Safety monitoring system and method for methanol-to-olefin separation

Abstract

The invention belongs to the field of chemical intelligent equipment, and relates to the technical field of methanol-to-olefin, in particular to a safety monitoring system and method for methanol-to-olefin separation. One of the purposes of the invention is to provide a safety monitoring system for methanol-to-olefin separation. The safety monitoring system comprises: a stripping tower; the first detection module, the second detection module, the third detection module and the information processing module are in data connection with the first detection module, the second detection module and the third detection module. According to the technical scheme, the continuous safety detection system integrating real-time performance diagnosis and intelligent prediction regulation and control is provided for solving the key problems that in a methanol-to-olefin steam stripping separation system, the performance of a flash liquid heat exchanger declines in a hidden mode, early warning is difficult to conduct on system coupling failure, and a slowly-changing fault intervention window is lacked. Different from a traditional passive mode depending on temperature fluctuation alarm, the technical scheme realizes early degradation 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] The present invention belongs to the field of intelligent chemical equipment and relates to the technical field of methanol to olefins, and in particular to a safety monitoring system and method for methanol to olefins separation. Background Art

[0002] In the methanol-to-olefins (MTO) process, the stripping and separation system is a key step in achieving efficient methanol recovery and olefin product refining. This system typically consists of key equipment, including a stripping tower and a flash liquid heat exchanger. The stripping tower uses fresh steam at high temperature (approximately 402K) and a specific pressure (approximately 0.13MPa) to strip and separate a mixture of methanol, water, and light hydrocarbons. The goal is 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, tightly coupled to the stripping tower, recovers waste heat from the high-temperature wastewater to preheat the material stream circulating back into the system.

[0003] However, this system operates under complex conditions of high temperature, high pressure, a weakly acidic medium containing methanol, and multiphase flow, presenting significant safety risks. Trace amounts of formic acid can accelerate electrochemical corrosion of metal equipment (especially heat exchanger tubes), easily inducing stress corrosion cracking (SCC) in stainless steel tubes. A decrease in the stripping tower's separation efficiency directly leads to a surge in methanol concentration in the wastewater at the bottom of the tower, further exacerbating the corrosion rate of the heat exchanger. At the same time, the failure of heat exchange can disrupt the system's thermal balance, forcing a surge in steam usage in the stripping tower, significantly increasing energy costs and potentially inducing failures such as tower equipment flooding or downstream compressor liquid shock. A single unplanned shutdown can result in losses of up to millions of dollars, posing a persistent threat to the safe and stable operation of the entire unit.

[0004] Early monitoring of separation equipment primarily relied on threshold alarm systems for basic process variables (such as temperature, pressure, and flow), which could only respond to obvious, sudden faults. With technological advancements, the introduction of online analyzers (such as real-time monitoring of methanol concentration in stripping wastewater) and enhanced data integration capabilities of distributed control systems (DCSs) have enabled real-time monitoring of key separation efficiency indicators, partially improving the speed of response to process anomalies. In recent years, more advanced technologies, such as real-time monitoring of steam consumption (for example, CN201510628312.1, A Distributed Energy Efficiency Assessment Index System for Ethylene Production Processes) and online corrosion probe monitoring of equipment (CN200720149735.6, An Online Corrosion Monitoring Probe), have been applied. These technologies aim to identify potential risks by analyzing energy consumption data trends or equipment failure status. However, despite continuous advancements in monitoring methods, existing technology systems still face significant challenges. For example, online methanol analyzers often exhibit significant response delays (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 the core equipment—the stripping tower and the flash liquid heat exchanger. In particular, the real-time attenuation of the heat exchanger's heat transfer performance (such as the heat transfer coefficient U value), a key parameter, is rarely accurately captured and warned of in the conventional monitoring systems of existing plants.

[0005] Despite the continuous upgrading of safety monitoring technology, the mainstream safety detection methods currently used in methanol-to-olefin stripping and separation systems still have the problem of hidden degradation of key equipment performance being difficult to detect in a timely manner. For example, when the heat transfer efficiency of the flash liquid heat exchanger drops by more than 20% due to scaling or initial corrosion, the temperature change of its outlet logistics may be less than 3°C. This change often falls within the normal tolerance range of process control and cannot trigger an effective alarm. At this time, relying solely on traditional temperature monitoring is very likely to fail. At the same time, the downstream stripping tower has a certain degree of process adaptability. It 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 product methanol to meet the standard. This "masking" effect will further delay the identification of potential equipment failures.

