A safety monitoring system and method for methanol to olefin separation

Abstract

The present application belongs to the field of chemical intelligent equipment, and relates to the field of methanol-to-olefin technology, in particular to a safety monitoring system and method for methanol-to-olefin separation. One of the purposes of the present application is to provide a safety monitoring system for methanol-to-olefin separation, which comprises a stripping tower, a first detection module, a second detection module, a third detection module and an information processing module (connected with the first detection module, the second detection module and the third detection module). The technical solution solves the key problems of hidden performance degradation of the flash liquid heat exchanger in the methanol-to-olefin stripping separation system, difficulty in early warning of system coupling failure and lack of intervention window for slow-changing faults, and proposes a continuous safety detection system combining real-time performance diagnosis and intelligent prediction and control. Unlike the passive mode of traditional temperature fluctuation alarm, the technical solution realizes early deterioration perception of the flash liquid heat exchanger through detection feedback of the stripping tower and real-time feedback of the flash liquid heat exchanger.

Description

Technical Field

[0001] This invention belongs to the field of intelligent chemical equipment, specifically the field of methanol-to-olefins technology, and particularly relates to a safety monitoring system and method for methanol-to-olefins separation. Background Technology

[0002] In the methanol-to-olefins (MTO) process, the stripping separation system is a crucial step in achieving efficient methanol recovery and olefin product refining. This system typically consists of main equipment such as a stripping tower and a flash liquid heat exchanger. The stripping tower uses fresh steam at high temperature (approximately 402 K) and a specific pressure (approximately 0.13 MPa) to strip a mixture containing methanol, water, and light hydrocarbons, aiming to recover over 99.99% of the methanol. The stripping wastewater discharged from the bottom of the tower requires further treatment or reuse. The flash liquid heat exchanger, closely coupled to the stripping tower, is responsible for recovering the waste heat from the high-temperature wastewater to preheat the material stream circulating back into the system.

[0003] However, the system operates under complex conditions of high temperature and pressure, weakly acidic media containing methanol, and multiphase flow, posing significant safety risks. Trace amounts of formic acid accelerate the electrochemical corrosion of metal equipment (especially heat exchanger tube bundles), easily inducing stress corrosion cracking (SCC) in stainless steel tube bundles. A decrease in the stripping tower's separation efficiency directly leads to a surge in methanol concentration in the bottom wastewater, further exacerbating the corrosion rate of the heat exchanger. Simultaneously, heat exchange failure can disrupt the system's thermal balance, forcing a spike in stripping tower steam consumption, significantly increasing energy costs, and potentially inducing flooding in the tower equipment or liquid slugging in downstream compressors. A single unplanned shutdown can result in losses of up to millions of dollars, posing a continuous threat to the safe and stable operation of the entire plant.

[0004] Early monitoring of separation equipment relied primarily on threshold alarm systems for basic process variables (such as temperature, pressure, and flow rate). These systems could only respond to explicit, sudden faults. With technological advancements, the introduction of online analyzers (such as real-time monitoring of methanol concentration in stripping wastewater) and the enhanced data integration capabilities of distributed control systems (DCS) have enabled real-time monitoring of key separation efficiency indicators, partially improving the response speed to process anomalies. In recent years, more advanced technologies such as real-time steam consumption monitoring (e.g., CN201510628312.1 A Distributed Energy Efficiency Evaluation Index System for Ethylene Production Processes) and online corrosion probe monitoring (CN200720149735.6 An Online Corrosion Monitoring Probe) have been applied, aiming to identify potential risks through the analysis of energy consumption data trends or equipment damage status. However, despite continuous progress in monitoring methods, existing technologies still face significant challenges. For example, the response of online methanol analyzers typically exhibits a significant delay (often exceeding 15 minutes), making it difficult to effectively prevent rapidly deteriorating corrosion processes. Existing technologies lack effective modeling and early warning capabilities for the failure coupling mechanism between core equipment—the stripping tower and the flash liquid heat exchanger; in particular, the key parameter of real-time degradation of heat exchanger heat transfer performance (such as the heat transfer coefficient U value) has almost failed to be accurately captured and warned of in the conventional monitoring system of existing plants.

