parameters and the respective revenue growth rates of acetylene gas and synthesis gas based on historical data, and then construct an acetylene gas model and a synthesis gas model. For the cracking gas model, it can be determined by data fitting. As shown in Figure 4, the yield gain of acetylene gas relative to natural gas at different oxygen ratios and preheating temperatures is 0.13-0.17 in terms of volume flow rate calculation range; as shown in Figure 5, the yield gain of synthesis gas relative to natural gas at different oxygen ratios and preheating temperatures is 1.5-1.9 in terms of volume flow rate calculation range. The applicable range of the above-mentioned revenue increment is: the load range of a single-row cracking furnace is 60%-120%, the oxygen ratio range is 0.52-0.58, and the preheating temperature range of a preheating furnace is 550-650°C.

[0063] For example, the acetylene gas model of the i-th cracking furnace can be expressed as: F1i=kij×Fi+△F1i; the synthesis gas model of the i-th cracking furnace can be expressed as: F2i=Kij×Fi+△F2i; the cracking gas model of the i-th cracking furnace can be expressed as: F3i=F1i+F2i+△F3i. After calculation, the deviation of the above model is within ±500m 3 / h range to meet actual application needs.

[0064] In the above embodiment, for each cracking furnace, a gas volume relationship balance model corresponding to the cracking furnace is constructed based on the gas yield gain that matches the intake parameters of the cracking furnace. This is equivalent to establishing a gas volume relationship balance model that matches the actual parameters of different cracking furnaces, which is conducive to improving the accuracy of the model.

[0065] In one embodiment, each cracking furnace is connected to a cracking gas cabinet; a portion of the cracking gas generated by each cracking furnace enters the cracking gas cabinet for storage, and a portion flows into the downstream process; the cracking gas includes synthesis gas; the change in the cracking gas includes the change in synthesis gas; and the downstream process includes an acetylene concentration process. In the case of this embodiment, based on the change in the cracking gas, the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain are adjusted, including: based on the change in synthesis gas, determining the first theoretical load value of the synthesis gas provided by the acetylene cracking process to the acetylene concentration process to which each cracking furnace belongs under the current operating state; determining the second theoretical load value of the synthesis gas provided by the cracking gas cabinet to the acetylene concentration process according to the proportion of synthesis gas in the cracking gas and the liquid level drop rate of the cracking gas cabinet; adjusting the outlet pressure of the main washing tower of the acetylene concentration process according to the difference between the theoretical load value of synthesis gas and the expected load value of synthesis gas.

[0066] Among them, the theoretical load value of syngas is the sum of the first theoretical load value and the second theoretical load value. The theoretical load value of syngas can characterize the ability of the acetylene cracking process to provide syngas to the downstream process when the cracking furnace jumps out. The expected load value of syngas refers to the syngas supply capacity that matches the working parameters before the downstream process is adjusted. The expected load value of syngas is determined based on the gas flow meter reading at the outlet of the main washing tower. The gas flow meter at the outlet of the main washing tower can be, for example, FT1 in Figure 2. It can be understood that due to the delay in the impact on the downstream process when the cracking furnace jumps out, the reading of FT1 after the main washing tower is concentrated can characterize the actual load value of the syngas before the jump out event occurs. The actual load value matches the working parameters before the cracking furnace jumps out. That is to say, the terminal can directly determine the gas flow meter reading at the outlet of the main washing tower as the expected load value of syngas; it can also be determined as the expected load value of syngas by superimposing an error value on the basis of the gas flow meter reading. The error value can be determined based on expert experience.

[0067] In actual application, as shown in Figure 2, part of the cracking gas produced by each cracking furnace enters the cracking gas cabinet for storage, and part flows into the downstream process. When the cracking furnace trip event is triggered, the amount of synthesis gas produced by the acetylene cracking process is reduced and cannot meet the needs of the downstream methanol synthesis process. At this time, the cracking gas in the cracking gas cabinet compensates for the reduced amount of synthesis gas to reduce the impact of the upstream trip event on the downstream process.

[0068] Specifically, on the one hand, the terminal can determine the first theoretical load value of the acetylene cracking process of each cracking furnace providing the syngas to the acetylene concentration process under the current operating state based on the change in the syngas. Optionally, the first theoretical load value can be expressed as: F2-△F2. On the other hand, the terminal can determine the second theoretical load value of the syngas provided by the cracking gas cabinet to the acetylene concentration process according to the proportion of syngas in the cracking gas and the liquid level drop rate of the cracking gas cabinet. Optionally, the second theoretical load value can be expressed as: Rs×T2×A. Among them, Rs refers to the proportion of syngas in the cracking gas, Rs=F2 / F3; T2 refers to the liquid level drop rate of the cracking gas cabinet; A refers to the liquid surface area of ​​the cracking gas cabinet. It can be understood that if T2 represents the liquid level drop rate of the cracking gas cabinet per unit time, then "Rs×T2×A" refers to the second theoretical load value of the syngas provided by the cracking gas cabinet to the acetylene concentration process per unit time.