[0006] Furthermore, due to the isolation of monitored parameters, while high-precision steam flow metering can clearly detect an abnormal increase in stripper steam consumption (perhaps as much as 5-10%), such safety monitoring methods often fail to establish a direct and clear causal relationship between this unambiguous energy consumption signal and the decline in heat transfer efficiency of upstream equipment. Manually capturing this phenomenon often leads to attributing the problem to common short-term disturbances (such as feed composition fluctuations), missing the optimal window for addressing the root cause. More critically, for equipment like flash liquid heat exchangers, which exhibit significant slow-degradation failure characteristics (e.g., a scaling layer can take weeks to accumulate from initial stage to critical failure), existing safety monitoring systems lack proprietary tools and algorithms for real-time performance assessment (such as heat load or scaling resistance calculations) and early warning. These blind spots mean that seemingly minor heat transfer efficiency declines (e.g., simple maintenance issues) cannot be quickly identified and addressed. This can ultimately lead to a series of consequences, such as complete heat exchanger blockage, forced bypass of high-methanol wastewater, and thermal shock-induced loss of control in the stripper, requiring equipment replacement and resulting in significant product errors and high losses.

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

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

[0009] Based on the above technical problems, one of the objectives of the present invention is to provide a safety monitoring system for methanol-to-olefin separation, which comprises: a stripping tower for separating light components in a liquid; a flash liquid heat exchanger connected to the stripping tower, which can provide heat for the separated liquid generated at the bottom of the stripping tower through heat exchange; a first detection module for passively triggering and collecting viscosity data related to the material transmitted from the flash liquid heat exchanger to the stripping tower; a second detection module for passively triggering and collecting data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger; a third detection module for actively triggering and partially or fully opening to obtain data related to the scaling factor of part or all areas of the flash liquid heat exchanger; and an information processing module for data connection with the first detection module, the third detection module, and the second detection module.

[0010] The information processing module is configured to:

[0011] Based on the viscosity data of the material transmitted 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 capacity 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 of the third detection module, a detection component related to the scaling factor in the area corresponding to the abnormal pressure data is actively triggered.

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

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

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

[0016] When the viscosity data of the material transmitted 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 capacity of the flash liquid heat exchanger transmitted by the second detection module both indicate that the operating condition of the flash liquid heat exchanger is abnormal, 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 comprises a viscosity detection component arranged 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 logistics of the flash liquid heat exchanger, a second temperature detection component for detecting the outlet temperature of the hot side logistics of the flash liquid heat exchanger, and a first flow detection component arranged on the hot side logistics of the flash liquid heat exchanger.

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

[0020] One of the objects of the present invention is also to provide a safety monitoring method for methanol to olefins separation, which comprises the following steps:

[0021] Based on the collected viscosity data of the material transmitted from the safety monitoring equipment to the downstream equipment and the data related to the instantaneous sensible heat exchange capacity of the flash liquid plus the heat exchanger, the operation of collecting the abnormal pressure data of the safety monitoring equipment is selectively triggered. Specifically, when the operation of collecting the abnormal pressure data of the safety monitoring equipment is triggered, based on the abnormal pressure data of the safety monitoring equipment, a detection operation related to the scaling factor in the area corresponding to the abnormal pressure data is actively triggered.

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

[0025] According to a preferred embodiment, the collection of viscosity data of the material transmitted from the safety monitoring device to the downstream device and data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger can periodically overlap in the collection time unit.

[0026] According to a preferred embodiment, when the viscosity data of the material transmitted from the flash liquid heat exchanger to the stripping tower and the data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger both indicate that the operating condition of the flash liquid heat exchanger is abnormal, 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 aims to solve 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. It proposes a continuous safety detection system that integrates real-time performance diagnosis and intelligent predictive control. Different from the traditional passive mode that relies on temperature fluctuation alarms, this technical solution realizes the early degradation perception of the flash liquid heat exchanger through the detection feedback of the stripping tower and the real-time feedback of the flash liquid heat exchanger, thereby reducing the loss volume of equipment. At the same time, this technical solution avoids the problem of data processing delays caused by redundant data processing during the accurate data collection process while maintaining accurate measurement through the active triggering of regional pressure detection and the reduction of regional detection range, promoting the maintenance strategy from "post-fault repair" to "predictive intervention", and realizing the effective management of slow-changing faults of complex equipment in the chemical industry. BRIEF DESCRIPTION OF THE DRAWINGS

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

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

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

[0032] Figure 4 It is a schematic diagram of the safety detection process set by the present invention;

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

[0034] Reference numerals

[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 gas compressor; 50: Spray tower; 60: Drying tower; 70: Crude product compressor; 80: Propylene separation tower. DETAILED DESCRIPTION

[0036] In the description of the present invention, terms are used for descriptive purposes only and should not be understood to indicate or imply relative importance or implicitly indicate the number of technical features indicated. In the description of the present invention, "plurality" means two or more, unless otherwise specifically defined.