[0005] Despite continuous upgrades in safety monitoring technology, current mainstream safety detection methods applied to methanol-to-olefins stripping separation systems still suffer from the problem of hidden degradation in the performance of critical equipment, making it difficult to detect in a timely manner. For example, when the heat transfer efficiency of the flash liquid heat exchanger decreases by more than 20% due to scaling or initial corrosion, the temperature change of its outlet stream may be less than 3°C. This change often falls within the normal tolerance range of process control and fails to trigger an effective alarm. In this case, relying solely on traditional temperature monitoring is highly likely to fail. Meanwhile, the downstream stripping tower possesses a certain degree of process self-adaptation capability, and can temporarily compensate for the impact of cold feed caused by insufficient heat exchange through internal adjustment mechanisms (such as increasing the reflux ratio or fine-tuning the operating pressure), temporarily maintaining the separation purity of the methanol product. This "masking" effect further delays the identification of potential equipment failures.

[0006] Furthermore, due to the isolation of monitoring parameters, although high-precision steam flow metering can clearly capture abnormal increases in stripping tower steam consumption (potentially by 5-10%), such safety detection methods often fail to establish a direct and clear causal relationship between this obvious energy consumption anomaly and the decline in heat exchange efficiency of upstream equipment. When this phenomenon is manually observed, the problem is often attributed to common short-term disturbances (such as fluctuations in feed composition), missing the optimal window for addressing the root cause. More importantly, for equipment like flash liquid heat exchangers, which exhibit significant slow-change failure characteristics (e.g., the scale layer may accumulate slowly from initial formation to critical failure over several weeks), existing safety monitoring systems lack proprietary tools and algorithms for real-time performance evaluation (such as heat load or scale thermal resistance calculation) and providing early warnings. These blind spots mean that a seemingly minor decline in heat exchange efficiency (requiring only simple repairs) cannot be quickly identified and addressed, potentially leading to a series of high-risk losses, such as complete heat exchanger blockage, forced bypass of high-methanol wastewater, and runaway stripping tower thermal shock, requiring equipment replacement and causing significant product errors.

[0007] Furthermore, on the one hand, there are differences in understanding among those skilled in the art; on the other hand, the inventors studied a large number of documents and patents when making this invention, but due to space limitations, not all details and contents were listed in detail. However, this does not mean that the present invention does not possess the features of these prior art. On the contrary, the present invention already possesses all the features of the prior art, and the applicant reserves the right to add relevant prior art to the background art. Summary of the Invention

[0008] This invention belongs to the field of intelligent chemical equipment, and in particular relates to a safety monitoring system and method for methanol-to-olefins separation.

[0009] Based on the aforementioned technical problems, one objective of this invention is to provide a safety monitoring system for methanol-to-olefins separation, comprising: a stripping tower for separating light components from a liquid; a flash liquid heat exchanger connected to the stripping tower, which provides heat to the separated liquid generated at the bottom of the stripping tower through heat exchange; a first detection module passively triggering the acquisition of viscosity data related to the substance transferred from the flash liquid heat exchanger to the stripping tower; a second detection module passively triggering the acquisition of data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger; a third detection module actively triggering the partial or complete activation of the third detection module to acquire data related to scaling factors in part or all areas of the flash liquid heat exchanger; and an information processing module connected to the first, third, and second detection modules.

[0010] The information processing module is configured as follows:

[0011] Based on the viscosity data of the substance transferred from the flash liquid heat exchanger to the stripping tower transmitted by the first detection module and the data related to the instantaneous sensible heat exchange rate of the flash liquid heat exchanger transmitted by the second detection module, the third detection module is selectively triggered, wherein...

[0012] Based on the abnormal pressure data from the third detection module, the detection components related to scaling factors in the corresponding area of ​​the abnormal pressure data are actively triggered.

[0013] According to a preferred embodiment, the third detection module includes a first pressure detection component disposed on the hot side of the flash liquid heat exchanger and a second pressure detection component disposed on the cold side of the flash liquid heat exchanger.

[0014] According to a preferred embodiment, the data acquisition of the first detection module and the second detection module can periodically overlap in terms of time units.