[0069] After obtaining the first theoretical load value and the second theoretical load value, the terminal can determine the theoretical load value of the syngas in the acetylene enrichment process when the trip event is triggered by summing the two. After determining the theoretical load value of the syngas after the trip, the theoretical load value of the syngas can be transferred to the downstream process, and 10-30s of preparation time can be obtained for the parameter adjustment of the downstream process, which can better guide the downstream process to determine the adjustment rate according to the current working conditions, making the entire adjustment more stable and reducing the fluctuation of each unit of the device.

[0070] For the acetylene concentration process, the terminal can adjust the outlet pressure of the main washing tower of the acetylene concentration process according to the difference between the theoretical load value of the syngas and the expected load value of the syngas, so as to ensure that the outlet pressure of the main washing tower matches the tripping condition. The difference between the theoretical load value of the syngas and the expected load value of the syngas can be represented by the difference or ratio between the two, for example.

[0071] In an optional embodiment, the relationship between the difference between the theoretical syngas load value and the expected syngas load value and the main scrubber outlet pressure adjustment value can be expressed as:

[0072]

[0073] Among them, △P(t) is the change of the outlet pressure P of the main washing tower in the acetylene concentration process at time t; △F2(t) is the deviation between the theoretical load value of synthesis gas and the expected load value of synthesis gas at time t; P is the proportional band, P = 50 ~ 600, I is the integral time, I = 10 ~ 300s, D is the differential time, D = 1.2 ~ 6s.

[0074] In the above embodiment, according to the change amount of synthesis gas in the cracking gas after the tripping event and the liquid level drop rate of the cracking gas tank, the theoretical load value of the synthesis gas that can be obtained by the acetylene concentration process is determined, and further according to the difference between the theoretical load value of the synthesis gas and the expected load value of the synthesis gas, the outlet pressure of the main washing tower of the acetylene concentration process is adjusted, which can ensure that the outlet pressure of the main washing tower matches the tripping condition, thereby avoiding the interlocking reaction of the acetylene concentration process caused by the cracking furnace tripping event, which is conducive to further improving the control effect of the natural gas to acetylene industry chain.

[0075] In one embodiment, the control method of the natural gas to acetylene industry chain also includes: determining the cracking gas change rate based on the change in the cracking gas and the amount of cracking gas before the cracking furnace trip event is triggered; and controlling the liquid level drop rate of the cracking gas cabinet according to a control strategy that matches the change in the cracking gas.

[0076] Among them, the cracking gas change rate R can be expressed as: R=(△F3 / F3)×100. Specifically, the terminal can configure a variety of candidate control strategies and establish a corresponding relationship between the candidate control strategies and the cracking gas change rate. When the cracking furnace jump event is triggered, the terminal can calculate the cracking gas change rate caused by the jump event based on the change in the cracking gas and the amount of cracking gas before the cracking furnace jump event is triggered, and further select a control strategy that matches the cracking gas change rate from each candidate control strategy. Finally, according to the control strategy, the liquid level drop rate of the cracking gas cabinet is controlled.

[0077] Exemplarily, the terminal can be configured with 4 different PID control strategies. When R is 0-10%, P is 400-600, I is 600-1200s, and D is 0s; when R is 10-40%, P is 200-400s, I is 100-400s, and D is 0; when R is 40-70%, P is 100-200s, I is 50-100s, and D is 1-5s; when R is greater than 70%, P is 50-100s, I is 20-100s, and D is 5-10s; where P is the proportional band, I is the integral time, and D is the differential time. When the trip signal Ri=1 is triggered, the terminal can select the corresponding PID control parameters to control the liquid level drop rate of the cracking gas cabinet according to the cracking gas change rate under the current working conditions, so as to ensure that the liquid level drop rate matches the actual demand of the current working conditions. Furthermore, the terminal can also time for 1-5 minutes when the rate of change of the cracking gas tank liquid level is lower than 0.5% / min. If R remains unchanged during this period, the PID control parameter is restored to R in the range of 0-10%.

[0078] It should be noted that the liquid level drop rate of the cracking gas cabinet can be controlled by a conventional immutable PID mode, a variable PID mode, or a combination of the two modes. In one possible implementation, the variable PID control mode can be implemented through a bypass. Specifically, the cracking gas change rate can be introduced through the bypass, and according to the cracking gas change rate, a corresponding PID control strategy is selected from multiple candidate control strategies included in the variable PID mode control. In the event of bypass failure, the original immutable PID control mode is maintained.

