CN107930557A - A kind of chemical process production capacity optimal control method and device - Google Patents
A kind of chemical process production capacity optimal control method and device Download PDFInfo
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- CN107930557A CN107930557A CN201711263640.1A CN201711263640A CN107930557A CN 107930557 A CN107930557 A CN 107930557A CN 201711263640 A CN201711263640 A CN 201711263640A CN 107930557 A CN107930557 A CN 107930557A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0033—Optimalisation processes, i.e. processes with adaptive control systems
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/008—Feed or outlet control devices
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B11/00—Automatic controllers
- G05B11/01—Automatic controllers electric
- G05B11/36—Automatic controllers electric with provision for obtaining particular characteristics, e.g. proportional, integral, differential
- G05B11/40—Automatic controllers electric with provision for obtaining particular characteristics, e.g. proportional, integral, differential for obtaining an integral characteristic
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D27/00—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00
- G05D27/02—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00 characterised by the use of electric means
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]
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- Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Automation & Control Theory (AREA)
- Physics & Mathematics (AREA)
- General Physics & Mathematics (AREA)
- Feedback Control In General (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The present invention provides a kind of chemical process production capacity optimal control method and device, including：High value selector, comparator, feedback controller and low value selector.The input of high value selector is to determine each operating quantity of chemical process production capacity size, the output connection comparator of high value selector, another input of comparator is maximal valve position setting value, compare the input of gained difference connection feedback controller, one input of the output connection low value selector of feedback controller, another input connected load setting value, the charging setting value of the output connection master control raw material of low value selector.This method determines each operating quantity of chemical process production capacity size by detecting, select big person therein and maximal valve position setting value to be compared, and master control feedstock amount is adjusted according to the positive and negative of difference is compared, so that production capacity is optimal.
Description
Technical field
The present invention relates to chemical field, is specifically related to a kind of production capacity optimal control method and dress suitable for chemical process
Put.
Background technology
Chemical process is to be related to the chemical process or physical process of chemical industry and the production of other process industrials.These industry
From base stocks such as oil, coal, natural gas and water, air, by chemically or physically method, change material composition, property and
State, so as to generate the higher product of various value.Typical chemical products basic process includes：Fluid conveying, heat exchange (heating
And cooling), distillation etc., all these basic processes are required for meeting the equipment of process production requirement to complete.In practice, one
The equipment investment of chemical process is usually very big, how to improve equipment automation control degree, and how to automatically adjust life
Load is produced so as to obtain maximized output on existing, is enterprise's issues that need special attention.
At present, Distributed Control System (DCS：Distributed Control System) it is universal in some large enterprises
Using.These DCS control systems instead of original conventional control instrument, it flexibly controls hardware and algorithm configuration also to make life
The degree of automation of production process greatly improves.But these DCS systems usually only focus on some independences in controlling plan design
The dynamic control problem of process, not from the system-level global optimization problem for considering whole process.Such as chemical process
Automatic drive and Load Regulation problem, these work will be manually operated by engineer and can completed substantially.Particularly with
It is related to safety of chemical production problem, engineering staff will be careful in concrete operations, and slightly slipping up all will be to whole chemical industry
Production brings huge security risk.
CN105045249A disclose it is a kind of realize the autocontrol method that adjusts produce load in Chemical Manufacture safely and
Device, overcomes conventional art and adjusts by artificial means firstly the need of the inventory for increasing or decreasing material, and inventory changes
Still need to immediately change when input full energies are given more sustained attention at the time of the actual inventory of the material reaches consistent with new setting value afterwards
Become the technological deficiency of another material amount, material amount change order is sent out when will change produce load by coordinated signals
The possibility of raw mistake is reduced to zero, reduces to greatest extent since produce load changes to huge peace caused by Chemical Manufacture
Full hidden danger.CN105468800A discloses a kind of optimization method of ethane cracking furnace produce load adjustment, solves ethane cracking furnace
The adjustment of produce load, optimal heat distribution is provided for ethane cracking furnace radiant section, reduces the energy consumption of ethane cracking furnace, and foundation
Raw material type and the adjustment of feature Optimization of Ethylene pyrolysis furnace produce load.CN102183892A discloses a kind of methanol three-tower rectification system
The varying duty energy consumption optimization control method of system, by building input as charging parameter, the operating parameter control after exporting as optimization
The varying duty optimal control for energy saving device of value, and the optimal ginseng of energy consumption is calculated using genetic algorithm using varying duty optimal control for energy saving device
Number, so that control system, which is operated in, ensures the minimum operating mode of energy consumption under the premise of quality.
