JP3058435B2 - Plant operation display - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION (Industrial Application Field)
Suitable when performing plant operation such as shutdown operation, emergency stop operation, etc. smoothly and reliably in actual equipment, or when performing these operations by simulating the plant by simulation to evaluate plant operation The present invention relates to a plant operation display device used for:

(Conventional technology and problems to be solved) A chemical plant is composed of a tower device such as a chemical reaction tank, a distillation column, and a heat exchanger, transport equipment, complicated piping, valves, and the like. Many are composed of components. The plant operation at the site of a chemical plant has been studied up to an extremely detailed operation and summarized in a work standard or the like. The entirety of these plant operations is usually considered based on three types of information:

First, the first information is information on the structure of the chemical plant. This information includes, for example, the type, height and position of the devices constituting the chemical plant, the connection status between the devices,
Equipment necessary for performing unsteady operations such as startup, the initial state of the plant, the final target state, and the like are included. The second information relates to a procedure for operating the device. The third information is information on timing for performing each procedure.

In the plant design, for example, the study of the plant operation procedure at the start-up is usually started when the basic design (basic flow sheet) is completed. This will be described with reference to FIG.
First, the designer decides the necessary piping design, pumps, main valves and other arrangements based on the operating procedure while keeping the operating procedure in mind. Next, the operation procedure of the startup is examined. However, there is a problem that the relation between the intention of the operation procedure of one designer and the design is often difficult for other designers to understand. In addition, since the plant designer and the operator are usually different, the concept of the operating procedure of the designer is not necessarily understood by the operator, and conversely, the concept of the operating procedure desired by the operator is not necessarily understood by the designer. There is a problem that there are many.

These problems are related to the fact that process design, operating procedures and their execution timing are closely related.
This is because there was no clear way to connect them. More importantly, such operation timing
Originally, it is desirable that the control system for plant operation is also registered in the distributed control system (DCS) and displayed sequentially on the display screen of the operation support equipment. The unclear expressions of the four relations such as the design and the operation procedure shown in FIG. 28 cause various problems.

For example, PFD (Process Flowsheet Diagra
m) and P & ID (Piping and Instrumentation Diagram)
Even if it is completed, it takes a lot of time and effort to express procedures such as startup and shutdown in a manual. The manual creation work has not yet been systematized, and the designer in charge has
The user confirms the operation procedure by tracing in order on the diagram. For this reason, an enormous amount of time is required, causing a problem that a user (especially, an operator) is extremely incomprehensible because there are errors or various expressions are used without unification. Further, conventionally, the work for converting a procedural expression into an operation support screen using a computer has been considered as a completely different work, and an enormous amount of labor and time have been spent on this conversion work.

In addition, chemical plants are often remodeled. In this case, it is necessary to consider changing operation procedures and execution timing at the same time. However, conventionally, it has not been possible to clearly express the changed portion of the plant equipment and the changed portion of the operating procedure to be changed correspondingly, so enormous labor and time are required to accurately perform the change work. Was needed. In such a case, it is necessary to change the operation support screen at the same time, but this change requires a considerable amount of time.

Furthermore, since the relationship between the operating procedure and the execution timing could not be clearly expressed at the design stage, it often happened that valves and the like were designed at inappropriate positions. This requires a great deal of labor for the operation, and complicates the operation.

Furthermore, for example, when it is desired to reduce the time required for startup, it is necessary to consider what kind of preparation equipment and equipment is required, or how to change the operation procedure and timing. It was a very difficult problem.

In addition, when the chemical plant is composed of similar units or multiple units integrating multiple units, the operating procedure when operating each component unit alone and the operating procedure for individual units when combining are combined. Is unclear, and it often occurs that it is difficult to confirm whether the operating procedure when each unit is operated alone can be applied to a combined unit plant as it is. .

Heretofore, studies on the expression of plant operation procedures have never been sufficient, but some studies have been known. For example, in a chemical plant operating procedure, a method for determining an operating procedure (JRRivas) is based on the assumption that if the opening and closing of a valve is determined so as to form a desired flow from the inlet to the outlet, the valve operation will determine the plant operating procedure. and
DFRadd, AIChE J., vol. 20 (2), 320-325 (1974); O '
Shima, J. Chem. Eng. Japan, vol. 11 (5), 390-395 (197
8)), an automatic start-up procedure synthesis method, which strictly hierarchizes the function definitions of the constituent units and uses a knowledge engineering approach to determine the plant operation procedure by combining the functions in order to determine the plant operation procedure (Huang Keisin , Shigeyuki Tomita, Eiji Oshima, Transactions of Chemical Engineering, vol.14 (6), 728-
738 (1988)), and an operation procedure determination method that determines plant operation procedures by handling procedures structured into a knowledge base of plant operations (R. Lakshmanan and G. Steph)
anopoulos, Comput. Chem. Enngng, vol. 12 (9/10), 985-1
002 (1988); R. Lakshmanan and G. Stephanopoulos, Com
put.Chem.Engng, vol.12 (9/10), 1003-1021 (1988);
RHFusillo and GJPowers, Comput.Chem.Engng, vol.
12 (9/10), 1023-1034 (1988)), and the like.

These conventional plant operation procedure determination methods are intended to determine an operation procedure based on a given plant structure, and are basically sentence expressions, and have difficulty in expressing parallel operations and the like. . Also, since the plant structure and the operating procedure are not clearly associated and expressed,
When the plant structure is changed, there is a drawback that the correspondence between the structure change part and the part where the operation procedure should be changed is difficult to understand,
It is necessary to reconsider the operation procedure from the beginning.

SUMMARY OF THE INVENTION The present invention has been made to solve the above-described problems. The relationship between the process design, the operation and the timing thereof can be clearly expressed, and the operation expression is simultaneously displayed on the screen for plant operation support. It is an object of the present invention to provide a plant operation display device that can be used as a device.

(Means for Solving the Problems) According to the present invention, in order to achieve the above-described object, each point of a plant component is represented by a node, and a fluid is supplied to the plant from the outside at the node. At least one system input node, and at least one system output node through which fluid flows out of the plant, and adjacent nodes are connected by fluid passages, respectively. In a plant operation display device of a plant, in which a transport means and / or a valve means for creating a fluid flow in the middle of a fluid passage at a required location are provided, the type of the fluid flowing in each of the fluid passages, the phase state of the fluid, , The fluids in the same phase state are sequentially traced from the system input node to the system output node, and these nodes are An output device arranged and displayed in one direction along a flow direction when a flow is generated in the fluid passage; a storage device for storing in advance operation conditions of the transport means and / or the valve means;
A sensor for determining whether or not the operating condition of each of the transport means and / or the valve means is satisfied, and whether or not the operating condition is satisfied in order from the transport means and / or the valve means on the system input node side. Determine whether or not
When the operating condition is satisfied, the output device highlights that the transportation means and / or the valve means should be operated, and the node between the nodes where the flow is generated by the operation of the transportation means and / or the valve means. And an output device control means for highlighting only the fluid passage of the plant.

This plant operation display device is provided with a driving means for driving the transportation means and / or the valve means, and when the operating condition is satisfied, the driving means is provided with the transportation means and / or the driving means.
Alternatively, the valve means can be driven.

According to another aspect of the invention, each point of a plant component is represented by a node, which includes at least one system input node, from which fluid is supplied to the plant from outside, and A transport means including at least one system output node flowing out of the plant and connecting adjacent nodes with fluid passages, and forming a fluid flow in a required portion of the fluid passages in these fluid passages An input device for inputting data by an external input operation, in a plant operation display device for performing a plant operation evaluation by simulating the plant, and / or a plant in which the valve means is disposed;
Based on the type of fluid that is input by the input device and flows from one node to an adjacent node through each of the fluid passages and the phase state of the fluid, the fluid that is in the same phase state is transmitted to the system input node. From the system output node to the system output nodes, and an output device for displaying these nodes in one direction along the flow direction when a flow occurs in each fluid passage, Storage means for storing operation conditions of the means and / or valve means in advance, simulation signal output means for outputting a simulation signal for simulating the operation conditions of the transportation means and / or valve means, and the system input Whether the operation condition is satisfied by the presence or absence of the simulation signal from the simulation signal output means in order from the transportation means and / or the valve means on the node side When the operating condition is satisfied, the output device highlights that the transport means and / or the valve means should be operated, and the flow is controlled by operating these transport means and / or the valve means. And an output device control means for highlighting only a fluid passage between nodes considered to have caused the occurrence of the plant operation display device.

(Operation) In the present invention, the plant operation such as the start-up of the plant basically performs “flow management” and “hold-up management” between each node of the plant components.
Recognizing that the flow of the fluid in the target state is to be created between the nodes, the fluids in the same phase state are sequentially traced from the system input node to the system output node, and these are moved in one direction along the flow direction. Is displayed based on the knowledge that the plant operation procedure and its timing can be displayed according to the line configuration of the plant.

The plant operation procedure and its timing displayed on the output device as described above, that is, the sequence graph of the plant is expressed along the flow of the fluid, that is, in correspondence with the line configuration. In addition, the fluid supplied from the outside to the plant includes a process fluid and a working fluid of a heat exchanger.