[0037] The present invention is further described below with reference to specific examples. Experimental methods in the following examples, where specific conditions are not specified, generally follow conventional conditions or the conditions recommended by the manufacturer. Unless otherwise defined, all professional and scientific terms used herein have the same meanings as those familiar to professionals in the field. In addition, any methods and materials similar or equivalent to those described herein can be applied to the present invention. The preferred embodiments and materials described herein are for illustrative purposes only.

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

[0039] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments may be combined with each other.

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

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

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

[0043] The liquid phase components of the flash tank are sent to the flash liquid heat exchanger 100 for 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 serves as stripping steam and enters the stripping tower 200 at the middle or upper middle part of the stripping tower 200. The methanol-containing stripping steam obtained at the top of the stripping tower 200 can be assembled into process steam for a methanol-to-olefins (especially fixed-bed methanol-to-olefins) device 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] The gaseous components compressed by the flash gas compressor 40 are washed with water in the spray tower 50 and dried in the drying tower 60. The mixed gas is then compressed to 2.0 MPa by the crude product compressor 70 and sent to the propylene separation tower 80, where a preliminary separation of C2 and C3 is performed. Pure water is sprayed into the spray tower 50 from the top, absorbing most of the methanol in the tower and discharged from the bottom of the spray tower 50 and sent to the flash tank 30 for methanol separation. The methanol is further treated in the stripping tower 200 and sent to the olefin reactor for a circulation reaction.

[0045] The dried product (primarily carbon dioxide and water) is discharged from the bottom of the drying tower 60. The top of the propylene separation tower 80 contains C2 and lower hydrocarbons and non-condensable gases such as methane and hydrogen. These can be used for ethylene purification and separation to obtain high-purity ethylene products, or recycled to the reactor for disproportionation reaction to produce propylene products as by-products. The bottom of the propylene separation tower 80 contains mainly propylene (along with C4 and higher hydrocarbons), which can be sent to subsequent processes (such as olefin oligomerization to produce higher carbon hydrocarbons, C4 hydrocarbon alkylation to produce gasoline, olefin carbonylation or hydroformylation to produce aldehyde chemicals, etc.) without significantly affecting the product quality of subsequent processes. Alternatively, the product can be sent to the propylene refining tower for separation of high-purity propylene products.

[0046] During this process, it was found that directly monitoring the heat exchange capacity (eg, temperature) of the flash liquid heater 100 would result in the flash liquid heat exchanger 100 not being able to detect hidden dangers until serious functional defects or damage occurred.

[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 column 200 and a flash liquid heat exchanger 100 communicating with the stripping column 200 .

[0049] like Figure 5 As shown, the system further includes a first detection module 300. The first detection module 300 includes a viscosity detection component for detecting the viscosity of the inflowing liquid of 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 disposed at the bottom of the stripping tower 200. The viscosity detection component is, for example, a vibrating tube viscosity sensor, a capillary viscosity sensor, a rotary viscosity sensor, and the like.

[0050] The system also includes a second detection module 400. This module 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, to monitor 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 further includes a first flow detection component 410 disposed at the hot side logistics inlet and outlet of the flash liquid heat exchanger 100 .

[0052] The system further includes a third detection module 500. The third detection module 500 includes a pressure detection assembly 510. The third detection module 500 includes a first pressure detection assembly disposed on the hot side of the flash liquid heat exchanger 100 and a second pressure detection assembly 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 assemblies 510 for collecting pressure data of the cold-side logistics. The third detection module 500 also includes one or more second flow detection assemblies 520 for collecting flow data of the cold-side logistics of the flash liquid heat exchanger 100. The third detection module 500 also includes multiple third temperature detection assemblies 530 spaced apart at locations where the liquid flows through the flash liquid heat exchanger 100.

[0054] like Figure 3 As shown, multiple first pressure detection assemblies 5101 are evenly distributed throughout the hot-side flow pipeline of the flash liquid heat exchanger 100. Specifically, the first pressure detection assemblies 5101 are located at the water inlet and outlet of the hot-side flow pipeline. Each first pressure detection assembly 5101 monitors a corresponding pipeline area.