[0079] In practical applications, the liquid level of the cracking gas cabinet is required to be controlled between 30% and 80%, which is controlled by the speed of the cracking gas compressor. The conventional control mode can only meet the control of slight load changes. For large load fluctuations under the tripping condition, the PID parameters have poor anti-interference ability to load fluctuations, and the adjustment effect is usually poor. In the above embodiment, by designing a variety of control strategies and using a control strategy that matches the cracking gas change rate under actual conditions to control the cracking gas cabinet, the control effect can be further improved.

[0080] In one embodiment, the downstream process also includes a methanol synthesis process. In the case of this embodiment, based on the change in the cracked gas, the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain are adjusted, and further include: adjusting the outlet pressure setting value of the compressor according to the change in the synthesis gas and the compressor inlet pressure of the methanol synthesis process before the cracking furnace trip event is triggered; determining the compressor parameter prediction value of the methanol synthesis process according to the change in the synthesis gas and the compressor parameters of the methanol synthesis process before the cracking furnace trip event is triggered; determining the anti-surge working point of the compressor according to the theoretical load value of the synthesis gas, the ratio of the outlet pressure prediction value to the outlet pressure setting value, and the ratio of the inlet temperature prediction value to the outlet temperature prediction value.

[0081] As mentioned above, the synthesis gas separated from the cracking gas will enter the methanol synthesis process. Due to the occurrence of the cracking furnace jump event, it is necessary to adjust the operating parameters of the formaldehyde synthesis compressor 5 accordingly to avoid the occurrence of an interlocking reaction. Specifically, the terminal can adjust the outlet pressure setting value of the compressor according to the change in the synthesis gas amount and the compressor inlet pressure of the methanol synthesis process before the cracking furnace jump event is triggered. Among them, the compressor inlet pressure can be read by a pressure monitor deployed at the inlet of the formaldehyde synthesis compressor 5, and the pressure monitor can be, for example, PC1 in Figure 2.

[0082] Optionally, the outlet pressure setting value Pi can be expressed as: Pi=Pio+Kpi×△F2, where △F2 is the change in synthesis gas; Pio is the compressor inlet pressure of the methanol synthesis process before the cracking furnace trip event is triggered; Kpi is the gain relationship between load and pressure, ranging from 0.00001 to 0.00005.

[0083] The terminal can also determine the predicted value of the compressor parameter of the methanol synthesis process according to the change in the synthesis gas and the compressor parameters of the methanol synthesis process before the cracking furnace jump event is triggered. Wherein, the compressor parameters include the compressor inlet temperature, the compressor outlet temperature and the compressor outlet pressure; the compressor parameter predicted value includes the inlet temperature predicted value, the outlet temperature predicted value and the outlet pressure predicted value. Exemplarily, the terminal can determine the predicted value of the inlet temperature of the methanol synthesis process according to the change in the synthesis gas and the compressor inlet temperature of the methanol synthesis process before the cracking furnace jump event is triggered; the terminal can also determine the predicted value of the outlet temperature of the methanol synthesis process according to the change in the synthesis gas and the compressor outlet temperature of the methanol synthesis process before the cracking furnace jump event is triggered; the terminal can also determine the predicted value of the outlet pressure of the methanol synthesis process according to the change in the synthesis gas and the compressor outlet pressure of the methanol synthesis process before the cracking furnace jump event is triggered.

[0084] In an optional embodiment, the predicted value of the inlet temperature, the predicted value of the outlet temperature and the predicted value of the outlet pressure can be expressed as:

[0085] Ti = Tio + Kti × △F2

[0086] To= Too+Kto×△F2

[0087] Po = Poo + Kpi × △F2

[0088] Among them, Ti represents inlet temperature containment; To represents outlet temperature prediction value; Po represents outlet pressure prediction value; Tio represents compressor inlet temperature before tripping; Too represents compressor outlet temperature before tripping; Poo represents compressor outlet pressure before tripping; Kti and Kto are the gain relationship between temperature and load, ranging from 0.000002 to 0.000006; Kpi is the gain relationship between load and pressure, ranging from 0.00001 to 0.00005.

[0089] Furthermore, the terminal can determine the anti-surge operating point of the compressor according to the theoretical syngas load value, the ratio of the outlet pressure prediction value to the outlet pressure setting value, and the ratio of the inlet temperature prediction value to the outlet temperature prediction value. Exemplarily, the anti-surge operating point can be expressed as:

[0090] WP=F2.T×(Po / Pi)×(Ti / To)

[0091] Wherein, F2.T is the theoretical load value of synthesis gas.

[0092] It can be understood that determining the anti-surge operating point is equivalent to predicting the anti-surge of the formaldehyde synthesis compressor. In the subsequent operation process, the terminal can compare the anti-surge operating point with the anti-surge line. If it is in the surge area, the feedforward is used to open the adjustment mode in advance. It can be adjusted specifically according to the compressor commissioning mode. If the commissioning mode is manual or semi-automatic, the anti-surge valve opening is adjusted in advance according to the anti-surge operating point; if the commissioning mode is fully automatic, the feedforward coefficient Ka is given according to the anti-surge operating point, ranging from 0.05-0.01, and the anti-surge valve and compressor speed are automatically adjusted in advance to achieve automatic control.