The plant operation display device of the present invention is provided with driving means for driving the transport means and the valve means, and when the operating conditions are satisfied, the driving means drives the transport means and the valve means to enable automatic operation. .

Further, the plant operation display device of the present invention is provided with a simulated signal output means for outputting a simulated signal for simulating the operating conditions of each transport means and / or the valve means, instead of the sensor means, and comprises a system. From the transportation means and / or the valve means on the input node side, it is determined whether or not the operation condition is satisfied based on the presence or absence of the simulation signal from the simulation signal output means. Design assistance is provided by highlighting that the vehicle and / or valve means should be operated and by highlighting only the fluid passages between nodes that are deemed to have flow caused by the operation of these vehicle and / or valve means. It can also be used as a simulation support device as a tool.

(Example) Hereinafter, an example of the present invention will be described in detail with reference to the drawings.

First, as a first embodiment of the plant operation display device according to the present invention, an example applied to a distillation column system will be described. Since this plant operation display device has a function as a process design support tool for a plant, a description will be given of a plant design procedure.

Line configuration at the time of steady operation The line configuration at the time of steady operation, and the operation and internal state of the plant are assumed to be already determined at the stage of the process basic design. That is, the distillation column has a tower section and a reboiler and a condenser for heating, which are heat exchange components, as main components, and the line configuration is represented by a plot plan shown in FIG. . In the figure,
Arrow indicates flow direction, solid line Indicates the flow of liquid Indicates the flow of the gas-liquid mixed phase Represents the gas flow. Also double line Represents the flow of heat. ○ indicates any of the inlet point, outlet point, and connection point of the fluid. In this case, the flow rate, the composition, the pressure, the temperature, the phase of the fluid, and the like, which are the internal states of the plant, are determined as the simulation data in the steady state. In addition to the selection prerequisites, operating conditions, preparation conditions, and the like for each component, conditions such as fluid properties and reactions, such as fluid reactivity (particularly, polymerization), explosiveness, and flammability It is also assumed that properties such as toxicity, corrosiveness, etc., and conditions such as easiness of crystallization and solidification, generation of scale, and ease of slurrying are given.

(Arrangement of Pumps, Valves, etc.) Next, the arrangement positions of valves, pumps, etc. necessary for plant operation are determined based on the above-described preconditions. In making this determination, the concept of “flow management”, which is a concept that plays an important role in establishing the present invention, is applied.

The concept of “flow management” has two meanings. The first is related to the state management of a fluid, that is, the management of flow creation, and the second is, as will be described in detail later, a valve operation. This is a concept related to the timing management of flow creation centered on. Here, to explain the former flow control, it is necessary to consider how to generate a steady-state fluid flow as shown in the plot plan of FIG. When doing so, the phase change requires a device that creates and removes heat (heat exchange) and a large change in pressure (flash, etc.), and such a device should be considered.

Therefore, the outline of the plot plan shown in Fig. 3 was created at the stage of PFD design, and the types and installation locations of the raw material tank, condenser, reflux tank, reboiler, bottom tank, etc. were determined as known information. In FIG. 3, the entry point, the exit point, and the connection point (each indicated by a circle) in the flowchart are rewritten, and at the same time, a fluid flow is created using an external force such as a pump or an ejector. Distinguish from those that are not. FIG. 4 is a flowchart showing the distinction of the fluid transport means,
In this embodiment, (G) can be used for transporting a fluid by gravity, (S) can be used for transporting a fluid by using the siphon effect, and the fluid can be transported by decompression due to condensation. (PR) is added to indicate that a fluid flow can be created without using an external force.

As shown in FIG. 4, fluids classified by the above-mentioned symbols and fluids other than the gaseous phase require transportation means by an external force in order to create a flow of the fluid. As means of transportation by this external force, a method of cooperating a heating operation with a compressor, a pump, an ejector, a throttle valve,
There is a means for applying a high pressure to the fluid to transport the fluid, such as a method for cooperating a gas condensing operation with a decompression pump, an ejector, a throttle valve, and the like. What is necessary is just to select an appropriate substance according to the type and properties of the fluid.

In the present embodiment, as shown in FIG. 5, a pump P1 is provided between the raw material supply inlet point and the raw material supply stage of the distillation column, and a pump P2 is provided between the reflux tank of the condenser and the top of the distillation column. A pump P3 is required between the reflux tank and the distillate outlet, and a pump P4 is required between the bottom tank and the bottom distillate (bottom product) outlet. Although not shown in FIG. 5, auxiliary equipment and maintenance lines may be added as appropriate by selecting such transportation means using an external force.

Next, regarding the selection of the valve, in the case of the distillation column system of the embodiment, for example, the valve may be arranged according to the following rules.

(Rule 1) A valve is provided on the discharge side of the pump in consideration of pump maintenance and the like. However, the valve may be omitted in the case of a fixed-quantity type pump.

(Rule 2) A valve is placed on the inlet side of the heating steam of the reboiler, and a drain valve is placed on the outlet side.

(Rule 3) A valve is placed at the inlet or outlet of the cooling water of the condenser.

(Rule 4) Install a valve in the outflow line from the tank.

(Rule 5) When a plurality of lines are connected from the tank, at least one control valve (CV) is required.

FIG. 5 shows the arrangement of valves in accordance with the rules described above. Needless to say, the type of the valve depends on the use and the type of fluid.

(Arrangement of hold-up) Apparent hold-up operation is not necessarily required during the steady operation of the plant. However, considering unsteady processes such as start-up operation and shutdown operation,
Hold-up plays an important role in determining the execution timing of a plant operation procedure. That is, the above-mentioned "flow management" is performed by arranging this holdup at a required position and managing this amount. In particular, in order to ensure stable transportation by the pump, it is necessary to arrange the pump upstream of the pump. Generally, the phase change of a fluid does not occur exactly at a constant speed, but involves a fluctuation. Therefore, a hold-up is provided at a position before the phase change to provide a residence time of the flow to absorb the flow fluctuation. . In addition, it is a matter of course that the hold-up is disposed for the purpose of storing the raw material liquid, the bottom distillate (the bottom product), and the top distillate (the top product).

FIG. 6 is a view in which a hold-up is arranged from the above viewpoint, in which a raw material supply tank H1, a bottom tank H5 at the bottom of the distillation column, a reflux tank H8 at the distillate outlet side of the condenser, An overhead product tank H9 is located downstream of the top distillate outlet.
Downstream of the bottom distillate outlet, bottom product tanks H10 are respectively disposed. In FIG. 6, these tanks are indicated by ◎.

Line configuration at startup operation Next, consider the line configuration at startup operation and add the necessary lines. As the operation method at the time of start-up, a so-called total reflux method, a circulation method, a dripping method, and the like are known, but as for the examination of the line configuration at the time of the start-up operation, an economical viewpoint and a viewpoint of shortening the start-up time. Therefore, it is sufficient to consider the former two, that is, the total reflux system and the circulation system.

(Line configuration of total reflux system) In the full reflux system, the raw material supply line, the top distillation line, and the bottom distillation line are shut off, and the top and bottom of the reflux tank H8 and the bottom tank H5 are separated. This is a system in which all fluids are recirculated until the discharged composition reaches a target composition. Valve V to shut off the line on any line
Since 1, V4 and V6 are arranged, as shown in FIG.
This method does not require any new equipment, and can be dealt with simply by opening and closing the valve.

(Circulation system line configuration) The circulation system uses the distillate at the top and bottom of the tower as a feed tank.
It is a system that returns to H1 and does not get out of the system. In the case of this system, it is desirable to shift to the above-mentioned total reflux system when the distillate at the top and bottom reaches a predetermined composition (temperature). You may start up with As an auxiliary line, the top distilling line S1
2 and the raw material supply tank from the bottom distillation line S14 respectively
Return lines S20 and S21 returning to H1 are required.

Since the raw material supply tank H1, the top product tank H9, and the bottom product tank H10 are all on the ground, the tanks H9, H10
, A pump is required for each of these return lines, but as shown in FIG. 8, switching valves are provided downstream of the valves V4 and V6 of each of the distillation lines S12 and S14. SV1 and SV2 are installed.
If return lines S20 and S21 are branched from V2, pumps P3 and P4
As a result, the distillate can be circulated to the raw material supply tank H1.

Although the basic plant design has been completed by the above procedure, it is more preferable to consider the inert gas replacement line and bypass line during the start-up operation, and also to examine the line configuration during the emergency stop operation. It is.

FIG. 9 shows the flow sheet of the distillation column system of FIG. 8 designed as described above, with nodes, process fluids,
And the valve are denoted by reference numerals. A node representing each point of the plant component utilizes an external force such as a pipe connection point, a part of the unit, for example, a unit having no connection point with another pipe, such as a heat exchanger, for example, a pump. It includes internal nodes such as a unit and a hold-up, a system input node where a process fluid or a working fluid is externally supplied to the plant, and a system output node where the process fluid or the working fluid flows out of the plant to the outside. The process fluid is indicated by a symbol S1 or the like with respect to the fluid flowing between the nodes adjacent to each other, and this symbol can be considered as an indication of a fluid passage through which the fluid flows between the nodes. The “fluid passage” referred to here may be regarded as a passage not only in a pipe such as a pipe but also in a tower device. As described above, the feature of the present invention resides in that the process fluid and the fluid passage correspond to each other.