[0015] According to a preferred embodiment, the information processing module is configured as follows:

[0016] When the viscosity data transmitted by the first detection module related to the substance transferred from the flash liquid heat exchanger to the stripping tower and the data transmitted by the second detection module related to the instantaneous sensible heat exchange of the flash liquid heat exchanger both indicate that the flash liquid heat exchanger is in abnormal condition, the pressure detection component of the third detection module is actively triggered to start working.

[0017] According to a preferred embodiment, the first detection module includes a viscosity detection component disposed at the bottom of the stripping tower.

[0018] According to a preferred embodiment, the second detection module includes a first temperature detection component for detecting the inlet temperature of the hot-side stream of the flash liquid heat exchanger, a second temperature detection component for detecting the outlet temperature of the hot-side stream of the flash liquid heat exchanger, and a first flow detection component disposed on the hot-side stream of the flash liquid heat exchanger.

[0019] According to a preferred embodiment, the first flow detection component and the pressure detection component are disposed on the same side of the device they are detecting.

[0020] One of the objectives of this invention is to provide a safety monitoring method for methanol-to-olefins separation, which includes the following steps:

[0021] Based on the viscosity data of the substance transmitted from the safety monitoring equipment to the downstream equipment and the data related to the instantaneous sensible heat exchange of the flash liquid and the heat exchanger, the operation of collecting abnormal pressure data of the safety monitoring equipment is selectively triggered. Among them, when the operation of collecting abnormal pressure data of the safety monitoring equipment is triggered, the detection operation related to scaling factors in the corresponding area of ​​the abnormal pressure data is actively triggered based on the abnormal pressure data of the safety monitoring equipment.

[0022] According to a preferred embodiment, the safety monitoring equipment is a flash liquid heat exchanger, stripping tower, flash vapor compressor, spray tower, drying tower, or propylene separation tower.

[0023] According to a preferred embodiment, the downstream device of the stripping tower is a flash liquid heat exchanger.

[0024] According to a preferred embodiment, the downstream device of the spray tower is a drying tower.

[0025] According to a preferred embodiment, the acquisition of viscosity data of the substance transmitted by the safety monitoring equipment to downstream equipment and data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger can periodically overlap in the acquisition time unit.

[0026] According to a preferred embodiment, when both the viscosity data of the substance transferred from the flash liquid heat exchanger to the stripping tower and the data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger indicate an abnormal operating condition of the flash liquid heat exchanger, the pressure detection component is actively triggered to collect the pressure data of the flash liquid heat exchanger.

[0027] The beneficial effects of this technical solution are as follows:

[0028] This technical solution addresses the key challenges of insidious performance degradation of flash liquid heat exchangers in methanol-to-olefins stripping separation systems, difficulty in predicting system coupling failures, and the lack of intervention windows for gradual faults. It proposes a continuous safety monitoring system integrating real-time performance diagnosis and intelligent predictive control. Unlike traditional passive alarm systems that rely on temperature fluctuations, this solution achieves early detection of flash liquid heat exchanger degradation through detection feedback from the stripping tower and real-time feedback from the flash liquid heat exchanger, reducing equipment losses. Simultaneously, this solution utilizes proactive triggering of regional pressure detection and a narrower regional detection range. While maintaining accurate measurements, it avoids data processing delays caused by redundant data processing during precise data acquisition, driving a shift in maintenance strategies from "post-failure repair" to "predictive intervention," enabling effective management of gradual faults in complex equipment in the chemical industry. Attached Figure Description

[0029] Figure 1 This is a flow chart of the methanol-to-olefins separation process;

[0030] Figure 2 This is a schematic diagram showing the positional relationship between the first detection module and the stripping tower;

[0031] Figure 3 This is a schematic diagram showing the positional relationship between the third detection module and the flash liquid heat exchanger;

[0032] Figure 4 This is a schematic diagram of the security detection process set up in this invention;

[0033] Figure 5 This is a module configuration diagram of the present invention.