[0093] The synthesis gas separated from the acetylene concentration process is sent to the methanol synthesis process, which has high pressure requirements and requires stable control, otherwise it is easy to trigger the methanol synthesis interlock. The flow rate of synthesis gas sent to methanol synthesis can be controlled by PCI, and specifically, the dual PID control mode can be used. The deviation △F2(t) between the theoretical load value F2.T of the synthesis gas and the expected load value F2.N of the synthesis gas is introduced into the DCS configuration and configured into the PID parameters of the pressure controller. The conventional control still uses pressure control as the standard, and the pressure control PID parameters remain unchanged. The jump-out condition uses the flow deviation as the key factor of the controller adjustment rate, which can be better combined with the actual jump-out condition, and is combined with the cracking gas compressor to adjust the gas cabinet liquid level to adjust the synthesis gas flow rate, thereby ensuring the rapid and stable recovery of the downstream gas supply. Wait for △F2(t) to be lower than 100m 3 / h, then the time is 1-2 minutes, during which △F2(t) is always lower than 100m 3 / h, it returns to pressure PID parameter control.

[0094] In the above embodiment, anti-surge prediction is performed on the compressor of the methanol synthesis process according to the change in synthesis gas, which can realize feedforward anti-surge control, thereby avoiding the interlocking reaction of jumping in the methanol synthesis process, which is beneficial to further improve the control effect of the natural gas to acetylene industry chain.

[0095] In one embodiment, the cracked gas includes acetylene gas; the change in the cracked gas includes the change in the acetylene gas; the downstream process includes a synthesis gas conversion process and a BYD synthesis process; the synthesis gas conversion process is used to provide hydrogen to the BYD synthesis process. In the case of this embodiment, based on the change in the cracked gas, the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain are adjusted, including: based on the change in the acetylene gas, adjusting the amount of formaldehyde input to the BYD synthesis process; determining the synthesis gas amount threshold of the synthesis gas conversion process according to the minimum gas volume and hydrogen-carbon ratio range required by the BYD synthesis process, and the actual hydrogen-carbon ratio input to the synthesis gas conversion process before the cracking furnace trip event is triggered.

[0096] Specifically, the terminal can design the correspondence between the change in acetylene load and the amount of formaldehyde required for the BYD synthesis process, and then adjust the amount of formaldehyde input into the BYD synthesis process according to the change in post-acetylene load when the cracking furnace jump event is triggered, thereby achieving closed-loop adaptive regulation.

[0097] Optionally, the corresponding relationship between the change in acetylene load and the amount of formaldehyde required for the BYD synthesis process can be expressed as:

[0098] F4.T=Km×Rm×F1.T+△Fm

[0099] Among them, F4.T represents the amount of formaldehyde required for the BYD synthesis process; F1.T=F1-△F1, which represents the theoretical load value of acetylene gas under the jumping condition; △F1 represents the change in acetylene load caused by the jumping event; Rm is the acetylene concentration coefficient that needs to be maintained, and the specific value should be (1 / required concentration-1), and its value is basically fixed at 67%; Km is the proportional coefficient, and its value is relatively small between 0.01-0.05; △Fm is the set formaldehyde revision value.

[0100] Furthermore, the hydrogen-to-carbon ratio will fluctuate dramatically after the cracking furnace is tripped, which will have an adverse effect on methanol synthesis. Therefore, it is necessary to adaptively adjust the hydrogen-to-carbon ratio of methanol synthesis while ensuring the minimum amount of hydrogen required for the BYD hydrogenation process. This process requires controlling the syngas load of the syngas conversion process through the syngas volume threshold to ensure that it matches the configured carbon-to-hydrogen ratio range. Specifically, when the theoretical syngas load exceeds the syngas volume threshold, the operator is reminded to make manual adjustments.

[0101] In an optional embodiment, the theoretical syngas load F5.T can be expressed as:

[0102] F5.T=F5.N-k5×△F2

[0103] Among them, F5.N is the amount of synthesis gas in the synthesis gas conversion process before the jump, which can be determined by reading the reading of the gas flow meter FC1 at the time of the jump; k5 is the gain of the synthesis gas change amount to the synthesis gas load of the conversion process, ranging from 0.05-0.3; △F2 is the synthesis gas change amount.