A supply line to the raw material supply tank H1 is added, and a system input node, that is, a raw material storage tank is denoted by H0, and a pump and a valve disposed on the supply line S0 are denoted by P0 and V0, respectively. The raw material storage tank H0 includes a mobile tank device such as a tank lorry.

FIG. 1 shows a distillation column system designed as described above,
It is represented by a block diagram and includes a tower section D, a reboiler RB and a condenser CD, a storage tank group, and pumps and valves. In the description of this configuration, since the same reference numerals are given to the components corresponding to the flow sheet shown in FIG. 9, it can be easily inferred, and detailed description thereof will be omitted.

The distillation column system of the first embodiment is provided with a plant operation display device shown in FIG.
The plant operation procedure and the operation execution timing are displayed, and the plant operation such as the start-up operation is executed while monitoring these displays.

Configuration of the plant operation display device The plant operation display device includes an electronic control unit (ECU) 40 for controlling the operation of the entire device, an input device 42 for inputting a plant configuration or a plant operation command signal by key operation or switch operation, and an electronic control device. A display device 44 for displaying the calculation results of the device 40 on the screen, a printer device 46 for printing out the calculation results and the like of the electronic control device 40, and an electronic control device 40
An external storage device 48 for storing arithmetic procedures (programs) and the like executed in the I / O interface, an I / O interface 50 for controlling input / output from the electronic control unit 40,
A drive device 5 for opening / closing a valve or operating a pump by a drive signal from an electronic control device 40 via 50
2. It comprises a sensor means 54 for detecting the liquid level position of the hold-up, the temperature in the tower, the pressure, the line flow rate, etc., and supplying them to the electronic control unit 40 via the I / O interface 50.

Next, the operation of the plant operation display device will be described.

Creation of sequence graph In describing the operation of the plant operation display device, first,
This is a basic technical idea of the present invention, and a procedure for creating a sequence graph to be displayed on the screen of the display device 44 of the plant operation display device will be described.

(Expression of fluid coupling and flow control conditions) The plant operation of a chemical plant, especially the start-up operation procedure, is naturally performed by performing “flow control” and “hold-up control” while basically maintaining the conditions related to safety and quality. Think it will be decided. That is, the basic technical idea of the present invention is based on the idea of “flow management” and “hold-up management”.

`` Flow management '' means that when a chemical plant performs a start-up operation from an initial state to a target steady state, a fluid passage between adjacent nodes from the system input node to the system output node, that is, This means managing the state of the fluid in the line and creating a target flow state from the initial state. As a method of expressing the flow of the fluid in the plant, in the present invention, focusing on the phase state of the fluid, if the fluid in the same phase state is sequentially traced from the node on the system input side to the node on the system output side, , The operation procedure can be naturally expressed.

By the way, when a fluid in the same phase state is traced from a node on the system input side, if the fluid changes the phase state on the way, the fluid cannot be traced after that position. A phase change is caused by the transfer of heat or a large change in pressure of the fluid,
When there is a large change in pressure, the phase-changed fluid is considered to be continuous at that position, and the fluid in the phase-changed state is traced toward the node on the system output side.

“Hold-up management” is necessary for stably performing plant operations, particularly operation timing, by arranging hold-ups at key points in the plant and managing the hold-up amount. That is, the valve operation is started when the hold-up amount of the fluid flowing into the hold-up reaches a preset determination value.
Used for valve operation start conditions and stop conditions. This discrimination value may be changed according to the plant state and take some appropriate values. For example, the determination value for operating the pump may be set to a value different from the determination value after reaching the steady state. That is, the determination value of the hold-up amount is considered to be a variable related to the time required for start-up and quality control.

Based on the above concept, when all the phase states of the process fluid flowing between the adjacent nodes of the flow sheet shown in FIG. 9, that is, the fluid coupling and the flow management conditions are written out, the following table can be obtained. .

The meanings of the expressions of the fluid connection and flow management conditions shown in Table 1 are described below for a few explanations.

The process fluid S1 is supplied to the node 1-H (the raw material supply tank H
Liquid L flowing from 1) to node 3 (distillation tower feed stage), the flow of which is created by the operation of pump P1. However, it starts when the valve V1 is opened.

The process fluid S3 is a liquid L flowing from the node 3 to the node 4, and the flow thereof flows without an external force.

Since the process fluid S6 is a gas-liquid mixed phase (L + V) flowing from the node 6 to the node 4 and changes its phase from the liquid phase L to the mixed phase (L + V) before and after the node 6, an external heating source + E2 is required at the node 6. I do.

The process fluid S10 is the liquid L flowing from the node 7 to the node 8-H (the reflux tank H-8).
Changes from the gas phase V to the liquid phase L before and after the
-H requires external cooling source -E1.

The process fluid S15 is the liquid L flowing from the node 17 to the node 10-H (tower product tank H-10), and the flow starts when the switching valve SV2 at the node 17 is in the state (2). .

Table 2 shows conditions under which a process fluid may be produced, that is, operating conditions of valves and pumps, and these conditions are set in advance.

For example, it may be flowed process fluid S0 condition (ON condition) is when the hold-up quantity of the hold-up H1 is a smaller than the set value (1-H ^S). At this time, the pump
Activate P0 and open valve V0. Also, the hold-up amount of hold-up H1 is equal to the set value (1
−H ^S ) and hold-up H5 and H8
Holdup amount, if from the large both set value (5-H ^S) and (8-H ^S), turns OFF the process fluid S0 to stop the pump P0. If it takes time to prepare the pump, the pump P0 should be operated in a standby state.

The ON condition of the process fluid S1 is when the hold-up amount of the hold-up H1 is larger than a set value (1−H ^S ). When the ON condition is satisfied, the pump P1 is operated to open the valve V1.

The process fluid S3 is always in the ON state. That is, if a fluid is supplied to the node 3, the flow of the process fluid S3 is created by gravity drop.

The process fluid S6, when the hold-up quantity of the hold-up H5 becomes larger than the set value (5-H ^S),
Steam is passed through the reboiler to create a flow of the process fluid S6. In addition, the timing of flowing steam to the reboiler is performed at the same time as the start of the start-up operation, so that the steam is warmed up.

Table 3 S15 [ON: 17 → 10:: SV2 (2): # 1] S13 [ON: 18 → 9:: SV1 (2): # 2] Table 3 shows the switching operation conditions from startup operation to steady operation. Is shown. When the condition for transition to the steady operation indicated by # 1 is satisfied, the switching valve SV2 is switched to the state of (2) and the process fluid S15 flowing from the node 17 to the node 10 is switched.
When the steady operation transition condition indicated by # 2 is satisfied in the ON state, the switching valve SV1 is switched to the state of (2) to turn on the process fluid S13 flowing from the node 18 to the node 9.
State. The conditions # 1 and # 2 for transition to the steady operation include, for example, each composition (temperature) of the distillate at the bottom and top of the column.
Need to reach their set values (target values).

When the above-described fluid connection and flow management conditions are prepared, the information is input to the electronic control device 40 by operating the keys of the input device 42. Then, after inputting all of these information, when the calculation start command signal is keyed into the electronic control device 40 via the input device 42, the electronic control device 40
In accordance with the stored calculation procedure, a sequence graph is created based on the input information shown in Tables 1 to 3 and displayed on the screen of the display device 44. FIG.
The calculation result calculated by the electronic control unit 40 is displayed on the display unit 44.
Shows a sequence graph at the time of the start-up operation displayed in FIG.

Sequence graph Next, based on the calculation results shown in Fig. 10, the electronic control unit
A description will be given of what calculation method is used to create this sequence graph.

By the way, in order to obtain the sequence graph shown in FIG. 10 based on the fluid coupling and flow management conditions shown in Tables 1 to 3 above, the creation of the program executed by the electronic control unit 40 itself is well known to those skilled in the art. Is easy, and there can be various methods of creating programs, and therefore, the contents thereof are not particularly described. That is, the present invention is characterized in that the designed plant configuration, the operation procedure, and the execution timing thereof are displayed on a screen of the display device 44 on the screen of the display device 44 according to the calculation result of the electronic control device 40, and the sequence graph is displayed. However, the computer software creation procedure itself has no feature.

In the sequence graph of the present invention, each point of the plant component is represented by a node, and sequentially traces from the system input node to the system output node based on the phase state of the fluid,
The images are arranged and displayed in one direction of the screen, that is, from the upper part to the lower part of the screen in the embodiment, along the flow direction. In the sequence graph of FIG. 10, the input node of the distillation column main body is one of the nodes 0 to H, which corresponds to the raw material storage tank H0. There are two output nodes, nodes 9-H and 10-H, which are the top product tanks.
H9 and bottom product tank H10 correspond. In addition, the reboiler and the condenser, which are heat exchange components, also have input nodes 14, 11 and output nodes 16, 13, respectively.