Above-mentioned technology solves the production capacity Optimal Control Problem of part workshop section or a certain process of producing product, but due to chemical industry
Process is an integrated system, is influenced each other between each process unit equipment, is mutually restricted, and the optimization of production capacity is whole with greater need for considering
The all devices of a process, therefore realize that chemical process production capacity optimal control requires further improvement.
The content of the invention
In view of the deficiencies of the prior art, the present invention intends to provide a kind of improved chemical process production capacity optimization
Control method and device." one-touch " driving to a certain specific chemical process, subsequent automatic lifting load can be achieved in the present invention
Size is to load setting value.Meanwhile the designed capacity of each chemical process unit of definite consideration of load, can make be entirely
System is operated under optimal production capacity.
A kind of chemical process production capacity optimal control method provided by the invention, it is characterised in that comprise the following steps：
1) initialize, close all conveying devices, all feedstock control loops of chemical process are placed in manually
Under control model, the control loop of the chemical/physical reaction unit of chemical process core is placed under MANUAL CONTROL mode, by even
The control loop for tapping into the ancillary equipment for expecting core chemical/physical reaction unit is placed under MANUAL CONTROL mode, and production capacity is excellent
Change control module to be placed under MANUAL CONTROL mode；
2) the charging control loop of each raw material is switched to automatic mode, starts each feed conveying device, and set
The Ratio control coefficient of good master control raw material and auxiliary control raw material, while charging ratio controller is switched to automatic mode；
3) control loop that the ancillary equipment for being fed to core chemical/physical reaction unit is related to is switched to automatically
Control model；
4) start catalyst conveying device when core chemical/physical reaction unit detects that raw material has inputted, will urge
Agent control loop is switched to automatic mode, and sets Ratio control coefficient, while catalyst ratio controller is cut
Change to automatic mode；
5) control loop that the chemical/physical reaction unit of chemical process core is related to is placed in automatic control mode
Under, and start and the relevant conveying device of each variable；
6) production capacity optimal control module is switched to automatic control mode after the dynamic process of each variable is stablized.In this hair
In bright preferred embodiment, the control of the chemical/physical reaction unit of chemical process core generally comprises temperature, pressure, liquid
The Variable Controls such as position, stirring, conductance, dissolved oxygen, pH；The ancillary equipment that connection is fed to core chemical/physical reaction unit is general
Including pipeline, tank or pre-processing device etc., it is related to the Variable Controls such as liquid level, flow, temperature and pressure.
The operation of production capacity optimal control module is in step 6)：Detection determines each operating quantity of chemical process production capacity size,
Select big person therein and maximal valve position setting value to be compared, if big person therein is less than maximal valve position, step up
Master control feedstock amount, if greater than maximal valve position, then gradually reduces master control feedstock amount.
In a preferred embodiment of the invention, each operating quantity for determining chemical process production capacity size can be feedstock
Variable, catalyst charge variable, is input to the charging variable of core chemical/physical reaction unit, can also be and maintain core
/ physical reactions device keeps determining the controlled quentity controlled variable of operating mode.
In a preferred embodiment of the invention, each operating quantity type for determining chemical process production capacity size can be control
The output valve of device or the valve place value of regulating valve, can also be based between after controller output valve or valve place value computing
The amount of connecing.
In a preferred embodiment of the invention, maximal valve position setting value is less than 100%, and valve has certain positive and negative two
The dynamic adjustable extent in direction.
A kind of chemical process production capacity optimal control device provided by the invention, it is characterised in that including high value selector, than
Compared with device, feedback controller and low value selector.The input of high value selector is to determine each operating quantity of chemical process production capacity size,
The output connection comparator of high value selector, another input of comparator is maximal valve position setting value, after their comparison operations
Gained difference connects the input of feedback controller, an input of the output connection low value selector of feedback controller, low value choosing
Select another input connected load setting value of device, the charging setting value of the output connection master control raw material of low value selector.