[0104] In an optional embodiment, the required range of hydrogen-to-carbon ratio of the inlet gas is configured to be 4.0 to 4.5, and the synthesis gas volume threshold can be expressed as:

[0105] F5.T.min=[(4.0-Ro) / kr+F6.T.min] / Kt

[0106] F5.T.max=[(4.5-Ro) / kr+F6.T.min] / Kt

[0107] Among them, Ro is the hydrogen-carbon ratio before tripping, which can be determined based on the reading of the hydrogen-carbon ratio monitor AT1; kr is the gain of hydrogen volume to hydrogen-carbon ratio, ranging from 0.0001 to 0.0003; F5.T.min is the minimum synthesis gas demand of the synthesis gas conversion process, and F5.T.max is the maximum synthesis gas demand of the synthesis gas conversion process; F6.T.min is the minimum gas volume required for the BYD synthesis process, which can be deduced according to historical data under the condition that the hydrogen volume demand remains basically unchanged, that is, maintaining 9000-10000m3 / h of hydrogen under a BYD load of 30t / h, and so on; Kt is the gain of synthesis gas hydrogen production, ranging from 0.6 to 0.85.

[0108] Furthermore, the hydrogen-carbon ratio monitor AT1 can calculate the hydrogen-carbon ratio based on the amount of carbon monoxide, carbon dioxide and hydrogen. Most of its conversion load is manually adjusted according to the hydrogen-carbon ratio, and the conversion gas load is adjusted by the FC1 control valve. When the adaptive system is put into use and the jump signal is triggered, it is determined whether the set value of FC1 is between F5.T.min and F5.T.max. If it is not in this range, the set value of FC1 is assigned to F5.T.min to achieve automatic adjustment.

[0109] In the above embodiment, based on the change in the amount of cracking gas when the cracking furnace jump event occurs, the amount of formaldehyde input to the BYD synthesis process and the synthesis gas amount threshold of the synthesis gas conversion process are adjusted, so that the hydrogen-carbon ratio that can maintain methanol synthesis can be adjusted in time to ensure the minimum conversion load, improve the utilization efficiency and economic benefits of the synthesis gas, and thus further improve the control effect.

[0110] It should be noted that in the above control method, the entire regulation process can be based on the flow prediction of key components (such as acetylene gas, synthesis gas, etc.), and the flow change rate and target value are used as the link between the upstream and downstream. It is written into the original conventional control in conditional program mode. When the jump signal is triggered, the program judgment mode is triggered. According to the judgment content, different PID control parameters are selected, and the corresponding relevant matching flow is output. There is a problem of excessive deviation between the flow prediction and the actual value in this process, so the adaptive adjustment process is set to use and remove buttons. When the deviation between the predicted value and the actual value of the synthesis gas volume is greater than 1000m 3 / h, and the deviation between the predicted value and the actual value of acetylene gas volume is greater than 500m 3 / h, the model error is considered to be too large, and the entire adaptive adjustment scheme is removed, that is, the load forecast value no longer outputs data, and control is performed according to the original PID control strategy. In addition, the abnormal operating conditions are automatically removed. If the compressor current signal is abnormal, the main wash tower pressure, the methanol synthesis reactor pressure and temperature, the water vapor ratio is changed, the acetylene compressor and methanol synthesis compressor outlet pressure, BYD reactor pressure and temperature, BYD hydrogenation reactor pressure and temperature are overreported or underreported, the entire adaptive adjustment scheme is automatically removed, so that the load forecast value cannot output data, the original PID control strategy and valve opening are maintained, and the operator takes over the control.

[0111] It should be understood that, although the various steps in the flowcharts involved in the above-mentioned embodiments are displayed in sequence according to the indication of the arrows, these steps are not necessarily executed in sequence according to the order indicated by the arrows. Unless there is a clear explanation in this article, the execution of these steps does not have a strict order restriction, and these steps can be executed in other orders. Moreover, at least a part of the steps in the flowcharts involved in the above-mentioned embodiments can include multiple steps or multiple stages, and these steps or stages are not necessarily executed at the same time, but can be executed at different times, and the execution order of these steps or stages is not necessarily to be carried out in sequence, but can be executed in turn or alternately with other steps or at least a part of the steps or stages in other steps.

[0112] Based on the same inventive concept, the embodiment of the present application also provides a control device for a natural gas to acetylene industry chain for implementing the control method of the natural gas to acetylene industry chain involved above. The implementation scheme for solving the problem provided by the device is similar to the implementation scheme recorded in the above method, so the specific limitations in the embodiments of the control device for one or more natural gas to acetylene industry chains provided below can refer to the limitations of the control method for the natural gas to acetylene industry chain above, and will not be repeated here.

[0113] In one embodiment, as shown in FIG6 , a control device for a natural gas to acetylene industry chain is provided, comprising:

[0114] The operation state determination module 601 is used to determine the operation state of each of the plurality of cracking furnaces in the natural gas to acetylene industry chain in response to the cracking furnace tripping event in the natural gas to acetylene industry chain; the operation state includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one cracking furnace changes from a normal state to a tripping state;

[0115] The cracking gas change amount determination module 602 is used to determine the change amount of the cracking gas output by each cracking furnace according to the operation status and input gas amount of each cracking furnace and the gas amount relationship balance model corresponding to the cracking furnace; the gas amount relationship balance model is used to characterize the relationship between the input gas amount and the output gas amount of the cracking furnace;

[0116] The parameter adjustment module 603 is used to adjust the working parameters of the downstream process of the acetylene cracking process of each cracking furnace in the natural gas to acetylene industry chain based on the change in the cracking gas.

