CN103472722A - Control method and system for petrochemical industry - Google Patents

Abstract

The invention discloses a control method and system for the petrochemical industry to solve the problem that due to the fact that parameters are controlled through manual operation in an existing control method and system, the control is not accurate, and the resource allocation is not optimized enough. The control method includes the steps of firstly, collecting or receiving production parameters of machining of an oil refinery in a given period of time; secondly, under the constraint conditions that the primary machining corresponding to a feed and crude distillation device and the secondary machining, refined oil product blending and delivery corresponding to a second machining device are simulated, solving the production parameters through a linear or non-linear optimization, and thereby generating control parameters; thirdly, generating control instructions according to the control parameters; fourthly, controlling production procedures of the machining of the oil refinery according to the control instructions. The control method has the advantages of being rapid in response, accurate in control and the like, the resource allocation of raw materials and devices is facilitated, therefore, production cost is reduced, and production efficiency is improved.

Description

Control method and system for petrochemical industry

Technical field

The present invention relates to the petrochemical technology field, particularly a kind of control method for petrochemical industry and system.

Background technology

The oil-refining chemical station-service, in the control parameter of controlling petrochemical industry processing, is by manually according to actual manufacturing parameter, manually deriving and obtain.Derive the manually strong experience that depends on the assigned work personnel, professional skill and duty.And the raw material type that petrochemical iy produced relates to is many, procedure of processing is numerous and diverse, often not only accuracy in computation and degree of accuracy are inadequate in manual analyzing calculating, also can't obtain optimized control parameter, often cause that working (machining) efficiency is low, wastage of material and stock or lack, finally all cause the problems such as production cost increase.

Summary of the invention

(1) technical matters that will solve

The technical problem to be solved in the present invention is: how a kind of control method for petrochemical industry and system are provided, the difficulty of making reduce to control parameter, and the optimal control parameter so that produce more smooth and easy, reduce production costs, enhance productivity.

(2) technical scheme

For addressing the above problem, the present invention comprises for the control method of petrochemical industry:

Gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, adopt linear or non-linear optimizing to solve described manufacturing parameter, control parameter thereby generate;

According to the instruction of described control parameter formation control;

Control the production procedure of refinery processing according to described steering order.

Further,

Simulating the secondary processing that described secondary processing device is corresponding adopts following formula to carry out:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _d? _min≤Q _d≤Q _d? _max，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{W}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{W}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d,

the initial tank farm stock of the mixed feeding of secondary processing scheme d, initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _d? _minthe feed properties that is the secondary processing scheme d allows the minimum value reached, Q _d? _maxthe feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream,

the tank farm stock of secondary discharging m when production is initial,

the tank farm stock of secondary discharging m when producing end, Δ Q _dq _dthe difference that departs from basic value,

for Q _dw while often departing from a unit of basic value _{d, m}modified value, Δ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m, the initial stock's of secondary discharging m property value,

for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l q _d? _min, Q _d? _max, W _{d, m},

q _{d, m}

and

all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{l, d}, Q _d, F _d, F _{m, e},

Δ Q _d, Δ T _d, and Q _m.

Further, simulating the time processing that described crude(oil)unit is corresponding adopts following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _b? _min≤Q _b≤Q _b? _max，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}\×Q_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max },$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max },$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _b? _minthat under distillation processing scheme b, feed properties allows the minimum value reached, Q _b? _maxthat the distillation processing scheme is that lower feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b,

that distillation discharging u is producing initial tank farm stock,

the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TR}? _minthe least commitment value of atmospheric tower machining load in TR, C _{aTM, TRmax}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TRmin}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TRmax}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _bmin, Q _bmax, W _{i, b, u},

q _{i, b, u}

c _{aTM, TRmin}, C _{aTM, TRmax}, C _{vTM, TRmin}, C _{vTM, TRmax}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c},

and Q _u.

Further, adopt the distribution recursive algorithm to solve described control parameter.