In a preferred embodiment of the invention, feedback controller is the controller that integral action is dominated.
Compared with prior art, chemical process production capacity optimal control method provided by the present invention and device can play equipment
Maximum production capacity, startup procedure is stablized, safe to use, is easily enlarged production capacity.
Brief description of the drawings
Fig. 1 is the production capacity Optimal Control System schematic diagram of one embodiment of the present of invention.
Fig. 2 is the production capacity optimal control function structure chart of the present invention.
Embodiment
In order to which the technical characteristic to the present invention, purpose and methods for using them are more clearly understood, in conjunction with attached drawing to this
The embodiment of invention is described further.It should be noted that the embodiment of detailed process described herein is only
For instruction and explanation of this explanation, it is not intended to limit the invention.
As shown in Figure 1, an exothermal reaction process, which mainly includes raw material, mixes and chemically reacts two stages.Raw material A and
Raw material B enters blending tank V101, raw material A in the case where conveying device raw material pumps the conveying that P101 and raw material pump P102 through piping respectively
It is master control raw material, raw material B is auxiliary control raw material, and raw material A and raw material B will feed according to a Ratio control COEFFICIENT K 1, connect on pipeline
It is connected to flowmeter FT, the size of raw material A and raw material B inlet amounies is controlled by regulating valve FV101 and FV102 respectively, flow controller
FC is used to control flow to make it ensure dynamic stability；Blending tank V101 is connected with liquid level sensor LT, and fluid level controller LC is used for
The liquid level of control blending tank V101 makes it ensure dynamic stability, is input to the size of reaction kettle V102 inlet amounies by regulating valve
FV103 is controlled；Reaction kettle V102 is provided with chuck, temperature sensor TT and agitating device M, and temperature controller TC is used to control anti-
Kettle V102 internal temperatures are answered it is ensured dynamic stability, the cooling water inflow size for being input to chuck is controlled by regulating valve FV105, cold
But flowmeter FT is connected with waterpipe, flow controller FC is used to control flow to make it ensure dynamic stability；Catalyst is being urged
Through piping enter reaction kettle V102 under the conveying of agent pump P103, be input to the catalyst charge amount size of reaction kettle V102 by
Regulating valve FV104 is controlled, and catalyst charge amount and master control raw material A feed according to a Ratio control COEFFICIENT K 2, connected on pipeline
There are flowmeter FT, flow controller FC to be used to control catalyst charge flow to make it ensure dynamic stability；Reaction kettle V102 is exported
Load size to other processes is controlled by regulating valve FV106, and the fluid level controller LC of regulating valve FV106 control connections is used
In the liquid level of control reaction kettle V102.
In this embodiment, determine that the operating quantity of chemical process production capacity size is the inlet amount of master control raw material A, and be used for
Reaction kettle V102 is maintained to keep the cooling water input quantity of temperature.
In this embodiment, determine the feed size of the master control raw material A of chemical process production capacity size by valve FV101's
The output quantity of valve position (aperture) or connected flow controller FC determine that another determines the cold of chemical process production capacity size
But water input quantity size is determined by the valve position (aperture) of valve FV105 or the output quantity of connected flow controller FC.
In a preferred embodiment of the invention, feedback controller is I-only controllers.
In a preferred embodiment of the invention, an input of the output connection low value selector of I-only controllers,
The setting value in the flow controller FC circuits of the output connection master control raw material A of low value selector.
