CN1169330A - Multiparameter on-line optimization control method for gas dephlegmation tower - Google Patents
Multiparameter on-line optimization control method for gas dephlegmation tower Download PDFInfo
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- CN1169330A CN1169330A CN 96115404 CN96115404A CN1169330A CN 1169330 A CN1169330 A CN 1169330A CN 96115404 CN96115404 CN 96115404 CN 96115404 A CN96115404 A CN 96115404A CN 1169330 A CN1169330 A CN 1169330A
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Abstract
The invention relates to a gas fractionating column multi-parameter on-line optimized-control method of a chemica installation in oil-extracting industry. An upper computor is proveded in the existing computer control system for production installation, and an improvement on cascade control and parameter contral is made to obtain a pressure, temp. multi-parameter on-line optimized-control algorithm for a gas fractionating column and according to that a computor programme can be assembled and operated to realize the optimized conputor programme can be assembled and operated to realize the optimized control to the backflow quantity and steam quantity of a gas fractionating column to reaonably distribute steam-eiquid phase load in the column, increase product quality and reduce energy.
Description
The present invention relates to the online excellent control method of microcomputer of gas fractionator of the chemical plant installations such as computer procedures control technology, particularly MTBE, gas fractionation, alkylation of gas fractionator in the petroleum refining industry.
The main production task of gas fractionator in the oil plant is that liquid hydrocarbon is slit into different product components by technological requirement in the undercutting of cat head tower.The quality of product quality depends on the distribution of the interior vapour of pressure, temperature and the tower of this tower, liquid phase load.Whether vapour, liquid phase load distribute on column plate all even stable, is the fractionating effect of decision tower and the principal element of product quality.And the vapour of tower, liquid phase load is provided by the quantity of steam and the overhead reflux amount of duplicator at the bottom of the tower respectively again.Old control scheme, no matter be the fractionating column of gas fractionation unit, or the fractionating column of MTBE, or the gas fractionator of the alkyl plant of introducing by U.S. field, to above-mentioned temperature, pressure and vapour, liquid phase load, all be to adopt the one-parameter control method, method owing to operating personnel differs like this, add artificial hysteresis and the adjustment of each parameter is attended to one thing and lose sight of another, not only water, electricity, vapour consume excessively, and quality can't guarantee.To the leakage of device cold exchange device and open long period etc. and all have a significant impact, directly influence the economic benefit of whole device.
The objective of the invention is the problems referred to above at current production existence, seeking the optimization thought of optimizing point down with multi-constraint condition in the optimal control theory is foundation, in conjunction with improvement to existing tandem control and one-parameter control, by optimization computing to relevant parameters such as the pressure of gas fractionator, top temperature, end temperature and sensitive plate temperature, realization is to fractionating column capacity of returns and the control of quantity of steam real-time closed-loop on-line optimization, finally reach vapour in the reasonable distribution tower, liquid phase load, improve the quality of products energy-saving and cost-reducing purpose of increasing economic efficiency.
For achieving the above object, the present invention is provided with one and finishes the host computer of optimizing computing and control on existing MTBE process units DCS system or other computer control system, and is slave computer with the computer that has control system now.Host computer CPU disposal ability requires IBM or the compatible more than 80386.At first, reach the bit optimization machine by the communication of upper and lower machine with relevant datas such as the measured value of top temperature, end temperature, sensitive plate temperature, pressure tower and the capacity of returns and the vapor volume of fractionating column, set-points.The optimization machine is through the multi-parameters optimization computing, and the best quantity of steam that obtains and the controlling value of capacity of returns are issued slave computer by the communication of upper and lower machine, finishes the control function by the field control unit of slave computer; Again the field control result is fed back to host computer, repeat the multi-parameters optimization computing of said process, and quantity of steam and capacity of returns are realized the control of closed loop on-line optimization with the realization fractionating column.The design philosophy of computer program of the present invention is to work out the on-line optimization control program of fractionating column gas phase load and liquid phase load respectively according to the Mathematical Modeling that concerns between temperature, pressure and the controlled quentity controlled variable.Set forth Mathematical Modeling, algorithm structure and the technical characterictic of two parts program below respectively.
1, fractionating column vapour phase load on-line optimization control program (algorithm 1)
With temperature---vapor flow rate (automatic control table) is an example:
If end temperature---main contral parameter is TO, allow fluctuation deviation ± Δ TO, allowing the fluctuation codomain is TO ± Δ TO;
If sensitive plate---auxilliary temperature adjustment degree is TBO;
The permission pressure tower is: PO (MPa);
If flow---sub-control parameter is FO, and allowing upper and lower limit is that FO is big, FO is little, initial controlled quentity controlled variable FO=(FO big+FO is little)/2, and fluctuating range is Δ FO=| (FO big+FO is little) |/2;
Initial step length is K * Δ F (Δ T+ Δ TB)/Δ TO; Wherein K is a hysteresis factors, can be according to the adjustment of table type, and suitable value is 0.1--10.
