JPH04114732A - Apparatus for displaying operation of plant - Google Patents

Abstract

PURPOSE:To easily and certainly operate a plant by displaying a sequence graph wherein the planning of the plant and the operation procedure and timing thereof are allowed to correspond to each other on an output apparatus. CONSTITUTION:The operating conditions of each transport means 52 and/or valve means are respectively preliminarily stored in a memory means 48. Further, it is discriminated whether the operating conditions of each transport means 52 and/or valve means are formed by a sensor means 54. Furthermore, it is discriminated whether the aforementioned operating conditions are formed in order from the transport means 52 and/or valve means on the side of a system input node by an output apparatus control means 40 and, when the operating conditions are formed, emphasis display such that the transport means and/or valve means must be operated is performed on an output apparatus 44 and only the fluid passage between nodes where flow is generated by the operation of the transport means and/or valve means is subjected to emphasis display. As a result, the operation of a plant can easily and certainly be performed.

Description

Detailed Description of the Invention (Industrial Application Field) This invention is useful for smoothly and reliably performing plant operations such as start-up, shutdown, and emergency stop operations in a chemical plant using actual equipment. Alternatively, the present invention relates to a plant operation display device that is suitably used when evaluating plant operation by simulating these operations and operating the plant in a pseudo manner.

(Conventional technology and problems to be solved) Chemical plants are composed of column and tank equipment such as chemical reaction tanks, distillation columns, and heat exchangers, as well as transportation equipment, complicated piping, valves, etc. There are many components. Plant operations at chemical plant sites are studied down to the very minute details and compiled into work standards and the like. These overall plant operations are typically considered based on three types of information:

First, the first information is information regarding the structure of the chemical plant. This information includes, for example, the type, height and location of the equipment that makes up the chemical plant, the connection state between equipment, the equipment required to perform unsteady operations such as startup, the initial state of the plant and the final target state, etc. It will be done. Second
The second information relates to procedures for operating the device.

The third information is information regarding the timing for implementing the turn procedure.

In plant design, for example, consideration of start-up plant operating procedures has conventionally typically started from the time the basic design (basic flow sheet) is completed. This will be explained with reference to Figure 28.
First, the designer keeps the operating procedure in mind and decides on the necessary piping design, pumps, main valve placement, etc. based on that. Next, there is a problem in that it is often difficult for other designers to understand the relationship between one designer's intention of the operating procedure and the design, whether the startup operating procedure is considered or not. Additionally, because plant designers and operators are usually different, operators may not necessarily understand the designer's approach to operating procedures, and conversely, the designer may not necessarily understand the operator's desired approach to operating procedures. The problem is that there are too many.

These problems arise from the fact that although process design, operating procedures, and their execution timing are closely related, there was no way to clearly link them. More importantly, it is desirable that such operation timings are originally registered in the control system for plant operation in the distributed control system (DC3) and sequentially displayed on the display screen of the operation support equipment. The design shown in FIG.
Unclear expressions of the relationships among the four, such as operating procedures, are causing various problems.

For example, at the design stage, PFD (Process F
lowsheetDiagram) and P&I
D (Piping and Instrument
Even if the tation diagram) is completed, it still takes a lot of time and effort to express procedures such as startup and shutdown in a manual. The process of creating manuals has not yet been systemized, and the designer in charge confirms the procedures he or she has in mind by following them in order on the diagram of the completed operating procedure. For this reason, a huge amount of time is required, errors may occur, and the information is written using various expressions that are not uniform, so users (especially operators)
This poses a problem that is extremely difficult for people to understand.

Furthermore, conventionally, the work of converting a procedural expression into an operation support screen using a computer has been considered as a completely separate work, and this conversion work also requires a huge amount of effort and time.

In addition, chemical plants are often remodeled, and in this case, it is also necessary to consider changes in operating procedures and execution timing at the same time. However, in the past, it was not possible to clearly express changes in plant equipment and corresponding changes in operating procedures, so it took a huge amount of effort and time to accurately implement changes. was necessary.

In such a case, it is also necessary to change the operation support screen at the same time, but this change also requires a considerable amount of time.

Furthermore, because the relationship between operating procedures and execution timing could not be clearly expressed at the design stage, valves, etc. were often designed in inappropriate positions, and plants designed in this way This resulted in requiring a great deal of effort and complicated operations.

Furthermore, for example, if you want to shorten the time required for startup, you may want to consider what kind of preparation equipment and facilities are required, or how to change the operating procedures and timing. It was an extremely difficult problem.

In addition, if a chemical plant is composed of similar units or composite units that integrate multiple units, the operating procedures for operating each constituent unit alone and the operating procedures for individual units when combined are provided. The differences between the two systems were unclear, and it was often difficult to confirm whether the operating procedures for operating each individual unit alone could be applied to a combined unit plant. .

Until now, research on expressing plant operating procedures has not been sufficient, or only a few have been known.

For example, an operating procedure determination method (J ,R.Rivas
and D, F, Radd.

AIChE J, vol, 20(2), 320
-325 (1974); O'Sbima.

J, Chem, εng, Japan, vol, 1
1(5), 390-395 (1978)), is called the automatic startup procedure synthesis method, which strictly hierarchizes the functional definition of component units and combines the functions sequentially using a knowledge engineering approach to improve plant operation. Operation procedure determination method for determining procedures (Hwang Kye-suk, Tomita Shigeyuki, Oshima Eiji, Chemical Engineering Journal, vol. 14(6), 728-73
8 (1988)) and an operating procedure determination method (R, Lakshmana
n and G, 5tephanopoulos.

Compute, Chem, Engng, vol.
12 (9/10), 985-1002 (1988)
; R, Lakshmanan and G, 5te
phanopoulos.

Compute, Chem, Engng, vol.
12 (9/10), 1003-1021 (1988
); R, H, Fusillo and G, J, P
powers, Compute.

Chem, Engng, vol, 12 (9/10
), 1023-1034 (1988)), etc. are known.

These conventional methods for determining plant operating procedures attempt to determine operating procedures based on a given plant structure, and are basically expressive of procedures in text, which has difficulties in expressing things such as parallel operations. .

In addition, since the plant structure and operating procedures are not expressed in a clear relationship, there is a drawback that when changing the plant structure, it is difficult to understand the correspondence between the parts of the structure that should be changed and the parts that should be changed in the operating procedures. Is there a need to consider operating procedures?

The present invention was made to solve the above-mentioned problems, and it is possible to clearly express the relationship between process design, operation, and its timing, and at the same time, the operation expression can be displayed on a screen for supporting plant operation. The purpose of the present invention is to provide a plant operation display device that can be used as a plant operation display device.

(Means for Solving the Problems) According to the present invention, each point of a plant component is represented by a node, and fluid is supplied to the plant from the outside to these nodes. and at least one system output node through which fluid flows out of the plant, and each adjacent node is connected by a fluid passage, and each of the adjacent nodes is connected to the other by a fluid passage. In a plant operation display device for a plant in which a transportation means and/or a valve means for creating a fluid flow are disposed in the middle of a fluid passage at a required location, the type of fluid flowing in each fluid passage and the phase state of the fluid are Based on this, fluids in the same phase are sequentially traced from the system input node to the system output node, and these nodes are arranged and displayed in one direction along the flow direction when a flow occurs in each fluid passage. storage means for storing in advance operating conditions for each of the transportation means and/or valve means; and a sensor for determining whether or not the operating conditions for each of the transportation means and/or valve means are satisfied. It is determined whether or not the operation condition is satisfied in order from the means, the transportation means and/or the valve means on the system input node side, and when the operation condition is satisfied, the pressure device is activated by the transportation means and/or the valve means on the system input node side. or an output device control means for highlighting that the valve means should be operated and highlighting only the fluid passage between the nodes in which a flow has occurred due to the operation of the transportation means and/or the valve means. A plant operation display device is provided which is characterized by:

The plant operation display device may be provided with a driving means for driving the transportation means and/or the valve means, and when the operation condition is satisfied, the driving means may be caused to operate the transportation means and/or the valve means. .