This sequence graph is obtained by converting the above-mentioned Tables 1 to 3 into a flow sheet by the following procedure. First, the electronic control unit 40 sequentially traces fluids in the same phase from the system input node to the system output node based on the input information of Table 1. More specifically, starting from the process fluid S0 which is a liquid phase, the fluid which is in the liquid state L is input to the node 0- which is the input node.
Starting from H, it reaches the hold-up node 5-H via the node 1-H → the node 3 → the node 4. This node 5
At -H, the fluid splits into two, one of which becomes process fluid S14 and reaches node 17. This fluid becomes one of the process fluids S15 and S21 at the node 17 which is the switching valve SV2 depending on the switching state of the valve, and reaches the node 10-H which is the output node, or the node 1 on the input side. -H is returned.

The other fluid branched off at the hold-up node 5-H reaches the node 6 as a process fluid S5. Node 6
Then, the phase change occurs due to the heat (+ E2) from the reboiler,
Although the gas phase V and the liquid phase L are mixed, if the heat is transferred according to the rules, the process fluid is considered to be continuous. This multiphase fluid S6 proceeds from node 6 to node 4.
The multi-phase fluid S6 is at the node 4 and the fluid, which is a liquid phase, becomes the above-described process fluid S4 and becomes the hold-up node
At -H, the fluid in the gaseous phase becomes the process fluid S7 and rises upward due to gravity (difference in density) and reaches node 7 of the capacitor via node 3 → node 2. During this time, the gas phase is maintained, so the broken line Is represented by the following flow.

At the node 7, heat (-E1) is taken by the cooling water, and a phase change from a gas phase to a liquid phase occurs. In this case, the process fluid is considered to be continuous because heat was transferred.
It becomes the process fluid S10 and reaches the hold-up node 8-H that is the reflux tank H8. At node 8-H, the fluid is branched into two, one of which is a liquid phase L process fluid S11.
Is returned to node 2 → node 3. Node 8-
The other fluid branched in H is the process fluid S12
To reach node 18. This fluid is processed fluid S13 and process fluid S13 according to the switching state of switching valve SV1.
As one of the steps S20, the signal reaches the node 9-H, which is the output node, or returns to the node 1-H on the input side.

From the input node 14 of the reboiler, the steam fluid S18 in the gaseous phase reaches the node 15 via the valve V5, where it undergoes a phase change and reaches the output node 16. From the input node 11 of the condenser, the cooling water fluid S16 in the liquid phase reaches the node 12 via the valve V3, where heat is transferred and reaches the output node 13.

Here, the various symbols in the sequence graph will be described.
Indicated by The components included in the structure node are as described above (see FIG. 9). The management of the hold-up or various judgment conditions is described in [].
This determination condition can arbitrarily add various conditions such as not only the hold-up amount and the liquid height, but also a transition condition from start-up to normal operation. As described above, it is needless to say that the determination conditions of the embodiment are all examined at the stage of preparing Tables 1 to 3.

The initial state of the valve is normally closed. However, depending on the operation procedure, an operation procedure such as closing → opening → closing can be considered. In order to indicate the closed state of the valve (CLOSE)
Symbol is added. This symbol can be displayed by changing the brightness of the screen, such as darkening when the valve is closed and brightening when the valve is open.

In FIG. 10, the progress of the flow is indicated by an arrow, and a broken line is drawn in a direction orthogonal to the flow so as to block the flow. Has been drawn. This dashed line indicates the activation of the valve, heating or cooling, operation of the pump or compressor. If there is a mark in all the nodes having a flow that is directly input to this activation and the determination condition, the operation can be started. For example, the first activation from the top of the flow shown in Figure 10 is the valve
Indicates the operation start of V0, judgment condition of the valve opening in this activation is the hold-up amount is set value 1-H ^S following conditions holdup H1, leave prepare pump P0, the When the condition is satisfied, all flows directly input to this activation are marked, and the valve V0 may be opened. In particular, when the temporal valve operation such as the valve opening speed is important, the activation symbol is indicated by a double dashed line. , And a time condition can be given between the double broken lines.

In the above-mentioned flow, in addition to the material flow such as gas, liquid, and multiphase flow, the heat flow (double line as described above) ) And the flow of information. In the information flow, there is information indicating that a judgment condition on hold-up management, a judgment condition on a process flow state, and the like are satisfied.
A broken line connecting between the judgment condition shown in [] and the activation , And the direction of the flow is indicated by an arrow. The material and heat flows are indicated by the same type of lines as described above (see FIG. 3), but can also be colored or represented by other line types.

The above-mentioned mark changes the screen display of the node or the determination condition to a bright luminance as described above, when the determination condition regarding the node where the flow exists, the state of the hold-up management or the flow of the process is satisfied. Display. Instead of changing the luminance, the color may be changed. Normally, when the valve is closed by valve operation, the material flows downstream (heat flow) through the valve.
Is gone. That is, the mark in the node related to the material flow (heat flow), which is combined with the flow from the activation of the valve operation, disappears. However,
If there is a material flow recycle loop downstream of the activation for the closed valve,
In such a case, the mark of the node in the loop will not disappear, since the material flow in the loop may be continued.

The aforementioned sensor means 54 constantly monitors whether or not the above-mentioned judgment conditions regarding the hold-up management and the state of the process flow are satisfied. That is, the sensor means 54
The liquid level position and hold-up amount of the hold-up, the temperature and pressure at each position in the tower, the composition of the distillate, etc. are constantly detected, and the detection signal is supplied to the electronic control unit 40 via the I / O interface 50. are doing. The electronic control unit 40 determines from the supplied detection signals whether or not the above-described determination conditions regarding the hold-up management and the state of the process flow are satisfied.

Now, the procedure and timing for starting up the distillation column system while monitoring the sequence graph will be described. Note that as an initial condition, the raw material is stored in the raw material storage tank H0, but the hold-up amount of other hold-ups is zero. Also pumps and reboilers
It is assumed that the preparatory work for RB startup operation has been completed. Then, it is assumed that the switching valves SV1 and SV2 are both switched to the state (1).
Further, the operation of the pump and the valve can be remotely controlled by outputting an open drive command signal from the electronic control device 40 to the drive device 52 by operating a switch or a key of the input device 42 of the plant operation display device. Shall be. However, it is needless to say that the operation of these pumps and valves may be a manual operation by an operator as appropriate, a manual operation at the time of the ON operation, and an automatic stop operation by the electronic control device 40 at the time of the OFF operation or emergency stop. It may be.

First, when the operation of the distillation column system is turned on, the sequence graph displayed on the screen of the display device 44 includes the hold-up 0-H and the control conditions [<1.
−H ^S ]. Nodes 14 and 11 are also marked and highlighted. The operator checks the display status of the mark on the sequence graph, and then checks the pump P0
Turn on the operation switch. The valve V5 of the reboiler RB is opened when the hold-up amount of the bottom tank H5 reaches a set value. Next, by the opening operation of the valve V3, all the nodes 11, 12, and 13 at each point of the capacitor CD are marked. These valves V3 and V5 may be operated in a preparation stage if there is no problem in safety and equipment.

On the other hand, the operation of the pump P0 also marks this pump node P0. Therefore, all the flows toward the activation for the valve V0 are marked, and all the conditions for determining the valve V0 are satisfied and the valve V0 is satisfied.
This means that V0 may be opened. Therefore, the electronic control device 40 outputs an open drive signal to the valve V0 via the drive device 52 to open the valve V0. This allows the raw material storage tank
From H0, the raw material fluid flows to the raw material supply tank H1, and the hold-up node 1-H on the display screen is highlighted, that is, marked.

Next, regarding the activation of the valve V1, the process waits until a predetermined amount of the raw material fluid is supplied to the raw material supply tank H1. At this time, the pump P1 is operating in the standby state, and the pump P1 is also marked.
When the hold-up amount of the tank H1 reaches the set value, the judgment condition is marked, and all the flows toward the activation are marked, so that the electronic control unit 40 controls the valve via the drive unit 52. An open drive signal is output to V1 to open valve V1. As a result, a flow has been created until the next activation, and each node up to each activation for valves V6, V4, V2 is marked. In practice, the flow of the process fluid S6 by the reboiler RB will not substantially occur unless the hold-up amount of the bottom tank H5 reaches the vicinity of the set value. It will be stored in tank H5.

When the hold-up amount of the bottom tank H5 reaches the set value, the determination condition is marked. After confirming this mark, the operator will operate the pump P4, and all flows toward each activation related to V2 will be marked, and the valve V6 will be opened. Valve V6
Is opened, the distillation column system has not yet reached a steady state, so the switching valve SV2 is set to (1).
And the fluid from the bottom tank H5
It is returned to the raw material supply tank H1 via the reflux line S21.

On the other hand, when the hold-up amount of the bottom tank H5 reaches the set amount, the valve V6 of the reboiler RB is opened, heating of the process fluid by steam is started, and the distillation components are changed from the node 4 to the node 3 to the node 2 via the node 2. 7 is reached,
Here, it is cooled and condensed by the cooling water, and flows into the reflux tank H8.