In a preferred embodiment of the invention, there is provided a kind of chemical process production capacity optimal control method include following step
Suddenly：
1) initialize, all conveying device P101, P102, P103 are closed, by all feedstock variable controls of chemical process
Circuit processed is placed under MANUAL CONTROL mode, including in Fig. 1 regulating valve FV101 and FV102 FC control loops, by chemical process core
The chemical/physical reaction unit of the heart, that is, the temperature controller TC of reaction kettle V102 and cooling water inflow regulating valve FV105
Flow controller FC is placed under MANUAL CONTROL mode, regulating valve FV103's connection being fed on nuclear reaction kettle V102 pipelines
Flow controller FC is placed under MANUAL CONTROL mode, and production capacity optimal control module is placed under MANUAL CONTROL mode；
2) the charging control loop of each raw material is switched to automatic mode, that is, will with regulating valve FV101 and
The FC control loops of FV102 connections are switched to automatic mode, start each feed conveying device P101 and P102, and set master control
The Ratio control COEFFICIENT K 1 of raw material and auxiliary control raw material, while charging ratio controller is switched to automatic mode；
3) the fluid level controller LC by the regulating valve FV103 connections being fed on reaction kettle V102 pipelines is switched to automatic control
Molding formula；
4) when the liquid level sensor LT of reaction kettle V102 connections detects that raw material has inputted, catalyst transport dress is started
P103 is put, catalyst control loop is switched to automatic mode, that is, the FC being connected with regulating valve FV104 is controlled back
Road is switched to automatic mode, and sets Ratio control COEFFICIENT K 2, while catalyst ratio controller is switched to automatic mode；
5) the temperature controller TC of reaction kettle V102 is placed under automatic control mode, temperature control is a tandem herein
Controller, the FC controllers connected with regulating valve FV105 are subloop controllers, start cooling water conveying device；
6) it is after the flow involved in above-mentioned steps, liquid level and the dynamic process of temperature control loop are stablized, production capacity is excellent
Change control module and be switched to automatic control mode, that is, I-only controllers is started to work.
In a preferred embodiment of the invention, there is provided a kind of chemical process production capacity optimal control device structure chart such as
Shown in Fig. 2, that is, the production capacity optimal control function structure chart of the embodiment of the present invention.
In the above-described embodiments, whole chemical process can realize one-key start and load automatic adjustment.Drive initial rank
Section, master control raw material A give a less inlet amount.After whole process dynamic stability, production capacity optimal control module starts work
Make.The big person of FV101 and FV105 valve place values by high value selector select after exported, the output valve again with maximal valve position setting value
Compare, herein the optional 90%-95% of maximal valve position setting value.If less than maximal valve position setting value, then I-only controllers
Output increase, if greater than maximal valve position setting value, then the output of I-only controllers reduces.The output of I-only controllers and
Load setting value is the input of low value selector respectively, and when the output of I-only controllers is less than load setting value, master control is former
The charging setting value of material A follows the output of I-only controllers, production capacity lifting；When the output of I-only controllers is not less than load
During setting value, the charging setting value of master control raw material A selects load setting value, then chemical process works in the case where setting production capacity.I-
The integral parameter of only controllers should be according to the feature-set of specific chemical process, a generally smaller value, to ensure to feed
Increase is a slow process.Production capacity lifted during, if the valve place value of FV101 close to maximal valve position setting value simultaneously
And exported from high value selector, this explanation feedstock ability has reached capacity, and production capacity cannot continue to lift up at this time；If
The valve place value of FV105 is exported close to maximal valve position setting value and from high value selector, the processing energy of this explanation reaction kettle V102
Power has reached capacity, and production capacity cannot equally continue to lift up at this time.Production capacity optimal control module provided by the invention selection it is above-mentioned into
The big person of material and respond, works so that whole process is maintained under maximum production capacity.
The foregoing is merely exemplified embodiment of the present invention, is not limited to the scope of the present invention.Any ability
The technical staff in domain, the equivalent variations made and modification on the premise of the design of the present invention and principle is not departed from, increase or
The use step of some devices is reduced, the scope of protection of the invention should all be belonged to.
Claims (7)
1. a kind of chemical process production capacity optimal control method, it is characterised in that comprise the following steps：
1) initialize, close all conveying devices, all feedstock control loops of chemical process are placed in manual control
Under pattern, the control loop of the chemical/physical reaction unit of chemical process core is placed under MANUAL CONTROL mode, will connect into
Expect that the control loop of the ancillary equipment of core chemical/physical reaction unit is placed under MANUAL CONTROL mode, production capacity is optimized and is controlled
Molding block is placed under MANUAL CONTROL mode；
2) the charging control loop of each raw material is switched to automatic mode, starts each feed conveying device, and set master
The Ratio control coefficient of raw material and auxiliary control raw material is controlled, while charging ratio controller is switched to automatic mode；
3) control loop that the ancillary equipment for being fed to core chemical/physical reaction unit is related to is switched to and automatically controlled
Pattern；
4) catalyst conveying device is started when core chemical/physical reaction unit detects that raw material has inputted, by catalyst
Control loop is switched to automatic mode, and sets Ratio control coefficient, while catalyst ratio controller is switched to
Automatic mode；
5) control loop that the chemical/physical reaction unit of chemical process core is related to is placed under automatic control mode,
And start and the relevant conveying device of each variable；
6) production capacity optimal control module is switched to automatic control mode after the dynamic process of each variable is stablized.