According to another aspect of the invention, each point of a plant component is represented by a node, including at least one system input node through which fluid is supplied to the plant from outside; A means of transportation that includes at least one system output node that flows out from the plant to the outside, and in which adjacent nodes are connected to each other by fluid passages, and that creates a fluid flow in the middle of the fluid passage at a required point among these fluid passages. and/or an input device for inputting data through an external input operation, and an input device for inputting data through an external input operation, in a plant operation display device for evaluating plant operation by simulating operation of the plant in a plant in which a valve means is installed; Based on the type of fluid flowing from one node to an adjacent node through each fluid passage and the phase state of the fluid, fluid in the same phase state is transferred from the system input node to the system output node. an output device that sequentially traces the nodes up to and displays the nodes arranged in one direction along the flow direction when a flow occurs in each fluid passage; a storage means for storing operating conditions of the respective means in advance; a simulation signal output means for outputting a simulated signal that simulates the operating conditions of each of the transport means and/or the valve means; and a transport means on the system input node side. and/or in order from the valve means, it is determined whether or not the operating condition is satisfied based on the presence or absence of the simulated signal from the simulated signal 8 force means, and when the operating condition is established, the output device is sent to the transportation means. and/or output device control means for highlighting that the valve means should be operated and for highlighting only the fluid passages between the nodes where flow is deemed to have occurred due to the operation of these transportation means and/or the valve means. A plant operation display device is provided.

(Function) In the present invention, plant operations such as plant startup are basically performed by
Recognizing that the goal is to create a fluid flow in the target state between each node by performing "flow management" and "hold up management," the fluid in the same phase state is transferred from the system input node to the system 8. This is based on the knowledge that by sequentially tracing all the way to the canode and displaying them in one direction along the flow direction, the plant operation procedure and its timing can be displayed in accordance with the line configuration of the plant.

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

The plant operation display device of the present invention is provided with a driving means for driving the transportation means and the valve means, and when the operating conditions are met, the transportation means and the valve means are driven by the driving means, thereby enabling automatic operation. .

Further, the plant operation display device of the present invention is configured to include, instead of the sensor means, a simulated signal output means for outputting a simulated signal that simulates the operating conditions of each transportation means and/or valve means, and the system Starting with the transportation means and/or valve means on the input node side, it is determined whether or not the operating condition is satisfied based on the presence or absence of a simulated signal from the simulated signal outputting means, and when the operating condition is established, the a-blade device is Highlighting that the vehicle and/or valve means should be operated and highlighting only the fluid passages between nodes where flow is considered to have occurred as a result of the operation of the vehicle and/or valve means is a design advantage. It can also be used as a simulation support device as a support tool.

(Example) Embodiments of the present invention will be described in detail below based on the drawings.

First, as a first embodiment of the plant operation display device according to the present invention, an example in which the plant operation display device is applied to a distillation column system will be described. Since this plant operation display device has a function as a plant process design support tool, it will be explained starting from the plant design procedure.

Line configuration during steady operation It is assumed that the line configuration during steady operation, plant operation, and internal conditions have already been determined at the basic process design stage. In other words, the distillation column has a column section, a heating reboiler and a condenser that are heat exchange components as the main components, and the line configuration of these is expressed by the plot plan shown in Figure 3. . In the figure, the arrows indicate the direction of flow, the solid line (-) represents the flow of liquid, the thick solid line (-) represents the flow of gas-liquid mixed phase, and the broken line (on the negative side) represents the flow of gas. There is. Moreover, the double line (-) represents the flow of heat. ○ indicates the fluid inlet point, outlet point,
and a bonding point. In this case, the plant internal conditions such as flow rate, composition, pressure, temperature, and fluid phase are also determined as simulation data during steady state. In addition, the selection prerequisites and operating conditions for each component,
In addition to determining preparation conditions, conditions such as fluid properties and reactions, such as fluid reactivity (especially related to polymerization), explosiveness, flammability, toxicity, and corrosivity, as well as crystallization and solidification. Conditions such as ease of spreading, scale generation, and ease of slurrying are also given.

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

The concept of "flow management" has two meanings; the first is the concept of fluid condition management, that is, the management of flow creation, and the second is the concept of valve operation, as will be described in detail later. It is a concept related to timing management of flow creation centered on. Here, to explain the former flow management, we will consider how to create a steady state fluid flow as shown in the plot plan in Figure 3, and the phase state of the fluid. When the phase changes, a device is needed to generate heat exchange (heat exchange) and a large change in pressure (flash, etc.), and such devices should be considered.

Therefore, the outline of the plot plan shown in Figure 3 was created at the PFD design stage, and the types and installation locations of the raw material tank, condenser, reflux tank, reboiler, bottom tank, etc. were determined as known information. At the same time, by rewriting the locations of the population point, outlet point, and connection point (respectively indicated by circles) in the flowchart in Figure 3, a fluid flow is created using an external force such as a pump or ejector. Distinguish from those that are not. FIG. 4 is a flowchart showing the distinction between fluid transport means,
In this example, (G) is a device that can transport fluid by gravity, (S) is a device that can transport fluid by using the siphon effect, and (S) is a device that can transport fluid by reduced pressure 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, the fluids classified with the above-mentioned symbols and the fluids other than the gas phase require transportation means using an external force in order to create a flow of the fluids. Transportation means using this external force include compressors, pumps,
A means for transporting fluid by applying high pressure to the fluid, such as a method for cooperating an ejector, a throttle valve, and a heating operation, and a method for cooperating a decompression pump, an ejector, a throttle valve, and a gas condensing operation, etc. There are means for transporting the fluid under reduced pressure, but an appropriate method may be selected depending on the type, properties, etc. of the fluid.

In this embodiment, as shown in FIG. 5, a pump P1 is installed between the raw material supply inlet point and the raw material supply stage of the distillation column, a pump P2 is installed between the reflux tank of the condenser and the top of the distillation column, and a pump P2 is installed between the condenser reflux tank and the top of the distillation column. A pump P3 is installed between the reflux tank and the distillate outlet.
A pump P4 is also 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 a means of transportation based on such external force.

Next, the valves may be selected, or in the case of the distillation column system of the embodiment, the valves may be arranged according to, for example, the following rules.

(Rule 1) A valve is placed on the discharge side of the pump in consideration of pump maintenance, etc. However, in the case of a metering type pump, the valve may be omitted.

(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) Place a valve at the inlet or outlet of the cooling water of the condenser.

(Rule 4) Place a knob on the outflow line from the tank.

(Rule 5) If multiple lines are connected from the tank, at least one control knob (CV) is required.

FIG. 5 shows the arrangement of valves according to the rules described above. It goes without saying that the type of valve etc. depends on the application and the type of fluid.

(Placement of hold-up) During steady plant operation, the upper hold-up operation is not necessarily required, but when unsteady processes such as startup and shutdown operations are taken into account, the hold-up is used to perform plant operation procedures. plays an important role in determining timing. In other words, the above-mentioned "flow management" is performed by arranging this hold-up at a required position and controlling its amount. especially,
To ensure stable transport by the pump, it must be placed upstream of the pump. Additionally, in general, phase changes in fluids do not occur strictly at a constant speed, but are accompanied by fluctuations, so a hold-up is installed at a position before the phase change to provide residence time for the flow and absorb fluid fluctuations. . It goes without saying that a hold-up is provided for the purpose of storing the raw material liquid, the bottom distillate (bottom product), and the top distillate (top product).

Figure 6 shows the arrangement of hold-ups from the above-mentioned perspective, with the raw material supply tank H1 being either the bottom tank H5 at the bottom of the distillation column, the reflux tank H8 at the distillate outlet side of the condenser, or the column There is a top product tank H downstream of the top distillate outlet.
A column bottom product tank HIO is disposed downstream of the column bottom distillate outlet. In Figure 6, these tanks are marked with a ◎.

Line configuration during startup operation Next, consider the line configuration during startup operation and add the necessary lines. The so-called total reflux method, circulation method, dripping method, etc. are known as operating methods during startup, but when considering the line configuration during startup, it is important to consider economic aspects and the viewpoint of shortening startup time. Therefore, it is sufficient to consider the first two methods, namely, the total reflux method and the circulation method.

(Line configuration of total reflux system) In the total reflux system, the raw material supply line, the top distillation line, and the top distillation line are shut off, and the top and bottom distillates in the reflux tank H8 and bottom tank H5 are This method involves refluxing all fluids until the composition of the effluent reaches the target composition.

Each line is equipped with valves Vl, V4 and V6 to shut off the line, so as shown in Figure 7, this method does not require any new equipment and can be done simply by opening and closing the valves. can be dealt with.

(Line configuration for circulation system) In the circulation system, the distillate at the top and bottom of the tower is transferred to the raw material supply tank H.
This method returns it to 1 and does not let it out of the system.

In the case of this method, it is desirable to switch to the above-mentioned total reflux method once the top and bottom distillates reach a predetermined composition (temperature), but the circulation method is used until the target composition (temperature) is reached. You can start up with .

As auxiliary lines, return lines S20. S21 is required.

The raw material supply tank H1, the top product tank H9, and the bottom product tank HIO are all above ground, so tank H
9. If the HIO is to be returned to the raw material supply tank H1, each of these return lines requires a pump, but as shown in FIG. 8, the valves V4. Switching valves SVI and SV downstream of V6
2 and branching the return lines S20 and S21 from the valves SVI and SV2, the pump P3. P4
This allows the distillate to be circulated to the raw material supply tank H1.