Linear relationship is: Δ T+ Δ TB → FO-K * Δ F (Δ T+ Δ TB)/Δ TO
Restrained boundary Δ TB is: 0≤| Δ TB|≤3 (round numbers)
Restrained boundary (flow): FO is little≤and (Δ T+ Δ TB)/Δ TO≤FO is big for FO-K * Δ F
Control procedure:
If actual measurement principal parameter changing value is TPV (end temperature), sensitive plate temperature measured value is TBPV, end temperature deviate Δ T=TPV-TO, sensitive plate deviation delta TB=TBPV-Δ TBO.
At first judge FPV.When FO little≤FPV≤FO is big, and the actual measurement tower is when pressing PPV≤PO, by controlling as drag:
ΔT+ΔTB→FO-K×ΔF(ΔT+ΔTB)/ΔTO
When FO little≤FPV≤FO is big, and the actual measurement tower is when pressing PPV 〉=PO, by controlling as drag:
ΔT+ΔTB→FO-|K×ΔF(ΔT+ΔTB)/ΔTO|
2. fractionating column liquid phase load on-line optimization control program (algorithm 2)
With sensitive plate+top temperature → capacity of returns (automatic control table) is example:
If top temperature → principal parameter is TO, allow the fluctuation deviation to be ± Δ TO, allowing the fluctuation codomain is TO ± Δ TO;
The sensitive plate desired temperature is TBO;
The pressure tower setting value is: PO (MPa);
If flow → sub-control parameter is FO, allowing upper and lower limit is that FO is big, FO is little,
First control amount (FO) model: FO=(FO big+FO is little)/2 (or come by optimizing computings);
Fluctuating range is Δ F=| (FO big+FO is little)/2|
Step-length is: K Δ F (Δ T+ Δ TB)/Δ TO
Linear relationship is: Δ T+ Δ TB → F+K Δ F (Δ T+ Δ TB)/Δ TO
Restrained boundary is :-3≤Δ TB≤O (Δ TB round numbers)
FO is little≤and (Δ T+ Δ TB)/Δ TO≤FO is big for F+K Δ F
Control procedure:
If actual measurement principal parameter changing value is TPV (a top temperature), micro-control (sensitive plate) measured value is TBPV, Δ T=TPV-TO then, Δ TB=TBPV-TBO.
At first judge FPV.When FO little≤FPV≤FO is big, and the actual measurement tower is when pressing PPV＜PO, by controlling as drag:
ΔT+ΔTB→FO+KΔF(ΔT+ΔTB)/ΔTO
When FO little≤during the big and PO≤PPV of FPV≤FO＜PO+0.06, by controlling as drag:
ΔT+ΔTB→FO-KΔF(ΔT+ΔTB)/(ΔTO+1)
When FO little≤FPV≤FO is big, and the actual measurement tower presses PPV 〉=PO+0.06, by controlling as drag:
ΔT+ΔTB→FO-KΔF(ΔT+ΔTB)/ΔTO
After adopting this method to gas fractionator vapour, the control of liquid phase load real-time online closed-loop optimization, can make the operation of the gas fractionator in MTBE, gas fractionation unit or other device realize regulating automatically vapour in the tower, liquid phase load, avoided easily making in the former control bad phenomenon of vapour, liquid phase load imbalance in the tower, the operation of having stablized tower.Compare with the tandem control that domestic same device adopts, it is stable to have control procedure, and the computing parameter is many, control accuracy height, good energy-conserving effect, characteristics such as constant product quality.And have functions such as safety, prediction.
The invention will be further described below in conjunction with drawings and embodiments.
Fig. 1 is a MTBE device fractionating column partial material flow chart;
Fig. 2 is the control procedure block diagram;
Fig. 3 is an optimal control parameter setting program flow chart;
Fig. 4 is fractionating column vapour phase load on-line optimization control operation program flow chart;
Fig. 5 is fractionating column liquid phase load on-line optimization control operation program flow chart;
Fig. 6 is a MTBE device fractionating column multi-parameter on-line optimization control design concept block diagram.
Among Fig. 1,1 is reaction mass, and 2 is first azeotrope column, and 3 is capacity of returns, and 4 is second reactor, and 5 is second azeotrope column, and 6 is capacity of returns, and 7 is quantity of steam.
Among Fig. 2, T304 is an azeotrope column, and PT is a pressure transmitter, and TT is the column bottom temperature transmitter, TBT is the sensitive plate temperature transmitter, and FT is a flow transmitter, and DQ is an electropneumatic transducer, XWJ is a slave computer, and KBT is variable step controller (host computer), and FS sets for the vapor volume bound.