Activation for valve V4 and valve V2 is based on the hold-up amount of tank H8 set value [8
−H ^S ]. When the hold-up amount reaches the above-mentioned set value, the pump P3 is operated to open the valve V4, and one of the distillate at the top of the reflux tank H8 via the switching valve SV1 which has been switched to the state (1). The part is returned to the raw material supply tank H1, and the pump V2 is operated to open the valve V2, and a part of the distillate at the top of the reflux tank H8 is returned to the top. Then, when all the determination conditions that the hold-up amount of the reflux tank H8 reaches the set value and the hold-up amounts of the hold-up nodes 5-H and 1-H are each equal to or more than the set value are satisfied, the valve V0 is closed. As a result, a standby state for transition to a steady operation by the circulation system is established.

The sensor means 54 constantly monitors the composition and temperature of the distillate at the bottom and top of the column, and the composition (temperature, etc.) of these distillates
Reaches the target value, and each transition condition # 1 to the steady operation
When # 2 and # 2 are established (YES), the corresponding switching valves SV1 and SV2 are respectively switched to the (2) state, and the top and bottom distillates circulated to the hold-up node 1-H are respectively discharged. Is started in the storage tanks H9 and H10, and the operation shifts to a steady operation.

Thus, in the initial stage of the start-up operation, the process fluid is circulated in a circulating manner until the bottom and top distillates of the hold-up nodes 5-H and 8-H reach the target composition (temperature), The startup time has been reduced.

In order to further reduce the startup time,
When the composition (temperature, etc.) of the bottom and top distillate reaches the set value by the sensor means 54, the valves V1, V4 and V6
It is also possible to reflux the distillate of the hold-up H5, H8 at the bottom and top of the column by a total reflux method. Also in this case, when the composition (temperature, etc.) of the bottom and top distillate reaches the target value, the valves V1, V4, and V6 are opened again, and the switching valves SV1 and SV2 are opened. Are switched to the state (2) and the operation is shifted to the steady operation.

Furthermore, before starting the start-up operation, the products are charged into the hold-ups H8 and H5 at the top and bottom of the product, and the start-up operation is started by the total reflux method, so that the start-up time can be further reduced.

Sequence Graph of Shutdown When performing a system stop operation (shutdown operation) from a steady operation of the distillation column system, the sequence graph of the start-up operation described above can be used as it is. The considerations for the shutdown operation are to consider the safety and the quality of the remaining fluid as a hold-up, and to cut off some of the flow conditions in the steady-state operation included in the sequence graph of the start-up operation. Is a shutdown operation. That is,
Since the equipment required for the start-up operation can be used as it is, there is no need to specially prepare equipment for the shutdown operation, and there is no structural difference from the equipment required for the start-up operation.

Therefore, the procedure of the shutdown operation may be sequentially executed according to the timing displayed on the display screen of the display device 44 using the sequence graph used at the time of the startup operation. In many cases, the operation procedure at the time of the shutdown operation does not follow the flow of “from raw material supply to product” as at the time of the start-up operation.

In the case of the distillation column system of the embodiment, the feed of the raw material is stopped by closing the valve V1 and stopping the operation of the pump P1, and the valve
Close V5 and cut off the steam supplied to the reboiler RB.
At the same time, the switching valves SV1 and SV2 are switched to the state (1) to suppress the distillation at the top and bottom, and to increase the amount of reflux. Then, if the valve V3 for supplying the cooling water is closed after the process fluid is sufficiently cooled, the shutdown operation is completed.

These operation procedures and operation timings can be sequentially taught to the operator by sequentially flashing activations corresponding to the next operation using the same sequence graph used at the time of the start-up operation.

Sequence graph for emergency stop In the emergency stop operation procedure, safety is generally given the highest priority. In many cases, emergency stop equipment is added to the plant based on safety. With this, an operation sequence graph is assembled. Additional equipment, for example, equipment that removes fluid from the main plant components,
Alternatively, it is a facility for supplying a sealing gas for preventing an explosion or the like. In the case of the emergency stop operation, the flow does not change from “raw material supply to product” as in the operation procedure and timing of the start-up operation, but can be expressed in the same expression as the shutdown operation.
In addition, for the supply of additional fluid and the removal of process fluid, it is necessary to add a line for fluid transportation to the main process line. Creating a graph is easy. When the process fluid is forcibly removed by the additional equipment, special consideration must be given to the node at the junction between the main process line and the exclusion equipment, such as a special symbol or color identification to distinguish it from other nodes. Is preferred.

The above-described plant operation display device, when the electronic control device 40 executes the drive control of all pumps and valves, the start-up operation and the shutdown operation can also be completely automatically operated. Can also be used as an automatic operation device.

Use as a simulation support device The plant operation display device of the present invention applied to the distillation column system in the above-described embodiment operates the operation procedure and the operation timing of the actual device such as start-up operation, shutdown operation, or emergency stop operation. Not only useful as a device to teach operators, but also as a design support tool when designing a plant while taking into account the plant operation procedure and its operation timing, or a simulation support device for mastering the operation of actual equipment operators Can also be used usefully.

When used as a simulation device, the flow rate, pressure, and temperature of the process fluid at each point in the distillation column, reboiler RB or condenser CD, or at the hold-up, instead of the sensor means 54 of the plant operation display device shown in FIG. A simulated signal generator for generating a simulated signal representing a state quantity such as a composition may be connected to the electronic control unit 40 via the I / O interface 50. Then, when a pump or a valve is operated, a change in the state quantity of the process fluid from the operation is predicted, and this is sequentially supplied to the electronic control unit 40.

When a plant operation display device is used as the simulation device, a sequence graph can be displayed on the display device 44 on the screen in the same manner as that applied to the actual device described above, and operated in accordance with the highlighted activation instruction. In addition, the operation evaluation such as the operability of the designed plant can be facilitated, and the plant operation can be easily used.

Second Embodiment The sequence graph displayed on the screen of the plant operation display device according to the present invention can be applied to a combined unit including a plurality of units. In particular, when the modularization of the basic unit is progressing, it can be applied more easily.
In other words, since the structure of the plant and the operating procedure correspond, if the structural change required to connect the two units is clarified, the change in the operating procedure corresponding to that part is clarified. can do. Such an example will be described using a distillation column system with a heat pump, which is the second embodiment. As in the first embodiment, in FIG. 11, the same reference numerals are used for the lines (fluid passages) as those for identifying the fluid.

Line configuration of heat pump The distillation column system of the second embodiment is a combined system in which the heat pump HP that uses water as a working fluid (heat medium) is connected to the distillation column system of the first embodiment. FIG. 11 shows a line configuration of a heat pump unit applied to the distillation column system.

The heat pump HP is a thin film falling-down type heat exchanger including two heat exchangers (side cooler and side heater) SC and SH. The side cooler SC takes condensed heat from the process fluid and gives the heat to the water as the working fluid to vaporize it. The side heater SH gives the condensed heat of the working fluid to the process fluid and removes it from the process fluid. The part is evaporated. At the bottom of the side cooler SC and the side heater SH, hold-up H55,
H54 is provided. The heat pump HP includes compressors C1 and C2 and a pressure reducer V51 for raising the temperature of the vaporized working fluid, in addition to these heat exchangers.

The side heater SH and the side cooler SC are provided with process fluid circulation lines S44 and (S52, S53), respectively, in order to increase the wetting area of the heat transfer surface, and these lines are provided with a circulation pump and a valve (P41). , V41), (P50, V52)
Is arranged.

Further, a working fluid (water) input line is required as operation preparation equipment for the heat pump HP. For example, a working fluid injection pipe S51 is attached to the side cooler SC. In addition,
The working fluid is heated by the process fluid in the side cooler SC and evaporates, passes through the compressors C1 and C2, condenses in the side heater SH, and accumulates in the hold-up H54 of the side heater SH. In order to start the compressors C1 and C2 smoothly, a pipe S60 for reducing the load at the time of starting is necessary.
The 60 is provided with a valve V54 that closes it during normal operation. Further, drain lines S65, S66, and S67 are provided for the purpose of eliminating working fluid condensed around the compressors C1 and C2. Further, there are provided exhaust lines S61 to S63 for air entering the heat pump HP, and a spray device (S64, V53) for working fluid for preventing superheat.

Change of Line Configuration of Distillation Column and Heat Pump The above-described heat pump HP is disposed at an intermediate stage between the condenser CD and the distillation column D of the first embodiment, and is provided with two heat exchangers S.
Since C and SH are in contact with the process fluid on the distillation column side and the heat transfer surface, respectively, the distillation column D and the heat pump HP
Requires structural changes to couple them together. Table 4 lists the joints between the distillation column D and the heat pump HP.

Based on the height positional relationship between both ends of each connection line shown in Table 4 above, as a necessary transport device, the pump P42 and the valve V43 are connected to the line S47 on the output side of the side cooler SC, and the side heater SH
Pump P40 and valve in line S41 on the process fluid input side
All you need to do is place each V40 and add a pipeline for the related utilities.