The basic plant design has been completed through the above steps, but it is more preferable to consider the inert gas replacement line and bypass line during startup operations,
Furthermore, it is also necessary to consider the line configuration during emergency stop operations.

FIG. 9 is a flow sheet of the distillation column system of FIG. 8 designed as described above, with nodes, process fluids, and valves labeled respectively. A node representing each point of a plant component can be a pipe connection point, a part of a unit, e.g. a heat exchanger, which has no connection points with other pipes, or a unit that utilizes an external force, e.g. a pump. It includes internal nodes such as units and hold-ups, system input nodes where process fluids and working fluids are supplied to the plant from the outside, and system output nodes where the plant flows out to the outside. A process fluid is a fluid flowing between adjacent nodes.
Although indicated by a symbol S1 or the like, this symbol can also be considered to indicate a fluid passage through which fluid flows between the nodes. Note that the "fluid passage" referred to here may refer to not only piping such as pipes but also tower and tank equipment as passages. A feature of the present invention is that the process fluid and the fluid passage are made to correspond to each other in this way.

Note that a supply line to the raw material supply tank H1 is added, and the system input node, that is, the raw material storage tank is HO, and the pump and valve disposed on the supply line so are po and v, respectively.

It is shown by . The raw material storage tank H (l) also includes a mobile tank device such as a tank truck.

FIG. 1 shows a block diagram of the distillation column system designed as described above, which is composed of a column section D, a reboiler RB, a condenser CD, a storage tank group, and pumps and valves. The explanation of this configuration can be easily understood since the same reference numerals are given to the constituent elements corresponding to those in the flow sheet shown in FIG. 9, and detailed explanation thereof will be omitted.

The distillation column system of the first embodiment is equipped with a plant operation display device shown in FIG. 2, which displays plant operation procedures and operation execution timing,
Plant operations such as startup operations are performed while monitoring these displays.

Plant operation table - device configuration The plant operation display device includes an electronic control unit (ECU) 40 that controls the operation of the entire device, an input device 42 that inputs the plant configuration and plant operation command signals by key operation or switch operation, and an electronic control unit (ECU) 40 that controls the operation of the entire device. A display device 44 displays the calculation results of the control device 40 on a screen, a printer device 46 prints out the calculation results of the electronic control device 40, and stores calculation procedures (programs) executed in the electronic control device 40. External storage device 48, electronic control device 40
an I10 interface 50 that controls input and output from the
Through this I10 interface 50, a drive signal from the electronic control device 40 is used to open and close the valve,
It is composed of a drive device 52 that operates the pump, a sensor means 54 that detects the liquid level position of the hold-up, the temperature inside the column, pressure, line flow rate, etc. and supplies this to the electronic control device 40 via the I10 interface 50. has been done.

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

Creation of Sequence Graph In explaining the operation of the plant operation display device, first, the procedure for creating a sequence graph, which is the basic technical idea of the present invention and is displayed on the screen of the display device 44 of the plant operation display device, will be explained.

(Expression of fluid coupling and flow management conditions) Plant operations in chemical plants, especially startup procedures, are basically conducted by performing "flow management" and "hold-up management" while observing safety and quality conditions. I think it will be decided. That is, the basic technical idea of the present invention is based on the ideas of "flow management" and "hold-up management."

“Flow management” refers to the fluid paths between adjacent nodes, starting from the system input node and ending at the system a canode, when starting up a chemical plant from an initial state to a target steady state. This means managing the state of the fluid in the line to create the target flow state from the initial state. As a method for expressing the fluid flow in a plant, the present invention focuses on the phase state of the fluid and sequentially traces fluids in the same phase state from a node on the system input side to a node on the system output side. This is based on the knowledge that operating procedures can be expressed naturally.

By the way, when fluids in the same phase state are traced from a node on the system input side, if the fluid changes its phase state midway, the fluid cannot be traced from that point onwards. A phase change occurs when a fluid receives or receives heat or a large change in pressure, so when there is such heat transfer or a large change in pressure, the fluid that has undergone a phase change is considered to be continuous at that position. Then, the fluid in the changed phase state is traced toward the system output node.

``Hold up management J is necessary to stably operate the plant, especially the operation timing, by placing hold ups at important points in the plant and managing the amount of hold up.

That is, it is used as a valve operation start condition and a valve operation stop condition, such as starting valve operation when the hold-up amount of fluid flowing into the hold-up reaches a preset determination value. This discrimination value may be changed depending on the plant state and may take several appropriate values. For example, the determination value for operating the pump may be set to a different value from the determination value after reaching a steady state. In other words, the discriminant value of the hold-up amount is considered to be a variable related to the time required for startup and quality control.

Based on the above idea, if we write out all the phase states of the process fluid flowing between adjacent nodes in the flow sheet shown in Figure 9, that is, the fluid coupling and flow management conditions, it can be expressed as shown in the table below. .

(Left below) A few explanations of what is meant by the expressions of fluid coupling and flow management conditions shown in Table 1 are as follows.

Process fluid S1 is a liquid flowing from node l-1 (raw material supply tank H1) to node 3 (distillation column supply stage), and the flow is created by operating pump PI. It begins when the state is reached.

Process fluid S3 is a liquid flowing from node 3 to node 4, and the flow is without external forces.

Process fluid S6 is a gas-liquid mixed phase (L-'-V) flowing from node 6 to node 4, and changes from liquid to mixed phase (L↓V) before and after node 6. Requires heating source-I-H2.

The process fluid SIO is in a liquid state flowing from node 7 to node 8-H (reflux tank 8), and changes phase from gas phase V to liquid phase before and after node 8-H.
H requires an external cold source - El.

Process fluid S15 flows from node 17 to node 1O-1
(The liquid flowing into the bottom product tank I(-10) is
It begins when state (2) is reached.

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

For example, the condition (ON condition) under which the process fluid SO may be allowed to flow is when the hold up amount of the hold up H1 is smaller than the set value (1-)1s).

At this time, the pump PO is operated and the valve v
Open O. Further, the hold up amount of the hold up H1 becomes larger than the set value (1-Hs), and
The hold up amount of hold up H5 and H8 is
If both are greater than the set values (5-H") and (8-Hs), the pump PO is stopped and the process fluid SO is turned off.
Make it FF. Note that if time is required to prepare the pump, the pump PO should be operated in a standby state.

The ON condition for the process fluid S1 is when the hold up amount of the hold up H1 is smaller than the set value (1-H"). When the ON condition is met, the pump Pi is operated and the valve V1 is opened. Make it.

Process fluid S3 is always in the ON state. That is, when fluid is supplied to the node 3, the flow of the process fluid S3 is created by gravity fall.

Regarding the process fluid S6, when the hold-up amount of the hold-up H5 becomes larger than the set value (5-Hs), steam is passed through the reboiler to create a flow of the process fluid S6. Note that the timing for supplying steam to the repoiler is to warm it up at the same time as the start-up operation begins.

Table 3 shows operating conditions for switching from startup operation to steady operation. When the steady operation transition condition indicated by #1 is satisfied, the switching valve SV2 is switched to the state (2), and the process fluid S15 flowing from node 17 to node 10 is turned on. When the steady operation transition condition indicated by #2 is satisfied, , the switching valve SVI is switched to the state (2) to turn on the process fluid 313 flowing from the node 18 to the node 9. In addition, steady operation transition condition #
For L#2, for example, it is necessary that each composition (temperature) of the distillate at the bottom and top of the column reaches its respective set value (target value).

Once the above fluid coupling and flow management conditions are prepared,
These pieces of information are input to the electronic control device 40 by key operations on the input device 42. After inputting all of this information, when a calculation start command signal is keyed into the electronic control device 40 via the input device 42, the electronic control device 4
0 is Table 1 entered according to the memorized calculation procedure
A sequence graph is created based on the information shown in Table 3 and displayed on the screen of the display device 44. FIG. 1θ shows a sequence graph during a startup operation in which the results of calculations performed by the electronic control unit 40 are displayed on the display device 44.

Sequence Graph Next, the calculation method used by the electronic control unit 40 to create this sequence graph will be explained based on the calculation results shown in FIG. 1O.

By the way, it is difficult for those skilled in the art to create a program that is executed by the electronic control unit 40 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. Since it is easy and there are various ways to create a program, its contents will not be explained in particular. That is, the present invention is characterized in that a sequence graph in which the designed plant configuration, operating procedures, and their execution timings are expressed in one flow sheet is displayed on the screen of the display device 44 based on the calculation results of the electronic control device 40. This is not a feature of the computer software creation procedure itself.