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

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

[0057] Those skilled in the art should understand that the information processing module 600 can be implemented in various ways.

[0058] The information processing module 600 of the present invention can be implemented by hardware circuits such as very large-scale integrated circuits, gate arrays, logic chips, transistors, field programmable gate arrays, programmable logic devices, etc., can also be implemented by software executed by various types of processors, or can be implemented by a combination of hardware circuits and software (such as firmware). These methods and devices can be implemented by 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 connected to the device system via a wired connection for confidentiality reasons to complete data transmission, processing, and instruction transmission. The information processing module 600 can also be connected wirelessly to the aforementioned detection components to remotely receive and process data in real time and send instructions or information to related devices. For example, it can send a device security assessment information report to a handheld terminal wirelessly connected to the information processing module 600.

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

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

[0062] The viscosity detection component set at the bottom of the stripping tower 200 collects the viscosity data V of the liquid flowing into the stripping tower 200 at intervals. out 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 provided on the hot side of the flash liquid heat exchanger 100 detects the temperature of the inflow at intervals T hot,in The second temperature detection component 430 provided on the hot side of the flash liquid heat exchanger 100 detects the outflow temperature T at intervals. hot,out 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 collects the hot side flow data at intervals. The data is transmitted in real time to the information processing module 600. The detection interval is, for example, 10 minutes, 20 minutes or 30 minutes.

[0065] The instantaneous sensible heat exchange capacity Q of the flash liquid heat exchanger 100 inst The calculation formula is as follows:

[0066]

[0067] Among them, Cp hot represents the specific heat capacity of the hot side stream (stripping wastewater) (kJ / (kg·K)); q inst Indicates instantaneous sensible heat exchange capacity (kW or kJ / h); T hot,in represents the real-time temperature of the hot side stream inflow of the flash liquid heater 100, in °C; T hot,out represents the real-time outflow temperature of the hot side stream of the flash liquid heater 100, in °C; is the hot side logistics flow rate, unit is (kg / h).

[0068] It should be noted that the specific heat capacity is determined by process simulation or historical analysis data. Preferably, a reference table of specific heat capacity is shown in Table 1 (the values ​​are set by the inventor based on the actual equipment conditions of the factory and in combination with the opinions of experts during equipment maintenance and repair).

[0069] Table 1

[0070] Furnace opening time (d) Specific heat capacity [kJ / (kg·K)] 0 4.2611 10 4.1616 20 4.1435

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

[0072] T1 Warning Information: |Q inst -Q design | / Q design >δ1;

[0073] T2 Warning Information: V out >V set ,

[0074] Among them, Qdesign represents the heat load (kW or kJ / h) of the flash liquid heat exchanger 100 under the design working condition; δ1 is the allowable deviation threshold of the design heat load of the flash liquid heater 100; V set Represents the set upper viscosity limit, in mPa·s. This value is directly related to the upper limit of methanol concentration allowed in the flow path at the bottom of stripping column 200 and is determined by actual production settings and requirements.

[0075] According to a preferred embodiment, the temperature sensor's testing intervals are aligned with those of the flash liquid heater 100, allowing the collected temperature data and viscosity data to periodically coincide. For example, for every test of the flash liquid heat exchanger 100, the temperature sensor is tested twice, with the second temperature sensor test time coinciding with the flash liquid heat exchanger 100 test time.

[0076] When neither the T1 warning information nor the T2 warning information appears, the flash liquid heat exchanger 100 operates normally.

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

[0078] Based on the evaluation result of the first detection, when T1 warning information and T2 warning information appear simultaneously, the information processing module 600 controls the pressure detection assembly 510 provided in the flash liquid heat exchanger 100 and the pipeline connecting the flash liquid heat exchanger 100 and the stripping column 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 of the corresponding area based on the detection result of the pressure anomaly.

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

[0081]

[0082]

[0083] Among them, A is the fitting constant, U clean,hot Indicates the heat load ratio of the clean state of the hot side stream of the flash liquid heat exchanger 100; U dirty,hot Indicates the real-time heat load ratio of the hot side stream of the flash liquid heat exchanger 100; H in,hotrepresents the enthalpy of the hot side stream inlet of the flash liquid heat exchanger 100, which is given by Calculated; H out,hot represents the enthalpy of the hot side stream inlet of the flash liquid heat exchanger 100, which is given by Calculated; H in,cold represents the enthalpy of the cold side stream inlet of the flash liquid heat exchanger 100, which is given by Calculated; H out,cold represents the enthalpy value of the cold side stream outlet of the flash liquid heat exchanger 100, which is given by Calculated.