Line configuration at start-up operation The line configuration required at start-up operation of the distillation column system with heat pump is as follows. First,
The circulation method described in the first embodiment is adopted,
A pipe for returning the distillate at the top and bottom to the raw material supply tank H1 is required.

In addition, in addition to the hold-up arrangement of the distillation column system of the first embodiment, the hold-up
Add 33-H. The hold-up 33-H is provided for receiving a process fluid flowing down from the top of the distillation column and sending it out to the heat pump HP side.

As a result of the above examination, FIG. 12 shows a structural expression of the distillation column system modified to connect the heat pump HP, and FIG. 13 shows a structural expression of the heat pump HP. In these figures, components corresponding to the distillation column system of the first embodiment are denoted by the same reference numerals.

Creation of sequence graph (Expression of fluid connection and flow management conditions of distillation column) By the same method as described in the first embodiment, the same fluid connection and flow management conditions as in Table 1 during startup operation on the distillation column side. Are summarized in Table 5 below.

Table 5 differs from Table 1 in that fluids S7 ', S
Only 7 ″, S7, S3 ′, S9, S9 ′ have been added or changed.

(Transition to Steady-State Operation) Switching from the start-up operation on the distillation column side to the steady-state operation is performed as follows.

When all the hold-ups satisfy the set value during the start-up operation, the valve V1 is closed to stop the supply of the raw material, and at the same time, the valves V4 and V6 are closed, and the steady-state operation transition conditions # 1 and # 2 are satisfied by the full reflux method. Wait for. Then, when the conditions # and # 2, which are the conditions for transition to the steady operation, are satisfied, the operation in Table 6 is executed.

Table 6 S13 (18 → 9−H: L::: SV1 (2)) S15 (17 → 10−H: L::: SV2 (2)) That is, open line S13 and close line S20, The line S15 is opened and the line S21 is closed. Here, the steady-state operation transition conditions # 1 and # 2 determine, for example, that the tower bottom temperature exceeds the set value (T17> T17 ^S ) and the tower top temperature exceeds the set value (T18> T18 ^S ). You may do so.

(Expression of fluid connection and flow management conditions of heat pump) First, considering the pre-operation preparation work of the heat pump HP, these are as follows.

Preparation work 1: Injecting working fluid This work is to open the valve 50 of the line S51 and inject working fluid into the hold-up H55. When the required amount of working fluid has accumulated, the valve 50 is closed (see the sequence graph in FIG. 15A).

Preparation work 2: heat exchanger circulating flow In this work, the pump P50 is operated, the valve V52 is opened, and the working fluid in the hold-up H-55 of the side cooler SC is circulated. Further, the pump P41 is operated, and the valve V41 is operated.
Is opened to circulate the working fluid in the hold-up H54 of the side heater SH. By circulating these working fluids, the wettability of the working fluid on the heat transfer surface is improved, and the heat transfer efficiency as a system is improved (see the sequence graph in FIG. 15B).

Preparatory work 3: Configuration of compressor circulation line This work needs to be prepared before starting the compressor.
The valve V54 is opened, and the discharge side of the compressor C2 is connected to the suction side of the compressor C1 to reduce the load at the time of starting the compressor (see the sequence graph in FIG. 15C).

Preparation 4: Construction of drain line This operation also needs to be prepared before starting the compressor.
The discharge side valve V56 of the first stage compressor C1 and the discharge side valve V55 of the second stage compressor C2 are opened to discharge the working fluid (water) accumulated in each compressor to the hold-up H-55 ( (See the sequence graph in FIG. 15D).

Preparation work 5: air release This work is also a work to be performed before starting the compressor. The valves 57 and 58 are opened, and the air in the heat pump HP is discharged by the ejector EJ (see the sequence graph in FIG. 15E).

Preparatory work 6: Configuration of overheating prevention line This work is performed when the outlet temperature of the compressor C2 exceeds the specified temperature.The valve 53 is opened from the circulation line of the side cooler SC, and the hold-up is performed. The working fluid (L) accumulated in H55 is sprayed onto a line between the compressors C1 and C2 to prevent overheating of the working fluid (see the sequence graph in FIG. 15F).

These preparation work sequence graphs
Along with the sequence graph shown in the figure, the display device 44
Can be displayed on the screen, and if necessary, these preparations can be taken into the sequence graph as a condition for determining activation. Normally, many of these preparations should be completed before the first activation related to the heat pump HP in the sequence graph shown in FIG. 15 appears.

Next, as in Table 1, Table 7 summarizes the fluid connection and flow management conditions in the heat pump and the auxiliary line during the start-up operation.

(Conditions for shifting the heat pump to the steady operation) The conditions for shifting the heat pump HP from the start-up operation to the steady operation include hold-up H54 and H55.
When the temperature T54, T55 of the working fluid is satisfied the set value T54 ^S, T55 ^S above conditions ^{(T54> T54 S, T55>} T55 S) respectively, by closing gradually valve V54 of the circulation line S60, transition Work is completed.

When the fluid connection and flow management conditions summarized in Tables 4 to 7 are input to the electronic control unit 40, the electronic control unit 40 creates each sequence graph of the distillation column and the heat pump in the same manner as described above. FIG. 14 and FIG. 15 show sequence graphs of the distillation column D and the heat pump HP, respectively.

The line configuration of the combined system is shown in FIG. 16 by superimposing the connecting portions of the two heat exchangers in FIG. 12 and FIG. On the other hand, the sequence graph of this composite system can be expressed by superimposing their joints in the same manner as the superposition of the line configuration, and this is shown in FIG. The heat pump HP shown in FIGS. 15A to 15F is shown in this sequence graph.
The sequence graph for the preparatory work is also displayed on the same graph (screen), and the procedure and timing of the startup operation of the entire system are expressed.

As described above, the sequence graph of the plant operation display device of the present invention corresponds to the line configuration of the plant, the operation procedure and the execution timing thereof, so that it is extremely easy to change the line configuration and to combine the units. It can be carried out.

For the startup operation of this complex system, activation may be performed sequentially from the entry node side as described in the first embodiment. Considering the startup operation of the heat pump HP, the startup operation of the heat pump HP is completed by closing the circulation line S60 of the heat pump HP, but heat exchange between the working fluid and the process fluid has already started before closing. . As a result, the working fluid is preheated, and when the working fluid reaches a certain temperature, if the circulation line is cut off, the intended function of the heat pump unit, that is, the compression function will be exhibited. The sequence graph shown in FIG. 17 clearly shows the relationship between the operation timings of the heat pump side and the distillation column side, and the operation procedure and the timing of the heat pump HP up to the transition to the steady operation are described. Is expressed. FIGS. 14, 15, 15A to 15F
In the figure and the sequence graph in FIG. 17, the display of the specific judgment conditions of the activation execution is omitted, but in actuality, if all the necessary judgment conditions are listed in [], Good.

In the sequence graph of the plant operation display device of the present invention, the flow direction corresponds to the time axis. The speed at which the process fluid flows between the nodes and the time required until the hold-up amount reaches the set value can be predicted from a simple arithmetic expression or an empirical value. When the sequence and timing of the start-up operation are arranged in a time series by a sequence graph, it is convenient to consider a reduction in the operation time during the start-up operation. For example, if the operation times of valves and pumps shown in the sequence graph are extracted and rearranged in chronological order, it is possible to more clearly express which part of the start-up operation requires the operation time. .

FIG. 18 shows the operation time of each valve from the start, that is, the time when each activation was started and the steady state entered when the start-up operation was performed based on the sequence graph shown in FIG. 17 by the demonstration pilot plant. Are arranged in chronological order.

The configuration and operating conditions of this demonstration pilot plant are as follows.

Distillation column D is a packed column (tower section) having a diameter of 200 mm and a height of 5000 mm. The packing is a 1-inch mini cascade ring, and the packed height is 4000 mm. The process fluid separated here is a mixture of ethanol and water, and experimental results have confirmed that the number of theoretical plates corresponding to the tray column of the target packed column is 11 including the reboiler RB. .

The raw material is supplied to the seventh stage when the top is the first stage, and the side cut stage for sending the process fluid to the side heater SH of the heat pump HP is a portion corresponding to the eighth stage. The reboiler RB of the distillation column D has a heat transfer area of 2.0 m ² , and uses 2.0 kgfG / cm ² of steam as the heating tube-side fluid. In this reboiler RB, heat exchange of about 40 KW is performed at startup and about 16 KW during steady operation.

The condenser CD of the distillation column D has a heat transfer area of 4 m ² and uses water as a cooling fluid. Table 8 shows the main specifications on the distillation column side of the pilot plant.

The heat pump HP is a compression heat pump of the indirect compression type, and uses water as a working fluid. The compressors C1 and C2 are rotary type compressors, and two compressors are used in series so that a large difference in compression temperature can be obtained. Furthermore, the compressor
C1 and C2 have inverters so that the load can be adjusted.

Side heater S, which transfers heat to and from distillation column D
H, the two heat exchangers called side coolers SC are of a liquid film falling type, and sufficient heat exchange is possible even if the temperature difference with the process fluid is relatively small. Table 9 shows the main specifications on the heat pump side of the pilot plant.