In the sequence graph of the present invention, each point of a plant component is represented by a node, which is sequentially traced from the system input node to the system 8 node based on the phase state of the fluid, in one direction on the screen, that is, in the embodiment. They are arranged along the flow direction from the top to the bottom of the screen. In the sequence graph of FIG. 10, the input node of the distillation column main body is one of the nodes 0-H, which corresponds to the raw material storage tank HO. There are two output nodes, nodes 9-H and 10-H, which correspond to the top product tank H9 and the bottom product tank HIO.

In addition, each input node 14.11 and each output node 16.13 are also connected to a reboiler and a capacitor, which are heat exchange components.
They each have

This sequence graph is obtained by converting Tables 1 to 3 described above into a flow sheet using the following procedure. First, the electronic control unit 40 sequentially traces fluids in the same phase state from the system input node to the system output node based on the input information in Table 1. More specifically, starting from a process fluid SO that is in a liquid phase, this fluid in a liquid phase enters an input node, node O.
It starts from H and reaches the hold-up node 5-H via node 1-)1→node 3→node 4. At this node 5-H, the fluid branches into two, one of which becomes the process fluid S14 and reaches the node 17. At node 17, which is switching valve SV2, this fluid becomes either process fluid S15 or S21 depending on the switching state of the valve, and reaches node 10-H, which is the output node, or node l on the input side. - Returned to H.

The other fluid branched at the hold up node 5-H is
It becomes process fluid S5 and reaches node 6.

At node 6, a phase change occurs due to the heat (+E2) from the reboiler, resulting in a mixed phase of gas phase V and liquid phase, but according to the rules, if heat is exchanged, the process fluid is continuous. be considered. This multiphase fluid S6 proceeds from node 6 to node 4. The multiphase fluid S6 is transferred to the node 4, where the fluid in the liquid phase becomes the process fluid S4 described above and returns to the hold-up node 5-H, and the fluid in the gas phase becomes the process fluid S7 and is held up by gravity (density difference). It rises upward and reaches node 7 of the capacitor via node 3→node 2. During this time, the gas phase state is maintained, so the flow is represented by a broken line (--1-).

At the node 7, heat (-El) is removed by the cooling water, causing a phase change from the gas phase to the liquid phase. In this case as well, the process fluid is considered to be continuous as there is an exchange of heat.
The process fluid becomes SIO and reaches the hold-up node 8-H, which is the reflux tank H8. At the node 8-H, the fluid is branched into two, one of which becomes a liquid phase process fluid Sll and is returned from the node 2 to the node 3. The other fluid branched at node 8-H becomes process fluid S12 and reaches node 18. This fluid becomes either process fluid S13 or S20 depending on the switching state of the switching valve SVI, and reaches the output node 9-H or is returned to the input side node 1-H, respectively.

From the input node 14 of the reboiler, the steam fluid S18 in a gas phase reaches the node 15 via the valve v5, where it undergoes a phase change and reaches the eight canodes 16.

From the input node 11 of the capacitor, the cooling water fluid S16 in a liquid phase reaches the node 12 via the valve 3, where it exchanges heat and reaches the output node I3.

Here, various symbols in the sequence graph will be explained. Structure nodes, including hold-up ellipses, are indicated by circles. What is included in the structure node is as described above (see FIG. 9). In addition, hold-up management and various judgment conditions are described in [ ]. Various conditions can be arbitrarily added to this judgment condition, such as not only the hold-up amount and liquid height, but also the conditions for transition from startup to steady operation. The judgment conditions for the example are:
As mentioned above, it goes without saying that all considerations have been made at the stage of creating Tables 1 to 3, and the initial state of the valve is normally closed, but depending on the operating procedure, it may change from closed to open to open. Since there are possible operating procedures such as closing..., the symbol (CLO3E) is added to indicate the closed state of the valve. This symbol can be displayed by changing the brightness of the screen, such as being dark when the bulb is closed and bright when it is open.

In Fig. 1θ, the progress of the flow is indicated by arrows, but broken lines (--1~) are drawn in the direction perpendicular to the flow so as to interrupt the flow. This dashed line indicates the activation of a valve, heating or cooling, pump or compressor. If marks exist for all nodes and judgment conditions that have flows that are direct inputs for this activation, the operation can be started. For example, the first
The activation that appears first from the top of the flow shown in diagram O indicates the start of operation of the valve vO, and the condition for determining whether to open the valve in this activation is that the hold-up amount of the hold-up H1 is less than or equal to the set value 1-Hs. This is a certain condition, the pump PO is prepared, and when this condition is met, all flows that are directly input to this activation will be marked, and the valve vO
This means that the valve opening operation may be performed. In particular, when temporal valve operation such as valve opening speed is important, the activation symbol is indicated by a double dashed line (...).
A temporal condition can also be placed between the double dashed lines.

The above-mentioned flows include not only material flows such as gas, liquid, and multiphase flows, but also heat flows (indicated by the double line - as described above) and information flows. The information flow includes information that indicates the establishment of judgment conditions for hold-up management, judgment conditions related to the state of the process flow, etc. The dashed line connecting the judgment conditions and activation shown in [ ] ) and the direction of flow is indicated by an arrow. Material and heat flows are shown with the same types of lines as described above (see Figure 3), but they can also be colored or represented with other line types.

The above mark indicates a node where a flow exists, or when a judgment condition related to hold-up management or process flow status is met, the screen display of that node or judgment condition is displayed.
As described above, this is to change the brightness to brighter for display. Instead of changing the brightness, the color may be changed. Typically, when a valve is closed by a valve operation, there is no downstream material flow (heat flow) through the valve. That is, the marks in the nodes associated with material flow (thermal flow) that are associated with the flow out of the activation of that valve operation disappear.

However, if a material flow recycling loop exists downstream of the activation for the closed valve, the material flow within that loop may continue; The marks of the nodes within will not disappear.

The above-mentioned sensor means 54 constantly monitors whether or not the judgment conditions regarding the hold-up management and process flow state described above are satisfied. That is, the sensor means 54 constantly detects the liquid level position of the hold-up, the amount of hold-up, the temperature and pressure of each chamber in the column, the composition of the distillate, etc., and sends the detection signal via the 110 interface 50. It is supplied to the electronic control device 40. The electronic control unit 40 determines from these supplied detection signals whether or not the above-described judgment conditions regarding the hold-up management and the state of the process flow are satisfied.

Now, we will explain the procedure and timing for starting up the distillation column system while monitoring this sequence graph. Note that, as an initial condition, the raw material is stored in the raw material storage tank HO, but the hold up amount of other hold ups is 0. It is also assumed that the preparatory work for starting up the pump and reboiler RB has been completed. and switching valves SVI and S
It is assumed that both V2 have been switched to the state (1). All pumps and valves can be operated remotely by outputting an open drive command signal from the electronic control device 40 to the drive device 52 by operating a switch or key on the input device 42 of the plant operation display device. shall be taken as a thing. However, it goes without saying that these pumps and valves may be operated manually by an operator as appropriate, and they may be manually operated when turned on, and automatically stopped by the electronic control device 40 when turned off or emergency stopped. You may also do so.

First, when the operation switch of the distillation column system is turned on, the sequence graph displayed on the screen of the display device 44 shows holdup 0-H and management conditions (<1
-Hs) is marked. Additionally, nodes 14 and 11 are also marked and highlighted. After confirming the display status of the mark on the sequence graph, the operator turns on the operation switch of the pump PO. Note that the valve v5 of the repoiler RB is opened when the hold-up amount of the bottom tank H5 reaches a set value. Next, by opening the valve V3, the node I at each point of the capacitor CD is
f, 12.13 are all marked. These valves V3. V5 may be operated in the preliminary stage if there are no safety and equipment issues.

On the other hand, due to the operation of pump PO, this pump node PO
can also be marked. Therefore, all the flows toward the activation of the valve VO are marked, and all the judgment conditions for the valve VO are satisfied, and the valve VO can be opened. Therefore, the electronic control device 40 outputs an opening drive signal to the valve vO via the drive device 52 to open the valve vO. As a result, the raw material fluid is transferred from the raw material storage tank HO to the raw material supply tank H.
1, 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 raw material fluid is supplied to the raw material supply tank H1. At this time, pump PL is operating in a standby state, and pump PI is also marked. When the hold-up amount of the tank H1 reaches the set value, a mark is added to the judgment condition, and all flows toward activation are marked, so the electronic control unit 40 uses the drive unit 52 to ＼Output an opening drive signal to the valve v1 to open the valve Vl.

This results in flow being created until the next activation of valve V6. V4° Each node up to each activation for V2 is marked.