A kind of 2. chemical process production capacity optimal control method as claimed in claim 1, it is characterised in that：Production capacity is excellent in step 6)
The operation for changing control module is each operating quantity that detection determines chemical process production capacity size, selects big person therein and maximal valve position
Setting value is compared, if big person therein is less than maximal valve position, master control feedstock amount is stepped up, if greater than most
Big valve position, then gradually reduce master control feedstock amount.
A kind of 3. chemical process production capacity optimal control method as claimed in claim 1, it is characterised in that：Determine chemical process production
Each operating quantity of energy size can be feedstock variable, and catalyst charge variable, is input to core chemical/physical reaction unit
Charging variable, can also be the controlled quentity controlled variable for maintaining core chemical/physical reaction unit to keep determining operating mode.
A kind of 4. chemical process production capacity optimal control method as claimed in claim 1, it is characterised in that：Determine chemical process production
Each operating quantity type of energy size can be the output valve of controller or the valve place value of regulating valve, can also be and be based on
Indirect amount after controller output valve or valve place value computing.
A kind of 5. chemical process production capacity optimal control method as claimed in claim 1, it is characterised in that：Maximal valve position setting value
Less than 100%, valve has the dynamic adjustable extent of certain positive and negative both direction.
A kind of 6. chemical process production capacity optimal control device, it is characterised in that including：High value selector, comparator, feedback control
Device and low value selector.The input of high value selector is to determine each operating quantity of chemical process production capacity size, high value selector
Output connection comparator, another input of comparator is maximal valve position setting value, gained difference connection after their comparison operations
The input of feedback controller, one of low value selector input of output connection of feedback controller, low value selector another
Input connected load setting value, the charging setting value of the output connection master control raw material of low value selector.
A kind of 7. chemical process production capacity optimal control device as claimed in claim 6, it is characterised in that：Feedback controller is long-pending
It is allocated as with leading controller.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711263640.1A CN107930557B (en) | 2017-12-05 | 2017-12-05 | Chemical process capacity optimization control method and device |
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| CN201711263640.1A CN107930557B (en) | 2017-12-05 | 2017-12-05 | Chemical process capacity optimization control method and device |
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| CN107930557A true CN107930557A (en) | 2018-04-20 |
| CN107930557B CN107930557B (en) | 2020-05-19 |
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Cited By (1)
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| CN108721934A (en) * | 2018-08-16 | 2018-11-02 | 青海黄河上游水电开发有限责任公司新能源分公司 | The overall process autocontrol method and system of rectifying column |
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| CN101279976A (en) * | 2008-04-29 | 2008-10-08 | 常熟市联邦化工有限公司 | Monitoring method for hot-spot temperature of gas-phase catalytic oxidation reaction in preparation of pyromellitic acid anhydride |
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| CN105045249A (en) * | 2015-09-10 | 2015-11-11 | 蓝星（北京）技术中心有限公司 | Automatic control method and device for realizing safe production load adjustment in chemical industry production |
| CN205959051U (en) * | 2016-08-19 | 2017-02-15 | 北京世纪隆博科技有限责任公司 | Multivariable intelligent coordination control system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108721934A (en) * | 2018-08-16 | 2018-11-02 | 青海黄河上游水电开发有限责任公司新能源分公司 | The overall process autocontrol method and system of rectifying column |
| CN108721934B (en) * | 2018-08-16 | 2024-04-12 | 青海黄河上游水电开发有限责任公司新能源分公司 | Full-process automatic control method and system for rectifying tower |
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| CN107930557B (en) | 2020-05-19 |
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