[0117] In one embodiment, each cracking furnace is connected to a cracking gas cabinet; a part of the cracking gas generated by each cracking furnace enters the cracking gas cabinet for storage, and a part flows into the downstream process; the cracking gas includes synthesis gas; the change amount of the cracking gas includes the change amount of synthesis gas; the downstream process includes an acetylene concentration process. In the case of this embodiment, the parameter adjustment module 603 is specifically used to: determine the first theoretical load value of the synthesis gas provided by the acetylene cracking process of each cracking furnace to the acetylene concentration process under the current operating state based on the change amount of synthesis gas; determine the second theoretical load value of the synthesis gas provided by the cracking gas cabinet to the acetylene concentration process according to the proportion of synthesis gas in the cracking gas and the liquid level drop rate of the cracking gas cabinet; adjust the outlet pressure of the main washing tower of the acetylene concentration process according to the difference between the theoretical load value of synthesis gas and the expected load value of synthesis gas; the theoretical load value of synthesis gas is the sum of the first theoretical load value and the second theoretical load value; the expected load value of synthesis gas is determined based on the gas flow meter reading at the outlet of the main washing tower.

[0118] In one of the embodiments, the control device of the natural gas to acetylene industry chain also includes a liquid level control module, which is used to: determine the cracking gas change rate based on the change in the cracking gas and the amount of cracking gas before the cracking furnace jump event is triggered; and control the liquid level drop rate of the cracking gas cabinet according to a control strategy that matches the change in the cracking gas.

[0119] In one embodiment, the downstream process also includes a methanol synthesis process. In the case of this embodiment, the parameter adjustment module 603 is specifically used to: adjust the outlet pressure setting value of the compressor according to the change in the synthesis gas and the compressor inlet pressure of the methanol synthesis process before the cracking furnace trip event is triggered; determine the compressor parameter prediction value of the methanol synthesis process according to the change in the synthesis gas and the compressor parameters of the methanol synthesis process before the cracking furnace trip event is triggered; the compressor parameters include the compressor inlet temperature, the compressor outlet temperature and the compressor outlet pressure; the compressor parameter prediction value includes the inlet temperature prediction value, the outlet temperature prediction value and the outlet pressure prediction value; determine the anti-surge working point of the compressor according to the theoretical load value of the synthesis gas, the ratio of the outlet pressure prediction value to the outlet pressure setting value, and the ratio of the inlet temperature prediction value to the outlet temperature prediction value.

[0120] In one embodiment, the cracking gas includes acetylene gas; the change in the cracking gas includes the change in the acetylene gas; the downstream process includes a synthesis gas conversion process and a BYD synthesis process; the synthesis gas conversion process is used to provide hydrogen to the BYD synthesis process. In the case of this embodiment, the parameter adjustment module 603 is specifically used to: adjust the amount of formaldehyde input to the BYD synthesis process based on the change in the acetylene gas; determine the synthesis gas amount threshold of the synthesis gas conversion process according to the minimum gas amount and hydrogen-carbon ratio range required by the BYD synthesis process and the actual hydrogen-carbon ratio input to the synthesis gas conversion process before the cracking furnace trip event is triggered.

[0121] In one of the embodiments, the control device of the natural gas to acetylene industry chain also includes a model building module, which is used to: obtain the intake parameters of each cracking furnace under the current operating state; for each cracking furnace, based on the gas yield gain matching the intake parameters of the cracking furnace, build a gas volume relationship balance model corresponding to the cracking furnace.

[0122] Each module in the control device of the above-mentioned natural gas to acetylene industry chain can be implemented in whole or in part by software, hardware and their combination. Each of the above-mentioned modules can be embedded in or independent of the processor in the computer device in the form of hardware, or can be stored in the memory of the computer device in the form of software, so that the processor can call and execute the operations corresponding to each of the above modules.

[0123] In one embodiment, a computer device is provided, which may be a terminal, and its internal structure diagram may be shown in FIG7. The computer device includes a processor, a memory, an input / output interface, a communication interface, a display unit, and an input device. The processor, the memory, and the input / output interface are connected via a system bus, and the communication interface, the display unit, and the input device are connected to the system bus via the input / output interface. The processor of the computer device is used to provide computing and control capabilities. The memory of the computer device includes a non-volatile storage medium and an internal memory. The non-volatile storage medium stores an operating system and a computer program. The internal memory provides an environment for the operation of the operating system and the computer program in the non-volatile storage medium. The input / output interface of the computer device is used to exchange information between the processor and an external device. The communication interface of the computer device is used to communicate with an external terminal in a wired or wireless manner, and the wireless manner can be implemented through WIFI, a mobile cellular network, NFC (near field communication) or other technologies. When the computer program is executed by the processor, a control method for a natural gas to acetylene industry chain is implemented. The display unit of the computer device is used to form a visually visible image, and can be a display screen, a projection device or a virtual reality imaging device. The display screen can be a liquid crystal display screen or an electronic ink display screen. The input device of the computer device can be a touch layer covered on the display screen, or a button, trackball or touchpad set on the computer device casing, or an external keyboard, touchpad or mouse, etc.