In reality, unless the hold-up amount of the bottom tank H5 reaches around the set value, the flow of the process fluid S6 by the reboiler RB will not occur, so the fluid that has fallen into the bottom tank H5 of the distillation column is It will be stored in tank H5.

When the hold-up amount of the bottom tank H5 reaches the set value, a mark is added to the judgment condition. After confirming this mark, the operator operates the pump P4, and all flows toward each activation related to V2 are marked, and the valve V6 is opened. When valve V6 is opened, the distillation column system has not yet reached a steady state, so switching valve SV is opened.
2 is maintained in the (1) state, and the fluid from the photom tank H5 is returned to the raw material supply tank H1 via the reflux line S21.

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

Activation regarding valve v4 and valve V2 both waits until the hold-up amount of tank H8 reaches a set value (8-H'). When the hold-up amount reaches the above-mentioned set value, the pump P3 is operated to open the valve V4, and the top distillate in the reflux tank H8 is transferred via the switching valve SVI, which has been switched to the (1) state. While returning the part to the raw material supply tank H1, operate the pump P2 to open the valve V2,
A portion of the overhead distillate in reflux tank H8 is returned to the top of the tower.

Then, the hold up amount of the reflux tank H8 reaches the set value, and hold up nodes 5-H and l-H
When all the conditions for determining that the hold up amounts of the valves are also equal to or larger than the set values are satisfied, the valve vO is closed and the system enters a standby state for transition to a steady operation using the circulation system.

The sensor means 54 constantly monitors the composition, temperature, etc. of the bottom and top distillates, and monitors the composition (temperature, etc.) of these distillates.
Reaching the target value and transitioning to steady operation #1
If #2 is established (YES), the corresponding switching valves Svl and Sv2 are switched to the (2) state, and the top and bottom distillates that were being circulated to the hold-up node 1-H are Storage in tank H9 and tank HIO is started, and steady operation is started.

Thus, in the initial stage of startup operation, the process fluid is circulated by the circulation method until the bottom and top distillates of hold-up nodes 5-H and 8-H reach the target composition (temperature). , the startup time has been shortened.

In addition, in order to further shorten the startup time, when the composition (temperature, etc.) of the tower bottom and tower distillate reaches a set value by the sensor means 54, the valves Vl and V4 are activated.
, and V6 can be shut off to reflux the distillate from the hold ups H5 and H8 at the bottom and top of the column in a total reflux mode. In this case as well, when the compositions (temperature, etc.) of the bottom and top distillates reach the target values, the above-mentioned valves V1, v4, and v6 are opened again, and the switching valves Sv1 and SV2 are opened again. (2)
state and transition to normal operation.

Furthermore, the start-up time can be further shortened by charging the product into the hold ups H8 and H5 at the top and bottom of the column before starting the start-up operation, and starting the start-up operation in a total reflux mode.

Shutdown Sequence Graph The above-mentioned startup operation sequence graph can be used as is when performing a system stop operation (shutdown operation) from the steady operation of the distillation column system. Considerations for shutdown operations include safety and hold-up considerations for the quality of the remaining fluid, and the ability to shut off some of the flow conditions in steady-state operation that are included in the sequence graph for startup operations. or a shutdown operation. In other words, since the equipment necessary for the startup operation can be used as is, there is no need to specially prepare equipment for the shutdown operation, and the structure is no different from the equipment required for the startup operation.

Therefore, the procedure for the shutdown operation can also be performed sequentially in accordance with the timing displayed on the display screen of the display device 44 using the sequence graph used during the startup operation. In many cases, the operating procedure during a shutdown operation does not follow the same flow from raw material supply to product as during a startup operation.

In the case of the distillation column system of the embodiment, the valve V1 is closed and the operation of the pump P1 is stopped to stop the raw material supply, and the valve V5 is closed to cut off the steam supplied to the reboiler RB. At the same time, switching valves SVI and SV2
Switch to state (1) to suppress distillation at the top and bottom of the column and increase the reflux amount.

The shutdown operation is then completed by waiting until the process fluid has cooled down sufficiently and closing the valve v3 that supplies the cooling water.

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 during the startup operation.

Sequence graph for emergency stop In general, safety is the top priority when it comes to operating procedures for emergency stop, so emergency stop equipment is often added to the plant based on safety, and the added line configuration An operation sequence graph is constructed accordingly. The additional equipment is, for example, equipment for removing fluid from the main plant components, equipment for supplying sealing gas to prevent explosions, etc. In the case of an emergency stop operation, the flow does not flow from "raw material supply to product" like the operating procedure and timing of a startup operation, but it can be expressed in the same way as a shutdown operation. Additionally, for the supply of additional fluids or the removal of process fluids, fluid transport lines must be added to the main process line, but lines are basically added and sequenced in the same way as expressed during startup operations. Creating graphs is easy. In addition, when forcibly removing process fluid to additional equipment, consideration should be given to the node at the connection point between the main process line and the removal equipment by using a special symbol or color to distinguish it from other nodes. is preferred.

The above-mentioned plant operation display device can completely automatically perform startup operations and shutdown operations by causing the electronic control device 40 to perform drive control of all pumps and valves, and the plant operation display device of the present invention can also be used as an automatic operating device.

Use as a simulation support device The plant operation display device of the present invention, which is applied to the distillation column system in the above-described embodiment, can be used to display operating procedures and timings for startup operations, shutdown operations, or emergency stop operations of the actual device. It is not only useful as a device for teaching personnel, but also as a design support tool when designing a plant while taking plant operation procedures and operation timing into consideration, or as a simulation support device for operators to familiarize themselves with the operation of actual equipment. It can also be usefully used as

When used as a simulation device, instead of the sensor means 54 of the plant operation display device shown in FIG. , a simulated signal generator that generates a simulated signal representing a state quantity such as composition may be connected to the electronic control device 40 via the I10 interface 50. Then, when a pump or valve is operated, a change in the state quantity of the process fluid due to the operation is predicted, and this is sequentially supplied to the electronic control device 40.

When using a plant operation display device as this simulation device, just as in the case applied to the actual device described above, a sequence graph is displayed on the screen on the display device 44, and operations are performed according to the highlighted activation instructions. , it is possible to easily evaluate the operability of the designed plant, and it can also be easily used to learn plant operation.

! Lord Ω! The sequence graph displayed on the screen of the plant operation display device of the present invention can also be applied to a composite unit consisting of a plurality of units. In particular, it can be applied more easily if the basic units are increasingly modularized. In other words, since the structure of the plant and the operating procedures correspond, if the structural changes necessary to combine two units are identified, the corresponding changes in the operating procedures will be revealed. can do. Let's consider this example as a second example.
This will be explained using a distillation column system with a heat pump, which is an example of the above. Note that, similarly to the first embodiment, in FIG. 11 as well, the symbols attached to the lines (fluid passages) are the same as the symbols used to identify the fluids.

Heat Pump Line Configuration The distillation column system of the second embodiment is a composite system in which the distillation column system of the first embodiment is combined with a heat pump HP that uses water as a working fluid (heat medium). 11th
The figure shows the line configuration of the heat pump unit applied to this distillation column system.

The heat pump HP is a thin film falling heat exchanger that includes two heat exchangers (side cooler and side heater) SC and SH. The side cooler SC takes the heat of condensation from the process fluid and gives it to water, which is the working fluid, to vaporize it.The side heater SH gives the heat of condensation of the working fluid to the process fluid, and gives it to water, which is the working fluid. It evaporates some parts. At the bottoms of the side cooler SC and side heater SH, hold ups H55 and H54 are provided to store the working fluid that has flowed down.

In addition to these heat exchangers, the heat pump HP is equipped with a compressor C1°C2 and a pressure reducer V51 for raising the temperature of the vaporized working fluid.

In order to increase the wetted area of their heat transfer surfaces, the side heater SH and the side cooler SC each have a process fluid circulation line S44. (S52゜553) are installed, and these lines are equipped with a circulation pump and a valve (P41
．． V41) and (P2O, VS2) are arranged.

Further, a working fluid (water) injection line is required as an operation preparation equipment for the heat pump HP, and for example, a working fluid injection pipe S51 is attached to the side cooler SC. Note that the working fluid is heated and evaporated by the process fluid in the side cooler SC, passes through the compressors C1 and C2, is condensed in the side heater SH, and is collected in the hold up H54 of the side heater SH. In order to smoothly start up the compressors C1 and C2, a pipe S60 is required to reduce the load at startup, and this pipe S60 is provided with a valve V54 that closes this during normal operation. .

Furthermore, train lines 365 and 366° S67 are provided for the purpose of removing working fluid condensed around the compressors C1 and C2. Furthermore, exhaust lines S61 to S63 for air entering the heat pump HP and a spray device (S64, VS2) for a working fluid to prevent superheating are provided.