[0034] Figure Labels

[0035] 10: Olefin reactor outlet condenser; 20: Gas-liquid separator; 30: Flash tank; 100: Flash liquid heat exchanger; 200: Stripping tower; 300: First detection module; 400: Second detection module; 410: First flow detection component; 420: First temperature detection component; 430: Second temperature detection component; 500: Third detection module; 510: Pressure detection component; 5101: First pressure detection component; 520: Second flow detection component; 530: Third temperature detection component; 600: Information processing module; 40: Flash vapor compressor; 50: Spray tower; 60: Drying tower; 70: Crude product compressor; 80: Propylene separation tower. Detailed Implementation

[0036] In the description of this invention, terminology is used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. In the description of this invention, "a plurality of" means two or more, unless otherwise explicitly defined.

[0037] The present invention is further illustrated below with reference to specific embodiments. Experimental methods in the following embodiments, unless otherwise specified, are generally performed under conventional conditions or as recommended by the manufacturer. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. Furthermore, any methods and materials similar to or equivalent to those described herein may be applied to the methods of the present invention. The preferred embodiments and materials described herein are for illustrative purposes only.

[0038] The hardware portion of the technical solution of this invention can be implemented through dedicated logic; the software portion can be stored in memory and executed by an appropriate instruction execution system (such as a microprocessor or dedicated design hardware).

[0039] It should be noted that, unless otherwise specified, the embodiments and features described in the present invention can be combined with each other.

[0040] The process flow involved in this application uses the following equipment: olefin reactor outlet condenser 10, gas-liquid separator 20, flash tank 30, flash liquid heat exchanger 100, stripping tower 200, flash vapor compressor 40, spray tower 50, drying tower 60, crude product compressor 70 and propylene separation tower 80.

[0041] The process flow involved in this application includes the following steps:

[0042] like Figure 1As shown, the mixed gas containing methanol and other volatile organic compounds at the outlet of the olefin reactor (taking the methanol-to-propylene reactor as an example) cooled by the condenser 10 at the outlet of the olefin reactor first enters the gas-liquid separator 20. The liquid phase component of the gas-liquid separator 20 is further separated into gas and liquid phases by the flash tank 30. The gas phase component at the top of the flash tank 30 and the gas phase component at the top of the gas-liquid separator 20 are mixed and then sent to the flash compressor 40 for compression to 0.8 MPa.

[0043] The liquid phase component from the flash tank is sent to the flash liquid heat exchanger 100 for inter-stream heat exchange with the stripping wastewater generated at the bottom of the stripping tower 200, and then sent to the upper part of the stripping tower 200 for stripping operation. Fresh water vapor is used as stripping steam and enters the stripping tower 200 in the middle or upper part. The methanol-containing stripping steam obtained at the top of the stripping tower 200 can be used as process steam for methanol-to-olefins (especially fixed-bed methanol-to-olefins) units and sent to the olefin reactor for reaction. The stripping wastewater (containing ~100% water and methanol content <7 ppb) cooled by the flash liquid can be used as circulating water makeup or as boiler steam feed.

[0044] After being compressed by flash compressor 40, the gaseous components are washed with water in spray tower 50 and dried in drying tower 60. The mixed gas is then compressed to 2.0 MPa by crude product compressor 70 and sent to propylene separation tower 80 for preliminary C2-C3 separation. Pure water enters the spray tower 50 from the top and sprays it to absorb most of the methanol in the tower. The water is then discharged from the bottom of the spray tower 50 and sent to flash tank 30 for methanol separation. The methanol is then further processed by stripping tower 200 and sent to olefin reactor for recycling reaction.

[0045] The drying and removal products (mainly carbon dioxide and water) are discharged from the bottom of drying tower 60. The top of propylene separation tower 80 contains C2 and smaller hydrocarbons and non-condensable gases such as methane and hydrogen. It can be used for ethylene refining and separation to obtain high-purity ethylene products, or it can be recycled to the reactor for disproportionation reaction to produce propylene products as a byproduct. The bottom of propylene separation tower 80 contains mainly propylene (and also C4 and larger hydrocarbons). It can be sent to subsequent processes (such as high-carbon hydrocarbons as a byproduct of olefin oligomerization, gasoline as a byproduct of C4 hydrocarbon alkylation, aldehyde chemicals as a byproduct of olefin carbonylation or hydroformylation, etc.), which will not have a significant impact on the product quality of subsequent processes. It can also be sent to the propylene refining tower to separate high-purity propylene products.