Further, when adopting the distribution recursive algorithm to solve described control parameter, the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}\×Q_{i,b,u}+Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1)};$

Q _uspan be $[\min \left(Q_{i,b,u,}{Q}_u^{p-1}\right),\max \left(Q_{i,b,u}{Q}_u^{p-1}\right)].$

Further, when adopting the distribution recursive algorithm to solve described control parameter, the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min \left(Q_{d,m,}{Q}_m^{p-1}\right),\max \left(Q_{d,m,}{Q}_m^{p-1}\right)].$

Further, when adopting the distribution recursive algorithm to solve described control parameter, for each carries out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is l/dd, and for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.

Further, generating described control parameter specifically comprises:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, in each time quantum, the fluctuation of all manufacturing parameters is not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

For addressing the above problem, the present invention comprises the manufacturing parameter harvester, controls parameter generating apparatus, steering order generating apparatus and controller for the control system of petrochemical industry;

Described harvester, gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Described control parameter generating apparatus, in order at simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding, be in harmonious proportion and the constraint condition of shipment under, adopt linearity or nonlinear optimization to solve described manufacturing parameter, thereby generate, control parameter;

Described steering order generating apparatus, receive described control parameter and according to the instruction of described control parameter formation control;

Described controller, in order to receive and to control according to described steering order the production procedure of refinery processing.

Further,

Described control parameter generating apparatus adopts following formula to carry out in order to simulate the secondary processing that described secondary processing device is corresponding:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _dmin≤Q _d≤Q _dmax，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{W}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{W}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d,

the initial tank farm stock of the mixed feeding of secondary processing scheme d,

initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _dminthe feed properties that is the secondary processing scheme d allows the minimum value reached, Q _dmaxthe feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream,

the tank farm stock of secondary discharging m when production is initial,

the tank farm stock of secondary discharging m when producing end, △ Q _dq _dthe difference that departs from basic value,

for Q _dw while often departing from a unit of basic value _{d, m}modified value, △ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m,

the initial stock's of secondary discharging m property value,

for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l q _dmin, Q _dmax, W _{d, m},

q _{d, m}

and

all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{l, d}, Q _d, F _d, F _{m, e}, △ Q _d, △ T _d, and Q _m.

Further,

Described control parameter generating apparatus, simulate the time processing that described crude(oil)unit is corresponding and adopt following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _bmin≤Q _b≤Q _bmax，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}\×Q_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max },$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max },$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _bminthat under distillation processing scheme b, feed properties allows the minimum value reached, Q _bmaxthat under distillation processing scheme b, feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b,

that distillation discharging u is producing initial tank farm stock,

the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TRmin}the least commitment value of atmospheric tower machining load in TR, C _{aTM, TRmax}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TRmin}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TRmax}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _bmin, Q _bmax, W _{i, b, u}, q _{i, b, u},

c _{aTM, TRmin}, C _{aTM, TRmax}, C _{vTM, TRmin}, C _{vTM, TRmax}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c}, and Q _u.

Further, described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter.

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}\×Q_{i,b,u}+Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1)};$

Q _uspan be $[\min \left(Q_{i,b,u,}{Q}_u^{p-1}\right),\max \left(Q_{i,b,u,}{Q}_u^{p-1}\right)].$

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min \left(Q_{d,m,}{Q}_m^{p-1}\right),\max \left(Q_{d,m,}{Q}_m^{p-1}\right)].$

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, for each carries out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is 1/dd, and for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.