Further details of the line configuration of the distillation column and heat pump The heat pump HP described above is placed at an intermediate stage between the condenser CD and the distillation column in the first embodiment, and is connected to two heat exchangers SC, S.
Since the H is in contact with the process fluid on each side of the distillation column across a heat transfer surface, the distillation column and the heat pump HP require structural changes to couple them together. Table 4 lists the connection parts between the distillation column and the heat pump HP.

(Leaving space below) Table 4 From the height positional relationship at both ends of each coupling line shown in Table 4 above, as necessary transport equipment, pump P42 and valve V43 are installed in line S47 on the output side of side cooler SC, and pump P42 and valve V43 are installed in line S47 on the output side of side cooler SC. A pump P40 and a valve V40 may be respectively arranged in the line S41 on the process fluid input side, and related utility pipelines may be added.

Line configuration for startup operation The line configuration required for startup operation of a distillation column system equipped with a heat pump is as follows. First, the circulation method described in the first embodiment is adopted, and piping is required to return the distillate at the top and bottom of the column to the raw material supply tank H1.

In addition to the arrangement of hold ups in the distillation column system of the first embodiment, there is also a hold up 3 between the top of the column and node 7.
3-Add H. This hold up 33-H receives and stops the process fluid flowing down from the top side of the distillation column.
This is installed to send this to the heat pump HP side.

As a result of the above study, Fig. 12 shows the heat pump HP
Figure 13 shows a structural representation of a distillation column system modified to couple the heat pump HP. In addition, in these figures, the same reference numerals are attached to the components corresponding to the distillation column system of the first embodiment.

Creation of a sequence graph (representation of fluid coupling and flow management conditions in the distillation column) Using the same method as explained in the first example, the fluid coupling and flow management conditions similar to those in Table 1 are created during startup operations on the distillation column side. The results are summarized in Table 5 below.

(Leaving space below) When all hold ups satisfy the set values during startup operation, valve Vl is closed to stop the raw material supply, and at the same time valves V4 and V6 are closed to use the total reflux method, steady operation transition condition #l and Wait for #2 to occur. Then, when conditions # and #2, which are conditions for transition to steady operation, are satisfied, the operations in Table 6 are executed.

In this Table 5, the changes from Table 1 are that the fluid $7', 3
7", S7°", S3', S9. S9
' has only been added or changed.

(Transition to steady operation) Switching from the startup operation on the distillation column side to steady operation is performed as follows.

That is, line S13 is opened, line S20 is closed, line S15 is opened, and line S21 is closed.

Here, steady operation transition conditions #l and #2 are, for example,
The bottom temperature of each tower exceeds the set value (TI?>T17s)
, the tower top temperature exceeds the set value (718>T18S
) may be determined.

(Expression of heat pump fluid coupling and flow management conditions) First, considering the pre-operation preparation work for the heat pump HP, these include the following.

Preparatory work 1: Injection of working fluid This work is to open the valve 50 of the line S51 and inject the working fluid into the hold up H55. When the required amount of working fluid has accumulated, the valve 50 is closed (15th A
(See sequence graph in figure).

Preparatory Work 2: Heat Exchanger Circulation Flow In this work, pump P50 is operated and valve V52 is opened to circulate the working fluid in the hold assembly H-55 of side cooler SC. In addition, the pump P41 is operated and the valve V41 is opened to circulate the working fluid in the hold assembly H54 of the side heater SH. Through these circulations of the working fluid, 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: Compressor circulation line configuration This work must be prepared before starting the compressor. Open valve V54 and connect the discharge side of compressor C2 to the suction side of compressor C1 to reduce the load when starting the compressor (first
(See sequence graph in Figure 5c).

Preparatory work 4: Configuring the Nidrain line This work also needs to be prepared before starting the compressor. Open the discharge side valve V56 of the first stage compressor CI and the discharge side valve V55 of the second stage compressor C2 to hold up the working fluid (water) accumulated in each compressor H-5
5 (see sequence graph in Figure 15D).

Preparatory work 5: Air venting This work is also a work that should be prepared before starting the compressor.
The valves 57 and 58 are opened, and the air inside the heat pump HP is discharged by the ejector EJ (see the sequence graph in FIG. 15E).

Preparatory work 6 - Overheating prevention line configuration This work is performed when the outlet temperature of the compressor C2 exceeds the specified temperature. Open the valve 53 from the above-mentioned circulation line of the side cooler SC and connect the hold up. H5
The working fluid (L) accumulated in No. 5 is sprayed into the line between the compressors CI and C2 to prevent overheating of the working fluid (see the sequence graph in Fig. 15F).

These preparatory work sequence graphs are shown in the 15th
Along with the sequence graph shown in the figure, the display device 4
It can also be displayed on the screen of 4, and if necessary,
These preparatory tasks can also be incorporated into the sequence graph as activation judgment conditions. Normally, most of these preparatory work should be completed before the first activation related to the heat pump HP appears in the sequence graph shown in FIG. 15.

Next, as in Table 1, Table 7 summarizes the fluid coupling and flow management conditions in the heat pump and auxiliary lines during startup operation.

(Conditions for transitioning the heat pump to steady operation) The conditions for transitioning the heat pump HP from startup operation to steady operation are as follows: Temperature T54 of the working fluid of the hold door knob H54 and H2S. T55 is each set value T54
', T55s or higher conditions (T54>T54', T5
5>T55'), the transition work is completed by gradually closing the valve V54 of the circulation line S60.

When the fluid coupling and flow management conditions summarized in Tables 4 to 7 are input to the electronic controller 40, the electronic controller 40 creates each sequence graph for 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 and heat pump HP, respectively.

The line configuration of the composite system is shown in FIG. 16 by overlapping the two heat exchanger joints in FIGS. 12 and 13.

On the other hand, the sequence graph of this composite system can be expressed by superimposing their connected parts in the same way as superimposing line configurations, and this is shown in FIG. This sequence graph includes Figures 15A to 1.
The sequence graph for the heat pump HP preparation work shown in the 5F diagram is also displayed on the same graph (screen).
The procedure and timing of startup operations for the entire system are expressed.

In this way, in the sequence graph of the plant operation display device of the present invention, the line configuration of the plant corresponds to the operation procedure and its execution timing, so it is extremely easy to change the line configuration and combine units. It can be carried out.

The startup operation of this complex system can be performed by sequentially performing activation from the entrance 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, this circulation line is cut off, and the intended function of the heat pump unit, that is, the compression function, is achieved. The sequence graph shown in Figure 17 clearly expresses the relationship between the operation timings of the heat pump side and the distillation column side, and also shows the sequence graph of the heat pump HP.
The operating procedures and timing up to the transition to normal operation are expressed. In addition, Fig. 14, Fig. 15, Fig. 15
Although the sequence graphs in Figures A to 15F and Figure 17 omit the display of specific judgment conditions for activation execution, in reality, []
It is sufficient to list all the necessary judgment conditions within.

The sequence graph of the plant operation display device of the present invention is
The direction of flow corresponds to the time axis.

The speed at which the process fluid flows between nodes and the time required for the hold-up amount to reach a set value can be predicted from simple calculation formulas or empirical values. Arranging the procedures and timing of startup operations in chronological order using a sequence graph is convenient for considering reduction in operation time during startup operations. for example,
By extracting the operation times of valves and pumps shown in the sequence graph and rearranging them in chronological order, it is possible to more clearly express which part of the startup operation requires operation time.

Figure 18 shows the operation time of each valve from the start when the demonstration pilot plant performs the startup operation based on the sequence graph shown in Figure 17, that is, the time when each activation starts and the steady state is entered. The times are arranged in chronological order.

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

The distillation column is a packed column (column section) with a diameter of 200+ nm and a height of 5000 mm, and the packing is a 1 inch mini cascade ring, and the packing 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 equivalent to the plate column of the target packed column is 11, including the reboiler RB. .

The raw material is supplied to the seventh stage when the top of the column is the first stage, and the side cut stage that sends the process fluid to the side heater SH of the heat pump HP corresponds to the eighth stage. The reboiler RB of the distillation column has a heat transfer area of 2.0 M, and uses steam of 2.0 kgfG/am2 as the heating tube side fluid. This reboiler RB exchanges heat at a rate of about 40 KW during startup and at a rate of about 16 KW during steady operation.

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

The heat pump HP is an indirect compression type heat pump and uses water as the 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 compressors CI and C2 are equipped with inverters to adjust the load.

Side heater SH, which is the part that transfers heat between the distillation column and the
The two heat exchangers called side coolers SC are of the 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 of the beet pump side of the pilot plant.