[0046] In this process, it was found that directly monitoring the heat exchange capacity (e.g., temperature) of the flash liquid heat exchanger 100 would lead to the potential problems not being detected until the flash liquid heat exchanger 100 suffers serious functional defects or damage.

[0047] This embodiment provides a chemical safety monitoring system. This embodiment also relates to a delayed equipment damage identification system.

[0048] like Figure 5 As shown, the system includes a stripping tower 200 and a flash liquid heat exchanger 100 connected to the stripping tower 200.

[0049] like Figure 5 As shown, the system also includes a first detection module 300. The first detection module 300 includes a viscosity detection component for detecting the viscosity of the liquid flowing into the stripping tower 200 under passive triggering. The viscosity detection component is, for example, an online viscometer capable of acquiring data in real time. Figure 2 As shown, the online viscometer is installed at the bottom of the stripping tower 200. Viscosity detection components include, for example, vibrating tube viscosities, capillary viscosities, and rotary viscosities.

[0050] The system also includes a second detection module 400. The second detection module 400 is passively triggered to detect the inlet and outlet temperatures of the flash liquid heat exchanger 100. The second detection module 400 includes multiple temperature sensors. Preferably, based on the purpose of monitoring the heat exchange efficiency of the flash liquid heat exchanger 100, the second detection module 400 includes a first temperature detection component 420 for detecting the inlet temperature of the hot-side stream and a second temperature detection component 430 for detecting the outlet temperature of the hot-side stream.

[0051] The second detection module 400 also includes a first flow detection component 410 installed at the hot-side inlet and outlet of the flash liquid heat exchanger 100.

[0052] The system also includes a third detection module 500. The third detection module 500 includes a pressure detection component 510. The third detection module 500 includes a first pressure detection component disposed on the hot side of the flash liquid heat exchanger 100 and a second pressure detection component disposed on the cold side of the flash liquid heat exchanger 100.

[0053] Preferably, the third detection module 500 includes one or more pressure detection components 510 for the purpose of collecting pressure data of the cold-side material. The third detection module 500 also includes one or more second flow detection components 520 for the purpose of collecting flow data of the cold-side material in the flash liquid heat exchanger 100. The third detection module 500 also includes a plurality of third temperature detection components 530 spaced at intervals along the liquid flow path in the flash liquid heat exchanger 100.

[0054] like Figure 3 As shown, multiple first pressure detection components 5101 are evenly distributed in the pipeline of the hot-side flow of the flash liquid heat exchanger 100. In particular, the first pressure detection components 5101 are respectively installed at the inlet and outlet of the hot-side flow. Each first pressure detection component 5101 corresponds to the monitoring of a pipeline area.

[0055] The second flow detection component 520 and the pressure detection component 510 are located on the same side of the device they are detecting.

[0056] According to a preferred embodiment, the flow detection component and the pressure detection component 510 are disposed on the same side of the device they are detecting. Preferably, the flow detection component (e.g., the second flow detection component 520) and the pressure detection component 510 are disposed in parallel. Preferably, the first flow detection component 410 and the pressure detection component 510 are disposed on the same side of the device they are detecting. The flow detection component and the pressure detection component 510 are disposed on the same side of the cold-side logistics pipeline. Detection on the same side improves data detection accuracy.

[0057] Those skilled in the art will understand that the information processing module 600 can be implemented in a variety of ways.

[0058] The information processing module 600 of this invention can be implemented using hardware circuits such as very large-scale integrated circuits, gate arrays, logic chips, transistors, field-programmable gate arrays, and programmable logic devices, or using software executed by various types of processors, or a combination of hardware circuits and software (such as firmware). These methods and devices can be implemented using computer-executable instructions and / or contained in processor control code. For example, such code can be placed on a carrier medium such as a disk, CD, or DVD-ROM, a programmable memory such as read-only memory (firmware), or a data carrier such as an optical or electronic signal carrier.

[0059] The information processing module 600 can be wired to the device system for reasons such as security, to complete data transmission, processing, and command transmission. The information processing module 600 can also be wirelessly connected to the aforementioned detection components, and can remotely receive and process data in real time, sending commands or information to relevant devices. For example, it can send a device security assessment report to a handheld terminal wirelessly connected to the information processing module 600.