Further, described control parameter generating apparatus specifically in order to:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, make the fluctuation of manufacturing parameters all in each time quantum be not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

(3) the present invention is used for control method and the system beneficial effect of petrochemical industry:

First: the present invention is for control method and the system of petrochemical industry, simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, thereby by computing machine, adopt linearity or non-linear optimizing to solve described manufacturing parameter and generate the control parameter, replace manually and derive, there is more quick, the accurate advantage of calculating, thereby reduced the error of deriving and forming manually, the phenomenon that wastage of material or defect rate are high, thus have advantages of and reduce production costs;

Second: thereby adopt linearity or non-linear optimizing to solve described manufacturing parameter by computing machine, generate the control parameter, what obtain thus is the control parameter after optimizing, control parameter again for production control, thereby obtained being conducive to enhance productivity, improve the utilization factor of material, the advantage reduced production costs.

The 3rd: the present invention is for control method and the system of petrochemical industry, described in the simulation charging, the time processing that crude(oil)unit is corresponding, the secondary processing that the secondary processing device is corresponding, under the constraint condition of product oil mediation and shipment, considered the character of material, flow, temperature in processing, pressure, the parameters such as duration, the while dynamic similation, follow the tracks of the variation of each parameter at the appointed time, thereby to the simulation of actual production closing to reality more, optimize the control parameter obtained by the multicycle more reasonable to the control of producing, thereby again suboptimization control, be conducive to again optimize production, have and raise the efficiency, the advantage such as reduce costs.

The accompanying drawing explanation

Fig. 1 is the described schematic flow sheet of the control method for petrochemical industry of the embodiment of the present invention;

Fig. 2 is one of described structural representation of the control system for petrochemical industry of the embodiment of the present invention;

Two of the described structural representation of the control system for petrochemical industry of Fig. 3 embodiment of the present invention.

Embodiment

Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in further detail.Following examples are used for the present invention is described, but are not used for limiting the scope of the invention.

Embodiment 1

As shown in Figure 1, the present embodiment comprises for the control method of petrochemical industry:

Step S1: gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Step S2: simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, adopt linearity or non-linear optimizing to solve described manufacturing parameter, thereby generate, control parameter;

Step S3: according to the instruction of described control parameter formation control;

Step S4: control the production procedure of refinery processing according to described steering order.

Oil refining in petrochemical industry processing refers to petroleum refining, is the method by physical separation or chemical conversion by oil, produces the production run of the fuel oil such as kerosene, gasoline, diesel oil, heavy oil, paraffin and industrial lubricant.The raw material related in the petrochemical industry process comprises by materials such as the catalyzer of heterogeneity and the crude oil that becomes to be grouped into, various reactions, promoter, and the equipment related to is also multiple pattern most amounts.Simulate in the present embodiment pan feeding, shipment and the middle process of the material of the main process equipment of refinery by the constraint condition extracted, and calculated the control parameter by computer equipment.In traditional control method, about control parameters such as the material linkings between input, output, processing and the processing unit (plant) of material, by manually being derived according to individual experience.Due to the procedure of processing that the material variety related to is many, relate to, reaction and flow process complexity, artificial derivation always be difficult to obtain one rationally, the control parameter of resource best configuration, occur while causing concrete controlled working that thereby the various errors that cause because of human factor occur that on wastage of material, the idleness of equipment or production line, part process equipment load is excessive, equipment component is being treated defective or unnecessary too high of work state, the product quality of producing again, causes that production efficiency is low, processing cost is high.And in the described control method of the present embodiment, the model of the correspondence of charging, crude distillation, secondary processing, product oil mediation and shipment is abstracted into can be for the model calculated, calculate factor more accurate, that consider comprehensive and comprehensive, and solved by equipment such as computing machines, and unartificial solving solved the limitations such as human error that above-mentioned artificial derivation causes easily.Therefore, while adopting the described control method of the present embodiment to be monitored refinery, control more accurate; Refinery is produced according to above-mentioned control method, and production efficiency is high, it is little to waste, finished product character is good, and production cost has reduced greatly.

Wherein, described crude distillation refers to the process that crude oil is separated according to different boiling points; Described secondary processing refers to makes with extra care again to the semi-manufacture after crude distillation separates; Described product oil is in harmonious proportion and refers to that the finished product of take after secondary processing is object, by various finished products with the ratio of presetting, the manufacturing process that character is mixed to form required article.