In this pilot plant, the state in which the distillation column enters the steady operation switching state is from the time when the heat pump HP is switched to the steady operation, which is 246 minutes after the start-up start time. The time when the entire system shifted to the normal operation state was 376 minutes after the start of the startup.

Thus, when the plant is operated in accordance with the sequence graph displayed on the screen by the plant operation display device of the present invention, the plant can be stably and reliably started up to the target state.

In the above-described first and second embodiments, the start-up operation procedure is based on “flow management” and “hold-up management”. The operation procedure is configured by adding the “transition condition”. Generally speaking, the timing of operation does not depend entirely on the state of hold-up, but rather the temperature, pressure,
In many cases, it is better to add or replace variables such as composition to adjust the operation timing. Further, operating conditions for avoiding dangerous operating conditions can be added. In any case, the plant operation can be made flexible by adding these conditions to the activation judgment conditions.

In the above-described second embodiment, it has been demonstrated that the pilot plant can surely operate the plant. However, it takes 376 minutes to complete the start-up operation, and there is room for improvement. Therefore, the operation procedure was improved. No.
Table 10 summarizes the time required to obtain the required hold-up amount from the valve operation time shown in FIG.

Table 10 H1: Raw material supply tank 5 minutes H5: Bottom tank 20 minutes H8: Reflux tank 70 minutes H55: Side cooler hold-up 2 minutes H54: Side heater hold-up 15 minutes Heat pump preheating time 80 minutes Standby operation transition waiting time 130 minutes Tower To reduce the hold-up preparation time to the bottom tank H5 at the bottom,
If the bottom distillate is previously charged in H5, the start-up time can be shortened accordingly. In this case, it is necessary to add a line for charging the bottom distillate to the bottom tank H5.

If the preheating of the heat pump HP is performed when the working fluid is inserted into the side cooler SC as a preparation work of the heat pump HP, the preheating time of the heat pump can be reduced.
In this case, it is necessary to add a steam supply line to the side cooler SC.

As for the reduction of the time for charging the hold-up into the reflux tank H8 at the top, if the distillate at the top is charged in advance to the reflux tank H8 before the start of startup, the start-up time can be reduced accordingly. Also in this case, a line for charging the top distillate to the reflux tank H8 is added.

When the above-mentioned demonstration pilot plant is started up with such a modification of the line configuration and the improvement of the operation procedure, as shown in FIG. 19, the start-up time from the start of the start-up operation to reaching the steady-state operation is 168. In minutes.

Further, the operation timing of each valve can be clearly understood from FIG. If valve operation is not remote operation, but an operator is arranged at the site and this is to be performed, by comparing the timing chart of FIG. 19 with the line configuration, it is possible to assign valve operation to any operator's work. If it is good, if all the valve operation is left to one operator, considering the efficiency of valve operation on site, the optimal arrangement position of the valve, etc. A valve arrangement plan and the like can be easily performed. These can be easily performed because the correspondence between the plant design, the plant operation, and the timing thereof is clear by the sequence graph of the plant operation display device of the present invention.

(Sequence graph during shutdown operation) In the case of a distillation column system equipped with a heat pump HP
The shutdown operation procedure can be determined based on the sequence graph shown in FIG.

When performing the shutdown operation, first, the supply of the raw material and the supply of the steam of the reboiler are stopped. No steam is generated from the reboiler RB by stopping the supply of steam,
Finally, the heat pump HP is stopped because the process fluid can circulate when the heat pump HP is operating.

The procedure and timing (operation sequence) of this shutdown operation can be set in the same manner as in the first embodiment, and the sequence displayed on the display screen of the display device 44 using the sequence graph of the startup operation. The luminance of the tivation is gradually reduced,
It can be expressed by such a method.

(Sequence Graph at Emergency Stop Operation) As described in the first embodiment, in the case of the second embodiment as well, on the basis of safety, an emergency stop facility such as a seal gas is installed in the plant as necessary. Supply equipment, installation of a line for emergency removal of process fluid, etc. will be added. And
The operation sequence considering the added equipment may be set in the same manner as in the first embodiment. Also in this case, it can be displayed on the display screen of the display device 44 in the same expression as at the time of the shutdown operation. When the above-mentioned emergency stop equipment is added, the operation of this equipment may be performed by adding an emergency stop condition and the operation order of the equipment to the activation determination condition, and then performing the shutdown described above. Operation is the same.

The plant operation display device of the present invention is not limited to the distillation column systems of the first and second embodiments described above, and can be applied to various chemical plants. It should be noted that a method of expressing a sequence graph of other plant components can be exemplified in a few ways as follows.

FIG. 20 shows an evaporator, in which a process fluid in the can is heated and evaporated by a heat exchanger HEX1 using steam as a working fluid, and the evaporated process fluid is sent from the can to a line S80.
The liquid accumulated in the can flows out to line S81. FIG. 21 shows a sequence graph of this evaporator.

FIG. 22 shows a configuration of a self-heat exchange type reactor, in which a reactive mixed process fluid reacts inside the reactor R to generate reaction heat, and two heat exchangers HEX2 and HEX3 are used. It has. The heat exchanger HEX2 preheats the process fluid reacting in the reactor R using steam as a heat medium, and the heat exchanger HEX3
The process fluid heated to a high temperature by the reaction heat generated in the reactor R heats the process fluid itself flowing into the reactor R. FIG. 23 shows a sequence graph of a part of the self-heat exchange type reactor.

In addition, in the case where a phase change occurs at a node due to crystallization, flash phenomenon, pressurized liquefaction, and sedimentation separation, a method of expressing flow coupling and flow management conditions will be described below.

Crystallization Table 11 S80 (N1 → N2: L :: :) S81 (N2 → N3: L + S: −E: :) Table 11 shows that the process fluid S80 that is the liquid phase L is the node N2.
, Is partially crystallized and becomes a process fluid S81 including the solid phase S and the liquid phase L.

Flash Table 12 S82 (N5 → N6: L :: :) S83 (N6 → N7: L :-P: :) S84 (N6 → N8: V :-P: :) Table 12 shows the process of liquid phase L Fluid S82 is connected to node N6
The process fluid S8 is decompressed and partially vaporized to form a gaseous phase V.
FIG. 4 shows that the remainder becomes the process fluid 83 in the liquid phase L.

Pressurized liquefaction Table 13 S86 (N10 → N11: V :: :) S87 (N11 → N12: L: + P: :) Table 13 shows the process fluid S86, which is a gas phase V, at the node N11.
, And condenses into a process fluid S87 which is a liquid phase L.

Sedimentation separation Table 14 S88 (N14 → N15: L + S :: :) S89 (N15 → N16: L :: :) S90 (N15 → N17: L + S :: :) Table 14 shows that the fluid S88 is in a slurry state and the node N15 , Where it is separated into a liquid phase fluid L and a slurry phase (L + S), forming a fluid S89 and a fluid S90, respectively, and exiting N15.

Supply of Process Fluids A and B Even with the same chemical plant configuration, different operations are possible. For example, when supplying process fluids A and B in a tank 100 as shown in FIG. 24, different methods described below may need to be taken depending on the process to be performed.

In the first supply method, first, the process fluid A is supplied to the tank 100, and then, when the hold-up amount reaches the set value [> 100−H ^S ], the process fluid B is supplied to the tank 1
00 is supplied. FIG. 25 shows a sequence graph in this case, and a hold-up amount condition [> 100−H ^S ] is added to the activation determination condition regarding the valve V102.

In the second supply method, the process fluids A and B are supplied to the tank 100 at the same time. FIG. 26 shows a sequence graph in this case. On the condition that the preparation work for the process fluids A and B has been completed, this condition is added to the judgment conditions of each activation for the valves V101 and V102. Have been. Therefore, when the preparatory operations for the process fluids A and B are both completed, the valves V101 and V102 are simultaneously opened. The sequence graph of FIG. 26 can be rewritten to the one shown in FIG. 27 according to a conventional method of expressing a sequence graph. The expression of this sequence graph also indicates that the valves V101 and V102 are opened synchronously.

In the above embodiment, the sequence graph is displayed on the display screen of the display device 44, but may be printed out to the printer device 46. As shown in FIG. 2, the operation display devices 49 are dispersed for each plant and connected to a distributed control system (DSC). When necessary, the central electronic control device 40 transmits the operation display devices 49 to the plant side. The above-described sequence graph may be sent to constitute a part of the distributed control system.