[0124] Those skilled in the art will understand that the structure shown in FIG. 7 is merely a block diagram of a partial structure related to the solution of the present application, and does not constitute a limitation on the computer device to which the solution of the present application is applied. The specific computer device may include more or fewer components than shown in the figure, or combine certain components, or have a different arrangement of components.

[0125] In one embodiment, a computer device is provided, including a memory and a processor, wherein a computer program is stored in the memory, and the processor implements the steps of any of the above method embodiments when executing the computer program.

[0126] In one embodiment, a computer-readable storage medium is provided, on which a computer program is stored. When the computer program is executed by a processor, the steps of any of the above method embodiments are implemented.

[0127] In one embodiment, a computer program product is provided, including a computer program, which implements the steps of any of the above method embodiments when executed by a processor.

[0128] It should be noted that the user information (including but not limited to user device information, user personal information, etc.) and data (including but not limited to data used for analysis, stored data, displayed data, etc.) involved in this application are all information and data authorized by the user or fully authorized by all parties, and the collection, use and processing of relevant data must comply with relevant laws, regulations and standards in the relevant regions and areas. In addition, the subject can choose not to authorize the subject information and related data, or refuse or conveniently refuse to push information, etc.

[0129] In this application, when collecting and processing relevant data during the instance application, the requirements of the laws and regulations of the relevant regions should be strictly followed to obtain the informed consent or separate consent of the personal information subject, and subsequent data use and processing should be carried out within the scope of authorization of the laws and regulations and the personal information subject.

[0130] Those skilled in the art can understand that all or part of the processes in the above-mentioned embodiment methods can be completed by instructing the relevant hardware through a computer program, and the computer program can be stored in a non-volatile computer-readable storage medium. When the computer program is executed, it can include the processes of the embodiments of the above-mentioned methods. Among them, any reference to the memory, database or other medium used in the embodiments provided in this application can include at least one of non-volatile and volatile memory. Non-volatile memory can include read-only memory (ROM), magnetic tape, floppy disk, flash memory, optical memory, high-density embedded non-volatile memory, resistive random access memory (ReRAM), magnetoresistive random access memory (MRAM), ferroelectric random access memory (FRAM), phase change memory (PCM), graphene memory, etc. Volatile memory can include random access memory (RAM) or external cache memory, etc. As an illustration and not limitation, RAM can be in various forms, such as static random access memory (SRAM) or dynamic random access memory (DRAM). The database involved in each embodiment provided in this application may include at least one of a relational database and a non-relational database. Non-relational databases may include distributed databases based on blockchains, etc., but are not limited to this. The processor involved in each embodiment provided in this application may be a general-purpose processor, a central processing unit, a graphics processor, a digital signal processor, a programmable logic device, a data processing logic device based on quantum computing, etc., but are not limited to this.

[0131] The technical features of the above embodiments may be combined arbitrarily. To make the description concise, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0132] The above-described embodiments only express several implementation methods of the present application, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the scope of the present application. It should be pointed out that, for a person of ordinary skill in the art, several variations and improvements can be made without departing from the concept of the present application, and these all belong to the protection scope of the present application. Therefore, the protection scope of the present application shall be subject to the attached claims.

Claims

1. A control method for a natural gas to acetylene industry chain, characterized in that: The method comprises: In response to a cracking furnace tripping event in a natural gas-to-acetylene industry chain, determining the operating status of each of a plurality of cracking furnaces in the natural gas-to-acetylene industry chain; the operating status includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one of the cracking furnaces changes from a normal state to a tripping state; Determine the change in the cracking gas outputted by each cracking furnace according to the respective operating states and input gas volumes of each cracking furnace and the gas volume relationship balance model corresponding to the cracking furnace; the gas volume relationship balance model is used to characterize the relationship between the input gas volume and the output gas volume of the cracking furnace; Based on the change in the cracked gas, the operating parameters of the downstream process of the acetylene cracking process to which each cracking furnace belongs in the natural gas to acetylene industry chain are adjusted.