(Left below) In this pilot plant, the distillation column entered the steady operation switch waiting state from the time when the heat pump HP was switched to steady operation, which was 246 minutes after the startup start time. Further, the time when the entire system transitioned to a steady operating state was 376 minutes after the start-up started.

In this way, by operating the plant according to the sequence graph displayed on the screen by the plant operation display device of the present invention, the plant could be stably and reliably started up to the desired state.

By the way, in the above-mentioned first and second embodiments, the startup operation procedure is based on "flow management" and "hold-up management", and "operation mode change conditions" and "regular operation change conditions" are changed as necessary. The operation procedure is configured by taking into account the "transition conditions". - In boat fishing, the operation timing does not depend entirely on the hold-up condition, but rather takes into consideration or replaces variables such as the temperature, pressure, and composition of the process fluid at an appropriate location. It is often better to make adjustments. Additionally, operating conditions can be added to avoid dangerous operating conditions. In either case, plant operation can be made more flexible by adding these conditions to the activation judgment conditions.

In the second embodiment described above, it was demonstrated that reliable plant operation could be performed using the pilot plant, but it took 376 minutes to complete the startup operation, so there is room for improvement. Therefore, we improved the operating procedure. Table 10 shows the time taken to obtain the required hold-up amount from the valve operation time shown in FIG. 18.

Table 10 Regarding shortening of the hold-up charging time to the bottom tank H5 at the bottom of the column, if the distillate at the bottom of the column is charged in advance to the bottom tank H5 before starting up, the startup 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 heat pump HP is preheated when filling the side cooler SC with the working fluid as a preparatory work for the heat pump HP, the preheating time of the heat pump can be shortened. In this case, it is necessary to add a steam supply line to the side cooler SC.

To shorten the hold-up preparation time to the reflux tank H8 at the top of the column, add the hold-up to the reflux tank H8 at the top of the tower.
If the top distillate is charged in advance, the start-up time can be shortened 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 by modifying the line configuration and improving the operating procedure, as shown in Figure 19, the startup time from starting the startup operation to reaching steady operation will be 168 yen. I was able to shorten it to minutes.

Further, from FIG. 19, the operation timing of each valve can be clearly seen. If valve operation is to be done by stationing an operator on site rather than by remote control, which operator should be assigned the valve operation by comparing the timing chart in Figure 19 with the line configuration? Is this OK? - If all valve operations are to be left to human operators, it is necessary to consider the work efficiency of valve operations on site and decide on the necessary operator placement plan, such as where is the optimal location for the valves, etc. , valve arrangement planning, etc. can be easily performed. These can also be easily performed because the sequence graph of the plant operation display device of the present invention makes clear the correspondence between plant design, plant operations, and their timing.

(Sequence graph during shutdown operation) Even 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 in FIG. 17.

When performing a shutdown operation, first, the supply of raw materials and the supply of steam from the reboiler are stopped.

When the steam supply is stopped, no steam is generated from the reboiler RB, but since the process fluid can also be circulated when the heat pump HP is in operation, the heat pump HP is finally stopped.

The procedure and timing of this shirt tank operation (operation sea fence) can be set in the same manner as in the first embodiment, and can be set on the display screen of the display device 44 using the sequence graph of the startup operation. This can be expressed by sequentially lowering the brightness of the displayed 7 activations.

(Sequence graph during emergency stop operation) As explained in the first embodiment, in the case of the second embodiment as well, safety is the basis and equipment for emergency stop, such as seal gas, is installed in the plant as necessary. Add supply equipment, installation of process fluid emergency removal lines, etc. Then, the operation sea fence may be set in consideration of the added equipment in the same manner as in the first embodiment. In this case as well, it is possible to display the same expression on the display screen of the display device 44 as at the time of the shutdown operation. When the above-mentioned emergency stop equipment is added, the operation of the equipment can be done by adding the occurrence of the emergency stop condition and the order of operation of the equipment to the activation judgment conditions, and then the above-mentioned shutdown The operation is similar.

It goes without saying that 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. Note that a few examples of how to represent sequence graphs of other plant components can be given as follows.

FIG. 20 shows an evaporator, the process fluid in the can is heated and evaporated by a heat exchanger HEX 1 using steam as a working fluid, and the evaporated process fluid is transferred from the can to a line S.
At 80, the liquid accumulated in the can flows out to line S81. FIG. 21 shows a sequence graph of this evaporator portion.

Figure 22 shows the configuration of a self-heat exchange reactor, in which a reactive mixed process fluid reacts inside reactor R to generate reaction heat, and two heat exchangers HEX2 and HE
It is equipped with X3. The heat exchanger HEX2 preheats the process fluid to be reacted in the reactor R using steam as a heat medium,
In the heat exchanger HEX3, the process fluid that has become high in temperature due to the reaction heat generated in the reactor R heats the process fluid itself that flows into the reactor R. FIG. 23 shows a sequence graph of this self-heat exchange type reactor.

In addition, the following is an example of how to express flow coupling and flow management conditions when a phase change occurs at a node due to crystallization, flash phenomenon, pressurized liquefaction, or sedimentation separation.

It is expressed that the process fluid S87 is pressurized at the node Nil and condensed to become a liquid phase process fluid S87.

Table 11 expresses that the process fluid S80, which is in a liquid phase, is cooled at the node N2, partially crystallized, and becomes a process fluid S81 containing a solid phase S and a liquid phase.

Flash table 12 expresses that the process fluid S82 in the liquid phase is depressurized at the node N6 and becomes a negative vapor to become the process fluid S84 in the gas phase V, and the rest becomes the process fluid 83 in the liquid phase. ing.

Pressurized liquefaction Table 13 shows that the process fluid S86 in gas phase V is shown in Table 14.
represents that fluid S88 enters node N15 in a slurry state, is separated into a liquid phase fluid and a slurry phase (L0S), and exits N15 as fluid S89 and fluid 590, respectively. .

Even if the configuration of the chemical plant supplying process fluids A and B is the same, different operations are possible. For example, a tank 100 as shown in FIG.
When supplying process fluids A and B,
Depending on the process you are running, you may need to take different approaches as described below.

In the first supply method, process fluid A is first supplied to tank 100, and then, when the hold-up amount reaches a set value [>100-HS], process fluid B is supplied to tank 100. FIG. 25 shows a sequence graph in this case, in which the activation judgment condition regarding the valve V 102 is set to the hold up amount condition [>
100-H"l is added.

In the second supply method, process fluids A and B are supplied to tank 100 simultaneously. FIG. 26 shows the sequence graph for this case, provided that the preparatory work for both process fluids A and B has been completed.
This condition is added to the determination conditions for each activation regarding valves VIOI and v102. Therefore, once the preparatory work on both process fluids A and B is completed, valves VIOI and v10 are simultaneously
2 will be opened. The sequence graph shown in FIG. 26 can be rewritten as shown in FIG. 27 according to the conventional sequence graph representation method. Even in this sequence graph representation, valves ■101 and ■10
This shows that the valves 2 and 2 are opened synchronously.

In the above embodiment, the sequence graph is displayed on the display screen of the display device 44, but it may be printed out on the printer device 46. Further, as shown in FIG. 2, the operation display device 49 is distributed for each plant and connected to a distributed control system (DSC), and the operation display device 49 on each plant side is transmitted from the central electronic control device 40 when necessary. Alternatively, the above-described sequence graph may be sent to form part of a distributed control system.

(Effects of the Invention) As detailed above, according to the plant operation display device of the present invention, the output device detects 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 the flow direction when a flow occurs in each fluid passage, and each transportation means is stored in the storage means. and/or the operating conditions of the valve means are stored in advance, the sensor means determines whether or not the operating conditions of each transport means and/or the valve means are satisfied, and the output device control means is used to control the system input node side. determining whether or not the operating conditions are satisfied in order from the transportation means and/or valve means;
If the operating conditions are met, the output device will highlight that the transport means and/or valve means should be operated, and the output device will highlight that the transport means and/or valve means should be operated, and the flow between the nodes where flow has occurred due to the operation of these transport means and/or valve means. Since only the fluid passages are highlighted, it is possible to display on the output device a sequence graph that corresponds to the plant line configuration, that is, the plant design, and the plant operation procedures and their timing, making it easier to control the plant operation. This can be done extremely easily and reliably. If a simulation signal output means is provided in place of the sensor means and used as a simulation device, it will be extremely useful as a design support tool, and it will be possible to grasp the operation procedures and their timing from the design stage of the plant line configuration, and to arrange valves etc. It is also possible to easily improve the plant and design a complex plant that combines a large number of units.