Fig. 3 is an optimal control parameter setting program flow chart.In this functional module, the user can select the initial set value of each tower quantity of steam or capacity of returns and revise relevant pre-set parameter by man-machine picture dialogue.Include: at the bottom of the tower, the tower top temperature initial value; At the bottom of the tower, tower top temperature deviation limit value; Tower is pressed limit value; Quantity of steam or capacity of returns limit value; The sensitive plate temperature limit; Hysteresis factors etc. are optimized the required various parameter values of computing.In this functional module, (throwing on-line automatic single loop regulates) quantity of steam or capacity of returns that the user can select to satisfy the requirements are thrown optimal control, also the quantity of steam or the capacity of returns of throwing optimal control can be extractd optimal control, get back to operation under the on-line automatic single loop regulative mode.
Fig. 4 is fractionating column gas phase load on-line optimization control operation program flow chart.This functional module is carried out multi-parameter integrated optimizing and is controlled required various computing.Mainly comprise the deviate Δ T, the Δ TB that at first calculate column bottom temperature and sensitive plate temperature, calculation of steam amount set-point SVO and measured deviation value Δ F limit the sensitive plate temperature then within ± 3 ℃; Whether (F is little at the setting limit value further to judge the measured value F of current quantity of steam, F is big) within, if in that (F is little, F is big) within, judge again then whether current pressure tower is lower than the setting tower and presses limit value, set the tower pressure if be lower than, then current quantity of steam optimum setting value is SV=FO-K Δ F (Δ T+ Δ TB)/Δ TO; Set tower pressure limit value if be higher than, then current quantity of steam optimum setting value is FO-|K Δ F (Δ T+ Δ TB)/Δ TO|, then best quantity of steam setting value is delivered to the variable step controller, is dealt into the slave computer field control unit and finishes the optimal control task.
Fig. 5 is fractionating column liquid phase load on-line optimization control operation program flow chart.This functional module is carried out multi-parameter integrated optimizing and is controlled required various computing.Mainly comprise the deviate Δ T, the Δ TB that at first calculate tower top temperature and sensitive plate temperature, calculate capacity of returns set-point SVO and measured deviation value Δ F, limit the sensitive plate temperature then within-3--0 ℃; Whether (F is little at the setting limit value further to judge the measured value F of current capacity of returns, F is big) within, if within (F is little, F is big), judge again then whether current pressure tower is lower than the setting tower and presses limit value, set the tower pressure if be lower than, then current capacity of returns optimum setting value is SV=FO+K Δ F (Δ T+ Δ TB)/Δ TO; Set tower pressure limit value if be higher than, then current capacity of returns optimum setting value is FO-K Δ F (Δ T+ Δ TB)/(Δ TO+1), then best capacity of returns setting value is delivered to the variable step controller, is dealt into the slave computer field control unit and finishes the optimal control task.
Fig. 6 is a MTBE device fractionating column multi-parameter on-line optimization control design concept block diagram.This functional module has been described the design and the implementing procedure of MTBE device fractionating column multi-parameter on-line optimization control.Mainly include: at first the relevant data of field computer control system is read in the optimization host computer, set picture in multi-parameter on-line optimization control parameter then and be set with related parameter by communication; Select the optimization table of vapor volume or capacity of returns respectively, when satisfying condition, can throw optimal control, give variable step advanced controller the result who optimizes computing, be dealt into the slave computer field control unit at last and finish the optimal control task.
The optimal control of gas fractionator line closed loop, carry out online dynamic optimization computing at temperature, pressure and other parameter of the gas fractionator in MTBE device, gas fractionation unit and other device exactly, and on its corresponding overhead reflux amount and the tower bottom steam amount tandem or the basis of single loop control separately, realize the multi-parameter line closed loop optimal control of gas fractionator.Be that example is illustrated now with MTBE device azeotrope column vapour phase load control procedure.
On last bit optimization machine, it is 146 ℃ by technique initialization at first with the azeotrope column column bottom temperature, allowing the fluctuation deviation setting is ± 3 ℃, the sensitive plate temperature is set at 141 ℃, the pressure restrained boundary is ≯ 0.75MPa, the quantity of steam upper limit is set at 4.4T/H, under be limited to 1T/H, hysteresis factors K is set at 1.0, throws on-line optimization control this moment.Carry out algorithm 1 computing by the optimization machine, the excellent control value of the quantity of steam that computing is obtained is given the variable step controller again, as the initial controlled quentity controlled variable of tower bottom steam amount; The Optimal Control amount that the variable step size controller is obtained is issued slave computer by the communication of upper and lower machine again, finishes column bottom temperature and quantity of steam near the column bottom temperature optimal value or the balance adjustment of quantity of steam bound in setting by the field control unit of slave computer again.Field control unit will be controlled the result and feed back to the bit optimization machine by TT, TBT, FT, PT, repeat said process then.