2. The method according to claim 1, characterized in that Each of the cracking furnaces is connected to a cracking gas cabinet; a portion of the cracking gas generated by each of the cracking furnaces enters the cracking gas cabinet for storage, and a portion flows into a downstream process; the cracking gas includes synthesis gas; the change in the cracking gas includes the change in synthesis gas; the downstream process includes an acetylene concentration process; and adjusting the working parameters of the downstream process of the acetylene cracking process to which each of the cracking furnaces in the natural gas to acetylene industry chain belongs based on the change in the cracking gas includes: Based on the change in the synthesis gas, determining a first theoretical load value of the synthesis gas provided by the acetylene cracking process of each cracking furnace to the acetylene concentration process under the current operating state; Determining a second theoretical load value of the synthesis gas provided by the cracking gas holder to the acetylene concentration process according to the proportion of synthesis gas in the cracking gas and the liquid level drop rate of the cracking gas holder; The outlet pressure of the main washing tower of the acetylene concentration process is adjusted according to the difference between the theoretical load value of the synthesis gas and the expected load value of the synthesis gas; the theoretical load value of the synthesis gas is the sum of the first theoretical load value and the second theoretical load value; the expected load value of the synthesis gas is determined based on the gas flow meter reading at the outlet of the main washing tower.

3. The method according to claim 2, characterized in that The method further comprises: Determining a cracking gas change rate according to the change amount of the cracking gas and the amount of cracking gas before the cracking furnace trip event is triggered; The liquid level drop rate of the cracking gas cabinet is controlled according to a control strategy that matches the change in the cracking gas.

4. The method according to claim 2, characterized in that: The downstream process also includes a methanol synthesis process; and adjusting the working parameters of the downstream process of the acetylene cracking process to which each cracking furnace in the natural gas to acetylene industry chain belongs based on the change in the cracking gas also includes: According to the change in the synthesis gas and the compressor inlet pressure of the methanol synthesis process before the cracking furnace trip event is triggered, adjusting the outlet pressure setting value of the compressor; Determine the predicted value of the compressor parameter of the methanol synthesis process according to the change amount of the synthesis gas and the compressor parameters of the methanol synthesis process before the cracking furnace trip event is triggered; the compressor parameters include the compressor inlet temperature, the compressor outlet temperature and the compressor outlet pressure; the predicted value of the compressor parameter includes the predicted value of the inlet temperature, the predicted value of the outlet temperature and the predicted value of the outlet pressure; The anti-surge operating point of the compressor is determined according to the theoretical syngas load value, the ratio of the outlet pressure prediction value to the outlet pressure setting value, and the ratio of the inlet temperature prediction value to the outlet temperature prediction value.

5. The method according to claim 4, characterized in that The cracked gas includes acetylene gas; the change in the cracked gas includes the change in the acetylene gas; the downstream process includes a synthesis gas conversion process and a BYD synthesis process; the synthesis gas conversion process is used to provide hydrogen to the BYD synthesis process; The method of adjusting the working parameters of the downstream process of the acetylene cracking process of each cracking furnace in the natural gas to acetylene industry chain based on the change in the cracked gas comprises: Adjust the amount of formaldehyde input to the BYD synthesis process based on the change in acetylene gas; The synthesis gas volume threshold of the synthesis gas conversion process is determined according to the minimum gas volume and hydrogen-carbon ratio range required by the BYD synthesis process and the actual hydrogen-carbon ratio input into the synthesis gas conversion process before the cracking furnace trip event is triggered.

6. The method according to any one of claims 1 to 5, characterized in that The method further comprises: Obtaining the gas inlet parameters of each of the cracking furnaces under the current operating state; For each of the cracking furnaces, a gas volume relationship balance model corresponding to the cracking furnace is constructed based on a gas yield gain that matches the gas inlet parameters of the cracking furnace.

7. A control device for the natural gas to acetylene industry chain, characterized in that: The device comprises: An operation state determination module is used to determine the operation state of each of the plurality of cracking furnaces in the natural gas to acetylene industry chain in response to a cracking furnace tripping event in the natural gas to acetylene industry chain; the operation state includes a normal state and a tripping state; the cracking furnace tripping event is triggered when at least one of the cracking furnaces changes from a normal state to a tripping state; A cracking gas change amount determination module is used to determine the change amount of cracking gas outputted by each cracking furnace according to the respective operating states and input gas amounts of each cracking furnace and the gas amount relationship balance model corresponding to the cracking furnace; the gas amount relationship balance model is used to characterize the relationship between the input gas amount and the output gas amount of the cracking furnace; The parameter adjustment module is used to adjust the working parameters of the downstream process of the acetylene cracking process of each cracking furnace in the natural gas to acetylene industry chain based on the change amount of the cracking gas.

8. A computer device comprising a memory and a processor, wherein the memory stores a computer program, wherein: When the processor executes the computer program, the steps of the method according to any one of claims 1 to 6 are implemented.

9. A computer-readable storage medium having a computer program stored thereon, characterized in that: When the computer program is executed by a processor, the steps of the method according to any one of claims 1 to 6 are implemented.

10. A computer program product, comprising a computer program, characterized in that When the computer program is executed by a processor, the steps of the method according to any one of claims 1 to 6 are implemented.

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