[0060] This embodiment provides a safety equipment monitoring method that combines high-frequency real-time passive triggering for primary detection with low-frequency high-precision active triggering for secondary detection.

[0061] like Figure 4 As shown, this method includes real-time detection-based primary data acquisition, regional screening-based secondary data acquisition, and targeted tertiary data acquisition.

[0062] A viscosity detection component installed at the bottom of the stripping column 200 intermittently collects viscosity data of the liquid flowing into the stripping column 200. The viscosity data collected by the first detection module 300 is transmitted to the information processing module 600 in real time.

[0063] The first temperature detection component 420, installed on the hot side of the flash liquid heat exchanger 100, intermittently detects the inflow temperature. A second temperature detection component 430, installed on the hot side of the flash liquid heat exchanger 100, intermittently detects the outflow temperature. The detection interval is, for example, 5 minutes, 10 minutes, or 15 minutes. The temperature data acquired by the temperature sensor is transmitted to the information processing module 600 in real time.

[0064] The first flow detection component 410 will intermittently collect hot-side material flow data. The data is transmitted in real time to the information processing module 600. The detection interval is, for example, 10 min, 20 min, or 30 min.

[0065] Instantaneous sensible heat exchange rate of flash liquid heat exchanger 100 The calculation formula is as follows:

[0066] …(1),

[0067] in, The specific heat capacity (kJ / (kg·K)) of the hot-side stream (stripping wastewater) is indicated. This indicates the instantaneous sensible heat exchange rate (kW or kJ / h). This indicates the real-time inflow temperature of the hot-side stream in the flash liquid heat exchanger 100, in °C. This indicates the real-time outflow temperature of the hot-side liquid from the flash liquid heat exchanger 100, in °C. This represents the flow rate of the hot-side material, expressed in kg / h.

[0068] It should be noted that the specific heat capacity is determined by process simulation or historical analysis data to obtain typical values. Preferably, the reference table for specific heat capacity is shown in Table 1 (this value was set by the inventor based on the actual equipment conditions of the plant and in conjunction with the opinions of experts during equipment maintenance and repair).

[0069] Table 1

[0070]

[0071] The information processing module 600 generates corresponding early warning information based on the following judgment formula.

[0072] T1 Warning Information: ;

[0073] T2 Warning Information: ,

[0074] in, This indicates the heat load (kW or kJ / h) of the flash liquid heat exchanger under design conditions. Design the allowable deviation threshold of heat load for flash liquid heat exchanger 100; This indicates the set upper limit of viscosity, in units of... This is directly related to the upper limit of the methanol concentration allowed in the bottom flow path of the stripping tower 200, and is determined by the settings and requirements in actual production.

[0075] According to a preferred embodiment, the detection interval of the temperature sensor is the same as the detection interval of the flash liquid heat exchanger 100, so that the collected temperature data and the collected viscosity data can periodically overlap in time. For example, after each detection of the flash liquid heat exchanger 100, the temperature sensor completes two detections, and the detection time of the second temperature sensor coincides with the detection time of the flash liquid heat exchanger 100.

[0076] When neither the T1 nor the T2 warning message appears, the flash liquid heat exchanger 100 is operating normally.

[0077] When a T1 warning or a T2 warning occurs alone, the information processing module 600 can send the relevant detection results to the personal terminal of the equipment maintenance personnel, who can then manually choose whether to trigger the next level of inspection.

[0078] Based on the evaluation results of the first test, when both T1 and T2 warning messages appear simultaneously, the information processing module 600 controls the pressure detection component 510 installed in the flash liquid heat exchanger 100 and its pipeline connected to the stripping tower 200.

[0079] Based on the detection results of the contact area of ​​the pressure detection component, such as Figure 3 As shown, the information processing module 600 can actively trigger the flow detection component and the third temperature detection component 530 in the corresponding area based on the detection result of pressure anomaly.

[0080] When the third temperature detection component 530 is located on the hot side of the flash liquid heat exchanger 100, the information processing module 600 calculates the scaling factor based on the following formula (2). .