Claims (4)
1, a kind of multiparameter on-line optimization control method for gas dephlegmation tower, it is characterized in that it is to be provided with one to finish the host computer of optimizing computing and control on the existing computer control system of process units, computer with existing control system is a slave computer, and carries out as follows:
A. determine according to the Mathematical Modeling that concerns between temperature, pressure and the controlled quentity controlled variable
I) fractionating column vapour phase load on-line optimization control algolithm;
Ii) fractionating column liquid phase load on-line optimization control algolithm;
B. work out online optimal control program according to control algolithm;
C) the online optimal control program of operation.
2, optimal control method according to claim 1 is characterized in that said fractionating column gas phase load on-line optimization control algolithm content comprises:
A, online excellent control relevant parameter is set;
B, deviate Δ T, the Δ TB of calculating column bottom temperature and sensitive plate temperature, calculation of steam amount set-point SVO and measured deviation value Δ F;
C, restriction sensitive plate temperature deviation is within ± 3 ℃;
D, whether the measured value F that judges current quantity of steam, then withdraws from as not existing setting within the limit value;
E judges whether current pressure tower is lower than the setting tower and presses limit value;
F sets the tower pressure if be lower than, and then current quantity of steam optimum setting value is SV=FO-K Δ F (Δ T+ Δ TB)/Δ TO;
G sets tower pressure limit value if be higher than, and then current quantity of steam optimum setting value is FO-|K Δ F (Δ T+ Δ TB)/Δ TO|;
H delivers to the variable step controller with optimum value quantity of steam setting value, is dealt into the slave computer field control unit and finishes optimal control.
3, optimal control method according to claim 1 is characterized in that said fractionating column liquid phase load on-line optimization control algolithm content comprises:
A, online excellent control relevant parameter is set;
B, deviate Δ T, the Δ TB of calculating tower top temperature and sensitive plate temperature calculate capacity of returns set-point SVO and measured deviation value Δ F;
C, restriction sensitive plate temperature deviation is within-3--0 ℃;
D, whether the measured value F that judges current capacity of returns, then withdraws from as not existing setting within the limit value;
E judges whether current pressure tower is lower than the setting tower and presses limit value;
F sets the tower pressure if be lower than, and then current capacity of returns optimum setting value is SV=FO+K Δ F (Δ T+ Δ TB)/Δ TO;
G sets tower pressure limit value if be higher than, and then current capacity of returns optimum setting value is FO-K Δ F (Δ T+ Δ TB)/(Δ TO+1);
H delivers to the variable step controller with best capacity of returns setting value, is dealt into the slave computer field control unit and finishes optimal control.
4, optimal control method according to claim 1, it is characterized in that said on-line optimization control program is that the computer program of fractionating column vapour phase load on-line optimization control algolithm and fractionating column liquid phase load on-line optimization control algolithm is realized that wherein the on-line setup parameter request is:
A, vapour phase load limit sensitive plate temperature deviation is at-3 ℃--within 3 ℃;
B, liquid phase load limit sensitive plate temperature deviation is at-3 ℃--within 0 ℃;
C, hysteresis factors K=0.1--10.
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| CN96115404A CN1048642C (en) | 1996-06-25 | 1996-06-25 | Multiparameter on-line optimization control method for gas dephlegmation tower |
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| CN96115404A CN1048642C (en) | 1996-06-25 | 1996-06-25 | Multiparameter on-line optimization control method for gas dephlegmation tower |
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| CN1048642C CN1048642C (en) | 2000-01-26 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100337711C (en) * | 2001-09-19 | 2007-09-19 | 拜尔技术服务有限责任公司 | Method for controlling the process of separating mixtures containing several substances |
| US8898018B2 (en) | 2007-03-06 | 2014-11-25 | Schlumberger Technology Corporation | Methods and systems for hydrocarbon production |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP6346582B2 (en) * | 2015-03-26 | 2018-06-20 | アズビル株式会社 | Control apparatus and control method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| SU825618A1 (en) * | 1979-08-20 | 1981-04-30 | Kd Polt Inst | Method of automatic control of fermentation column of fermentized material rectification apparatus |
| DE3303571C2 (en) * | 1982-03-11 | 1984-07-26 | Buckau-Walther AG, 4048 Grevenbroich | Process and plant for the production of ethanol |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100337711C (en) * | 2001-09-19 | 2007-09-19 | 拜尔技术服务有限责任公司 | Method for controlling the process of separating mixtures containing several substances |
| US8898018B2 (en) | 2007-03-06 | 2014-11-25 | Schlumberger Technology Corporation | Methods and systems for hydrocarbon production |
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