(Effect of the Invention) As described in detail above, according to the plant operation display device of the present invention, the output device sets the same phase state based on the type of fluid flowing in each fluid passage and the phase state of the fluid. A certain fluid is sequentially traced from the system input node to the system output node, and these nodes are arranged and displayed in one direction along a flow direction when a flow occurs in each fluid passage. And / or operating conditions of the valve means are stored in advance, and it is determined by the sensor means whether or not the operating conditions of the respective transport means and / or the valve means are satisfied.
It is determined in order from the transportation means and / or the valve means on the system input node side whether or not the operating condition is satisfied, and when the operating condition is satisfied, the output device operates the transportation means and / or the valve means. In addition to highlighting what to do and highlighting only the fluid passages between nodes where flow has occurred due to the operation of these transport means and / or valve means, the plant line configuration, i.e., plant design and In addition, a sequence graph corresponding to the operation procedure and the timing of the plant can be displayed on the output device, and the plant operation can be performed extremely easily and reliably. If a simulation signal output unit is provided instead of the sensor unit and used as a simulation device, it is extremely useful as a design support tool. From the design stage of the line configuration of the plant, the operation procedure and its timing are grasped while grasping the operation procedure and its timing. Can be determined, and the improvement of the plant and the design of a complex plant combining a large number of units can be easily performed.

[Brief description of the drawings]

The drawings show an embodiment of a plant operation display device according to the present invention, and FIG. 1 is a block diagram showing a configuration of a distillation column system of a first embodiment to which the plant operation display device of the present invention is applied. FIG. 2 is a block diagram showing a configuration of a plant operation display device applied to the distillation column system, and FIG.
FIG. 4 is a diagram showing a flow sheet having a line configuration in a stationary state of the distillation column, FIG. 4 is a diagram of the flow sheet showing the distinction of the fluid transport means, and FIG. 5 is a pump required for the flow sheet of FIG. 6 is a diagram showing the arrangement position of the hold-up, and FIG. 7 is a diagram of a flow sheet having a line configuration necessary for a steady-state transition operation by a full recirculation method at a start-up operation. FIG. 8 is a diagram of a flow sheet having a line configuration necessary for a steady-state transition operation by a circulation system during a start-up operation. FIG. 9 is a diagram showing a node configuration of the distillation column system of the first embodiment. FIG. 10 is a sequence graph displayed on the display screen of the display device 44 of FIG. 2, and FIG. 11 is a diagram of the distillation column system of the second embodiment to which the plant operation display device of the present invention is applied. Combined FIG. 12 is a block diagram showing the configuration of the heat pump, FIG. 12 is a diagram showing the node configuration on the distillation column side of the second embodiment, FIG. 13 is a diagram showing the node configuration on the heat pump side, and FIG. 15 is a sequence graph when only the distillation column side of the second embodiment is operated, FIG. 15 is a sequence graph when only the same heat pump side is operated,
FIG. 15A is a sequence graph for a working fluid injection preparation work of a heat pump, FIG. 15B is a sequence graph for a working fluid circulation preparation work of a heat pump heat exchanger, and FIG. 15C is a circulation of a heat pump compressor. Sequence graph for line preparation work, Figure 15D is a sequence graph for heat pump drain line preparation work, Figure 15E is a sequence graph for heat pump air release preparation work, and Figure 15F is a heat pump FIG. 16 is a diagram showing a node configuration in which a distillation column and a heat pump are connected to each other, and FIG. 17 is a distillation column of the second embodiment. Figure 18 is a sequence graph of the system.
FIG. 19 is a timing chart showing operation times of valves and the like when the distillation column system is started up according to the sequence graph shown in FIG. 19; and FIG. 19 is a timing chart showing operation times of valves and the like when shortening the start-up time. FIG. 20 is a chart showing the structure of the evaporator, FIG.
FIG. 21 is a diagram illustrating a method of expressing a sequence graph of the evaporator portion, FIG. 22 is a diagram illustrating a configuration of a self-heat exchange reactor,
FIG. 23 is a diagram showing a method for expressing a sequence graph of the self-heat exchange type reactor part, and FIG. 24 is a block diagram showing a line configuration for supplying two types of fluids A and B to the tank 100. FIG. 25 is a diagram showing a method of expressing a sequence graph in a case where supply of fluid B is started after a set amount of fluid A is put into a tank, and FIG. 26 is a diagram showing a case where fluids A and B are simultaneously supplied to a tank. Diagram showing a method of expressing a sequence graph of FIG.
The figure shows the case where fluids A and B are simultaneously supplied to the tank.
A diagram showing an expression method equivalent to the expression method of FIG. 26, FIG. 28,
FIG. 2 is a block diagram for explaining a basic concept of the present invention. 40 ... Electronic control device, 42 ... Input device, 44 ... Display device, 46 ... Printer device, 49 ... Distributed control system, 52 ... Drive device, 54 ... Sensor device, C1, C2 ... Compression Machine, CD: condenser, D: tower, RB: reboiler, HP: heat pump, H0: raw material storage tank, H1:
… Raw material supply tank, H5 …… bottom tank, H8 …… reflux tank, H9 …… top product tank, H10 …… bottom product tank, P …… pump, SC …… side cooler, SH …… side heater, V ... Valve.

──────────────────────────────────────────────────続 き Continuation of front page (56) References JP-A-2-193300 (JP, A) JP-A-1-150815 (JP, A) JP-A-63-274987 (JP, A) JP-A-61-1987 11615 (JP, A) (58) Fields investigated (Int. Cl. ⁷ , DB name) B01J 19/00 G09G 5/00

Claims (10)

(57) [Claims] 1. Each point of a plant component is represented by a node, which has at least one system input node to which fluid is supplied from outside to the plant.
And at least one system output node from which the fluid flows out of the plant to the outside, and adjacent nodes are connected by fluid passages, respectively. In a plant operation display device of a plant in which a transport means and / or a valve means for generating a flow are disposed, fluids in the same phase state are determined based on a type of a fluid flowing in each of the fluid passages and a phase state of the fluid. An output device that sequentially traces the nodes from the system input node to the system output node and arranges and displays these nodes in one direction along a flow direction when a flow occurs in each fluid passage; Or, a storage means for storing operating conditions of the valve means in advance, and an operation of each of the transport means and / or the valve means Sensor means for determining whether or not the condition is satisfied; and, in order from the transport means and / or the valve means on the system input node side, it is determined whether or not the operating means is satisfied, and the operating condition is satisfied. In some cases, the output device highlights that the transportation means and / or the valve means should be operated, and only the fluid passage between the nodes where the flow has been generated by the operation of the transportation means and / or the valve means. And an output device control means for performing highlighted display. 2. Each point of a plant component is represented by a node, which includes at least one system input node to which fluid is supplied to the plant from outside;
And at least one system output node from which the fluid flows out of the plant, and adjacent nodes are connected by fluid passages, respectively, and a fluid flow is provided in a required portion of the fluid passages. A plant operation display device for performing a plant operation evaluation by simulating the plant, wherein an input device for inputting data by an external input operation; Based on the type of fluid that is input by the input device and flows from one node to an adjacent node through each of the fluid passages and the phase state of the fluid, the fluid in the same phase state is transmitted from the system input node to the system input node. Tracing sequentially to the system output nodes, these nodes are aligned along the flow direction when flow occurs in each fluid passage. An output device for arranging the display in one direction Te, is input by the input device, wherein the transporting means and /
Or storage means for preliminarily storing operation conditions of the valve means, simulation signal output means for outputting a simulation signal for simulating the operation conditions of the transport means and / or the valve means, and a system input node side. It is determined in order from the transportation means and / or the valve means whether or not the operation condition is satisfied based on the presence or absence of the simulation signal from the simulation signal output means. When the operation condition is satisfied, the transportation is transmitted to the output device. Output device control means for highlighting that the means and / or valve means should be operated, and highlighting only the fluid passages between nodes which are considered to have flow caused by the operation of these transport means and / or valve means; A plant operation display device comprising: 3. The apparatus according to claim 1, further comprising command means for outputting a pseudo command signal for manually activating or deactivating said specific transport means and / or valve means, and wherein said output device control means includes a pseudo-command from said command means. When the specific transportation means and / or the valve means are activated or deactivated in response to the signal, only the fluid passage between the nodes where the new flow has occurred is highlighted, and each of the above-mentioned respective flow means is changed due to the change in the flow. 3. The method according to claim 2, wherein when the operating condition of the transport means and / or the valve means changes, the fact that the transport means and / or the valve means should be operated is highlighted according to the changed operating condition. Plant operation display. 4. The system according to claim 1, wherein said plant component comprises components of a plurality of plant units.
4. The plant operation display device according to any one of items 3 to 3. 5. The plant component includes a heat exchange component, wherein one of said nodes is connected via energy exchange with a node of said heat exchange component, said heat exchange component being connected to said output device. The plant operation display device according to any one of claims 1 to 4, wherein the display is displayed in parallel. 6. A fluid flowing in a fluid passage connected to a node for transferring energy with a node of the heat exchange component changes a phase state before and after the node. Plant operation display device. 7. The plant operation display device according to claim 1, wherein the plant component includes a hold-up device, and is displayed as one of the nodes. 8. The plant operation display device according to claim 1, wherein said output device is an image display device. 9. The plant operation display device according to claim 1, wherein said output device is a printer device. 10. The plant operation display device according to claim 1, further comprising a drive device for driving said transport means and / or valve means, wherein said drive means is provided with said transport means and / or said drive means when said operating condition is satisfied. Alternatively, an automatic plant operation device characterized in that the valve means is driven and operated.