[0081] (2)

[0082] …(3)

[0083] …(4)

[0084] Where A is the fitting constant, This represents the heat load ratio of the hot-side material in the clean state of the flash liquid heat exchanger 100. This represents the real-time heat load ratio of the hot-side stream in flash liquid heat exchanger 100. This represents the enthalpy value of the hot-side stream inlet of flash liquid heat exchanger 100, which is determined by ( Calculated; This represents the enthalpy value of the hot-side stream inlet of flash liquid heat exchanger 100, which is determined by ( Calculated; This represents the enthalpy value of the cold-side flow inlet of flash liquid heat exchanger 100, which is determined by ( Calculated; This represents the enthalpy value of the cold-side stream outlet of flash liquid heat exchanger 100, which is determined by ( Calculated.

[0085] When the third temperature detection component 530 is located on the cold side of the flash liquid heat exchanger 100, the information processing module 600 calculates the scaling factor based on the following formula (2). .

[0086] (5)

[0087] …(6)

[0088] Where B is the fitting constant, This represents the heat load ratio of the cold-side material in the clean state of the flash liquid heat exchanger 100. This indicates the real-time heat load ratio of the cold-side flow in flash liquid heat exchanger 100.

[0089] The fitting constants A and B, as well as the threshold values ​​for the scaling factor, are adaptive adjustment parameters based on different specifications of flash liquid heat exchangers 100, and are mainly set based on historical data.

[0090] When the scaling factor exceeds the set threshold, it indicates that the abnormal operating condition of the flash liquid heat exchanger 100 is caused by scaling and blockage in the area.

[0091] When the scaling factor does not exceed the set threshold, the flash liquid heat exchanger 100 may suffer equipment damage.

[0092] Based on the assessment results of scaling factors, the information processing module 600 can send higher-level alarms to the personal terminals of the relevant equipment maintenance personnel.

[0093] For example, when the scaling factor exceeds the set threshold, the information processing module 600 synchronously sends the corresponding warning information to the personal terminals of the person in charge of the equipment general management center and the person in charge of the flash liquid heat exchanger 100, and based on the authorization, it links with the flash liquid heat exchanger 100 to send the corresponding instructions to shut down (shut down for cleaning) and / or activate the backup heat exchange equipment.

[0094] Furthermore, when a secondary detection is triggered, the information processing module 600 can perform preliminary authorization. That is, based on the confirmation of the relevant person in charge, when the scaling factor in more than three actively triggered areas exceeds the set threshold, the system's operating power is reduced in real time (without waiting for manual instructions) to obtain methanol and olefins that meet the standards by reducing the flow rate.

[0095] It should be noted that the specific embodiments described above are exemplary, and those skilled in the art can devise various solutions inspired by the disclosure of this invention. These solutions all fall within the scope of this invention and its protection. Those skilled in the art should understand that this specification and its accompanying drawings are illustrative and not intended to limit the scope of the claims. The scope of protection of this invention is defined by the claims and their equivalents.

Claims

1. A safety monitoring system for methanol-to-olefins separation, characterized in that, Include: A stripping column (200) is used to separate light components from liquids; The flash liquid heat exchanger (100) connected to the stripping tower (200) can provide heat to the separated liquid generated at the bottom of the stripping tower (200) through heat exchange. The first detection module (300) passively triggers the acquisition of viscosity data of the substance transmitted from the flash liquid heat exchanger (100) to the stripping tower (200); The second detection module (400) passively triggers the acquisition of data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger (100); The third detection module (500) is actively triggered to partially or fully open in order to obtain data related to scaling factors in part or all areas of the flash liquid heat exchanger (100); The information processing module (600) is data-connected to the first detection module (300), the third detection module (500), and the second detection module (400); wherein, The information processing module (600) is configured as follows: Based on the viscosity data of the substance transmitted from the flash liquid heat exchanger (100) to the stripping tower (200) transmitted by the first detection module (300) and the data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger (100) transmitted by the second detection module (400), the third detection module (500) is selectively triggered, wherein, Based on the abnormal pressure data from the third detection module (500), the detection component related to the scaling factor in the corresponding area of ​​the abnormal pressure data is actively triggered. The detection component includes a flow detection component and a third temperature detection component (530). When the third temperature detection component (530) is located in the hot side of the flash liquid heat exchanger (100), the information processing module (600) calculates the scaling factor based on the following formula (2). , （2） …（3） …（4）， Where A is the fitting constant, This represents the heat load ratio of the hot-side material in the clean state of the flash liquid heat exchanger (100); This represents the real-time heat load ratio of the hot-side flow of the flash liquid heat exchanger (100); This represents the enthalpy value of the hot-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the hot-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the cold-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the cold-side stream outlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This refers to the flow rate of the hot-side material, expressed in kg / h. Specific heat capacity of the hot-side stream, expressed in kJ / kg·K.