[Brief explanation of drawings]

The drawings show an embodiment of the plant operation display device according to the present invention, and FIG. 1 is a block diagram showing the configuration of a distillation column system of the first embodiment to which the plant operation display device of the present invention is applied. Figure 2 is a block diagram showing the configuration of the plant operation display device applied to the distillation column system, and Figure 3 is a block diagram showing the configuration of the plant operation display device applied to the distillation column system.
A diagram showing a flow sheet of the line configuration in a steady state of the distillation column, Figure 4 is a flow sheet diagram showing the distinction of fluid transport means, and Figure 5 is a diagram showing the pumps necessary for the flow sheet in Figure 4. Figure 6 is a diagram showing the location of the hold-up, and Figure 7 is a flow sheet diagram of the line configuration required for steady-state transition operation using the total reflux method during startup operation. Figure 8 is a flow sheet diagram of the line configuration necessary for steady-state transition operation using the circulation method during startup operation, and Figure 9 is a diagram showing the node configuration of the distillation column system of the first embodiment. 10 shows a sequence graph displayed on the display screen of the display device 44 in FIG. 2, and FIG. 11 shows a distillation column system of a second embodiment to which the plant operation display device of the present invention is applied. FIG. 12 is a block diagram showing the configuration of the heat pumps to be combined. 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. Figure 14 is a sequence graph when only the distillation column side of the second embodiment is operated;
Figure 5 is a sequence graph when only the heat pump side is operated, Figure 15A is a sequence graph for preparing to inject working fluid into the heat pump, and Figure 15B is preparing to circulate heat exchanger working fluid in the heat pump. Figure 15C is a sequence graph for preparing the circulation line of a heat pump compressor. Figure 15D is a sequence graph for preparing a heat pump drain line. Figure 15E is a sequence graph for preparing a heat pump's drain line. Sequence graph for heat pump air vent preparation work,
Figure 15F is a sequence graph for the preparation work of the overheating prevention line of the heat pump compressor, and Figure 16 is the
A line diagram showing a node configuration in which a distillation column and a heat pump are combined, FIG. 17 is a sequence graph of the distillation column system of the second embodiment, and FIG. 18 is a diagram showing the sequence graph of the distillation column system according to the sequence graph shown in FIG. 17. FIG. 19 is a timing chart showing the operation times of valves, etc. when the startup time is shortened;
Fig. 20 is a diagram showing the configuration of the evaporator, Fig. 21 is a diagram showing a method of expressing the sequence graph of the evaporator part, and Fig. 2
Figure 2 is a diagram showing the configuration of the autothermal exchange reactor, Figure 23 is a diagram showing how to represent the sequence graph of the autothermal reactor section, and Figure 24 is a diagram showing the configuration of the autothermal exchange reactor. FIG. 25 is a block diagram showing a line configuration for supplying fluid A to the tank 100, and FIG. 25 is a diagram showing a method of expressing a sequence graph when supplying fluid B is started after a set amount of fluid A has been added to the tank. Figure 26 is a diagram showing how to represent the sequence graph when fluids A and B are supplied to the tank at the same time, and Figure 27 is a diagram showing how to represent the sequence graph in Figure 26 when fluids A and B are supplied to the tank at the same time. Diagram showing the equivalent expression method, 2nd
FIG. 8 is a block diagram for explaining the basic concept of the present invention. 40... Electronic control device, 42... Input device, 44.
... Display device, 46... Printer device, 49.
...Distributed control system, 52...Driving means, 54...
・Sensor means, CI, C2...Compressor, CD...Condenser, D...Tower section, RB...Reboiler, HP・
・・Heat pump, HO・・Raw material storage tank, HL・
・・Raw material supply tank, H5・Bottom tank, H8・
...reflux tank, H9...top product tank, HIO.
...Bottom product tank, P...pump, SC...side cooler, SH...side heater, ■...valve. Applicant Yuji Applicant Techno Systems Co., Ltd. Agent Patent Attorney Kanji Nagato Figure 2 Figure 4 Figure 7 "H9 Figure 8 Figure 20 r----" Figure 22 Figure 21 Figure 23 Figure 24 Figure 25 +00 Figure 26 Figure 27 Figure 28

Claims (16)

[Claims] (1) Each point of a plant component is represented by a node, including at least one system input node from which fluid is supplied to the plant from the outside, and from which fluid exits the plant to the outside; At least one system output node is included, adjacent nodes are connected to each other by fluid passages, and among these fluid passages, there are transportation means and/or valve means for creating a fluid flow in the middle of the fluid passage at required points. In the plant operation display device of the installed plant, based on the type of fluid flowing in each fluid passage and the phase state of the fluid, fluids in the same phase state are sequentially moved from the system input node to the system output node. Tracing these nodes,
an output device that arranges and displays in one direction along the flow direction when a flow occurs in each fluid passage; a storage means that stores in advance the operating conditions of each of the transportation means and/or the valve means; A sensor means for determining whether the operating condition of the means and/or the valve means is satisfied, and a sensor means for determining whether the operating condition is satisfied or not, starting from the transportation means and/or the valve means on the system input node side. and when the operating conditions are met, the output device highlights that the transportation means and/or the valve means should be operated, and the flow is caused by the operation of the transportation means and/or the valve means. and output device control means for highlighting only fluid passages between nodes. (2) The plant component includes a heat exchange component, one of the nodes is connected to a node of the heat exchange component via energy exchange, and the heat exchange component is parallel to the output device. The plant operation display device according to claim 1, wherein the plant operation display device displays the following information. (3) The plant according to claim 2, wherein the fluid flowing in the fluid passage connected to the node of the heat exchange component and the node that transfers energy changes the phase state before and after the node. Operation indicator. (4) The plant operation display device according to claim 1, wherein the plant component includes a holdup device and is displayed as one of the nodes. (5) The plant operation display device according to claim 1, wherein the output device is an image display device. (6) The plant operation display device according to claim 1, wherein the output device is a printer device. (7) The plant operation display device according to any one of claims 1 to 6, wherein the plant component comprises components of a plurality of plant units. (8) The plant operation display device according to claim 1 is provided with a driving means for driving the transportation means and/or the valve means, and when the operation condition is satisfied, the driving means causes the transportation means and/or the valve to be activated. An automatic plant operation device characterized by driving and operating means. (9) Each point of a plant component is represented by a node, including at least one system input node from which fluid is supplied to the plant from the outside, and from which fluid exits the plant to the outside; At least one system output node is included, adjacent nodes are connected to each other by fluid passages, and transport means and/or valve means for creating a fluid flow are arranged in the fluid passages at required points among these fluid passages. of the plant to be installed,
A plant operation display device that evaluates plant operation by operating the plant in a simulated manner includes an input device for inputting data through an external input operation; Based on the type of fluid flowing from the node to the adjacent node and the phase state of the fluid, 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 for unidirectionally arranging and displaying information along the flow direction when a flow occurs; and a storage device for pre-storing operation conditions for each of the transportation means and/or the valve means inputted by the input device; a simulated signal output means for outputting a simulated signal that simulates the operation conditions of each of the transportation means and/or the valve means;
Alternatively, in order from the valve means, it is determined whether or not the operating condition is satisfied based on the presence or absence of a simulated signal from the simulated signal outputting means, and when the operating condition is established, the output device is configured to output the transportation means and/or Output device control means for highlighting that the valve means should be operated and for highlighting only the fluid passages between nodes where flow is deemed to have occurred due to the operation of these transportation means and/or the valve means. A plant operation display device characterized by: (10) the plant component includes a heat exchange component;
10. The plant operation according to claim 9, wherein one of the nodes is connected to a node of the heat exchange component via energy exchange, and the heat exchange component is displayed in parallel on the output device. Display device. (11) The fluid flowing in the fluid passage connected to the node of the heat exchange component and the node that transfers energy is
The plant operation display device according to claim 10, characterized in that the phase state is changed before and after the node. (12) The specified means of transportation and/or
or a command means for outputting a pseudo command signal for activating or stopping the valve means, and the output device control means controls the specific transportation means and/or the valve means in response to the pseudo command signal from the command means. When activated or deactivated, only the fluid path between the nodes where a new flow has occurred is highlighted, and the operating conditions of each of the transportation means and/or the valve means change due to this change in flow; 10. The plant operation display device according to claim 9, wherein the plant operation display device emphatically displays that the transport means and/or the valve means should be operated in accordance with the changed operating conditions. (13) The plant operation display device according to claim 9, wherein the plant component includes a holdup device and is displayed as one of the nodes. (14) The plant operation display device according to claim 9, wherein the output device is an image display device. (15) The plant operation display device according to claim 9, wherein the output device is a printer device. (16) The plant operation display device according to any one of claims 9 to 15, wherein the plant component comprises components of a plurality of plant units.