[0084] When the third temperature detection component 530 is located at the cold side of the flash liquid heat exchanger 100, the information processing module 600 calculates the scaling factor R based on the following formula (2): f,cold .

[0085]

[0086] Among them, B is the fitting constant, U clean,cold Indicates the heat load ratio of the clean state of the cold side stream of the flash liquid heat exchanger 100; U dirty,cold Indicates the real-time heat load ratio of the cold side stream of the flash liquid heat exchanger 100.

[0087] The set thresholds of the fitting constants A and B and the fouling factor are adaptive adjustment parameters based on flash liquid heat exchangers 100 of different specifications, and are mainly set based on historical data.

[0088] When the fouling factor exceeds the set threshold, it indicates that the abnormal operating condition of the flash liquid heat exchanger 100 is caused by fouling and blockage in the area.

[0089] When the fouling factor does not exceed the set threshold, the flash liquid heat exchanger 100 may be damaged.

[0090] Based on the evaluation result of the fouling factor, the information processing module 600 can send a higher level alarm to the personal terminal of the corresponding equipment maintenance personnel.

[0091] For example, when the scaling factor exceeds a set threshold, the information processing module 600 simultaneously sends corresponding warning information to the personal terminal 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 synchronizes with the flash heat exchanger 100 to send instructions to shut down the corresponding flash liquid heat exchanger 100 (shutdown for cleaning) and / or activate the backup heat exchange equipment.

[0092] Furthermore, when the secondary detection is triggered, the information processing module 600 can perform advance authorization, that is, based on the confirmation of the corresponding person in charge, when the fouling factor of 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 separation and purification of methanol and olefins that meet the standards by reducing the flow rate.

[0093] It should be noted that the above-described specific embodiments are illustrative only. Those skilled in the art may devise various solutions based on the disclosure of the present invention, and such solutions fall within the scope of the present invention and are intended to be protected by the present invention. Those skilled in the art should understand that the present description and its accompanying drawings are intended to be illustrative only and are not intended to limit the scope of the claims. The scope of protection of the present 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 tower (200) for separating light components from the liquid; a flash liquid heat exchanger (100) in communication with the stripping tower (200), capable of providing heat to the separated liquid generated at the bottom of the stripping tower (200) by heat exchange; A first detection module (300) is passively triggered to collect viscosity data of a substance transmitted from the flash liquid heater (100) to the stripping tower (200); A second detection module (400) collects data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger (100) under passive triggering; A third detection module (500) is actively triggered to partially or fully open to obtain data related to scaling factors in a part or all areas of the flash liquid heater (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 to: Based on the viscosity data of the material 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 capacity 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 of the third detection module (500), a detection component related to the scaling factor in the area corresponding to the abnormal pressure data is actively triggered.

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

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

4. The safety monitoring system according to claim 1, characterized in that: The information processing module (600) is configured to: When the viscosity data of the material transmitted from the flash liquid heater (100) to the stripping tower (200) transmitted by the first detection module (300) and the data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger (100) transmitted by the second detection module (400) both indicate that the operating condition of the flash liquid heat exchanger (100) is abnormal, 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) comprises a viscosity detection component arranged at the bottom of the stripping tower (200).

6. The safety monitoring system according to claim 7, characterized in that: The second detection module (400) comprises a first temperature detection component (420) for detecting the inlet temperature of the hot side logistics of the flash liquid heat exchanger (100), a second temperature detection component (430) for detecting the outlet temperature of the hot side logistics of the flash liquid heat exchanger (100), and a first flow detection component (410) arranged on the hot side logistics of the flash liquid heat exchanger (100).

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

8. A safety monitoring method for methanol to olefins separation, characterized in that: The following steps are involved: Based on the collected viscosity data of the material transmitted from the safety monitoring device to the downstream device and the data related to the instantaneous sensible heat exchange capacity of the flash liquid heat exchanger (100), the operation of collecting abnormal pressure data of the safety monitoring device is selectively triggered, wherein, When triggering the operation of collecting abnormal pressure data of the safety monitoring device, based on the abnormal pressure data of the safety monitoring device, a detection operation related to the scaling factor of the area corresponding to the abnormal pressure data is actively triggered.

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

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

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