2. The safety monitoring system according to claim 1, characterized in that, The third detection module (500) includes a first pressure detection component (5101) disposed on the hot side of the flash liquid heat exchanger (100) and a second pressure detection component disposed on the cold side of the flash liquid heat exchanger (100).

3. The safety monitoring system according to claim 1, characterized in that, The data acquisition of the first detection module (300) and the second detection module (400) can periodically overlap in terms of time units.

4. The safety monitoring system according to claim 1, characterized in that, The information processing module (600) is configured as follows: When the viscosity data transmitted by the first detection module (300) related to the substance transmitted from the flash liquid heat exchanger (100) to the stripping tower (200) and the data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger (100) transmitted by the second detection module (400) both indicate that the flash liquid heat exchanger (100) is in abnormal condition, the pressure detection component (510) of the third detection module (500) is actively triggered to start working.

5. The safety monitoring system according to claim 1, characterized in that, The first detection module (300) includes a viscosity detection component disposed at the bottom of the stripping tower (200).

6. The safety monitoring system according to claim 4, characterized in that, The second detection module (400) includes a first temperature detection component (420) for detecting the inlet temperature of the hot side of the flash liquid heat exchanger (100), a second temperature detection component (430) for detecting the outlet temperature of the hot side of the flash liquid heat exchanger (100), and a first flow detection component (410) disposed on the hot side of the flash liquid heat exchanger (100).

7. The safety monitoring system according to claim 6, characterized in that, The first flow detection component (410) and the pressure detection component (510) are located on the same side of the device they are detecting.

8. A safety monitoring method for methanol-to-olefins separation, characterized in that, Includes the following steps: Based on the collected viscosity data of the substance transmitted from the safety monitoring equipment to downstream equipment and the data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger (100), the operation of selectively triggering the collection of abnormal pressure data from the safety monitoring equipment is performed, wherein... When triggering the operation to collect abnormal pressure data from the safety monitoring equipment, based on the abnormal pressure data from the safety monitoring equipment, the detection operation related to scaling factors in the area corresponding to the abnormal pressure data is actively triggered, and the scaling factor is calculated based on the following formula (2). , （2） …（3） …（4）， Where A is the fitting constant, This represents the heat load ratio of the hot-side material in the clean state of the flash liquid heat exchanger (100); This represents the real-time heat load ratio of the hot-side flow of the flash liquid heat exchanger (100); This represents the enthalpy value of the hot-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the hot-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the cold-side flow inlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This represents the enthalpy value of the cold-side stream outlet of the flash liquid heat exchanger (100), which is determined by... Calculated; This refers to the flow rate of the hot-side material, expressed in kg / h. Specific heat capacity of the hot-side stream, expressed in kJ / kg·K.

9. The safety monitoring method according to claim 8, characterized in that, The acquisition of viscosity data of substances transmitted from safety monitoring equipment to downstream equipment and data related to the instantaneous sensible heat exchange of flash liquid heat exchanger (100) can periodically overlap in the acquisition time unit.

10. The safety monitoring method according to claim 8, characterized in that, When the viscosity data of the substance transferred from the flash liquid heat exchanger (100) to the stripping tower (200) and the data related to the instantaneous sensible heat exchange of the flash liquid heat exchanger (100) both indicate that the flash liquid heat exchanger (100) is in abnormal condition, the pressure detection component (510) is actively triggered to collect the pressure data of the flash liquid heat exchanger (100).

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