Embodiment 2

The described control method for petrochemical industry processing of the present embodiment comprises

Step 1: gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Step 2: simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, adopt linearity or non-linear optimizing to solve described manufacturing parameter, thereby generate, control parameter;

Step 3: according to the instruction of described control parameter formation control;

Step 4: control the production procedure of refinery processing according to described steering order.

Wherein, simulating the secondary processing that described secondary processing device is corresponding adopts following formula to carry out:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _d? _min≤Q _d≤Q _d? _max，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{W}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{W}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d,

the initial tank farm stock of the mixed feeding of secondary processing scheme d, initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _d? _minthe feed properties that is the secondary processing scheme d allows the minimum value reached, Q _d? _maxthe feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream,

the tank farm stock of secondary discharging m when production is initial, the tank farm stock of secondary discharging m when producing end, △ Q _dq _dthe difference that departs from basic value,

for Q _dw while often departing from a unit of basic value _{d, m}modified value, △ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m,

the initial stock's of secondary discharging m property value, for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l

q _d? _min, Q _d? _max, W _{d, m},

q _{d, m}

and

all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, d}, Q _d, Q _d, F _{m, e}, △ Q _d, △ T _d, and Q _m.

The constraint condition of simulating described secondary processing can have multiple, and the present embodiment provides a kind of constraint condition of particularly, preferably simulating secondary processing with respect to embodiment 1.The constraint condition that adopts above-mentioned formula to form, taken into full account the character of material (as parameter Q _l), also introduced Q _d, Δ Q _dand

etc. parameter, when departing from basic value, material properties revised controlling parameter.Concrete is as follows: Δ Q wherein _dfor feed properties Q under scheme d _ddepart from basic value q _ddifference, i.e. Δ Q _d=Q _d-q _d;

for character Q _doften depart from basic value q _dyield W during a unit _{d, m}modified value.

when all character that are charging depart from its basic value to the modified value sum of material m yield.Depart from reference value owing to having taken into full account material properties, the simulation production and processing process is the closing to reality situation more, also more reasonable, the control parameter obtained is also more reasonable, thereby during production control, production procedure product property more smooth and easy, that produce meets the requirements, thus again suboptimization production.

Embodiment 3

The present embodiment, on the basis of embodiment 2, further provides the constraint condition of one group of Optimized Simulated time processing, and concrete is as follows:

Simulating the time processing that described crude(oil)unit is corresponding adopts following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _bmin≤Q _b≤Q _bmax，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}\×Q_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max },$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max ,}$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _bminthat under distillation processing scheme b, feed properties allows the minimum value reached, Q _bmaxthat under distillation processing scheme b, feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b,

that distillation discharging u is producing initial tank farm stock,

the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TRmin}the least commitment value of atmospheric tower machining load in TR, C _{aTM, TRmax}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TRmin}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TRmax}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _bmin, Q _bmax, W _{i, b, u},

q _{i, b, u},

c _{aTM, TRmin}, C _{aTM, TRmax}, C _{vTM, TRmin}, C _{vTM, TRmax}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c},

and Q _u.

Constraint condition in the present embodiment has been simulated a plurality of work flows of refinery Crude Oil distilling apparatus, by being superimposed of above-mentioned work flow linearity, define one and just paid close attention to the character of charging, charging control, discharging, charging and discharging, the constraint condition of discharge relation, accurately, fully reflected the actual conditions of producing, thereby made the production control parameter more be conducive to optimal control.

In concrete implementation procedure, calculate described control parameter and can adopt multiple computing method, preferentially adopt in the present embodiment the distribution recursive algorithm to solve described control parameter.The present embodiment, then solves and obtains a plurality of majorization of solutions values by optimizing the nonlinear problem linearization process by the distribution recursive algorithm, and the control parameter therefore obtained is also the parameter after optimizing, and then has optimized production.

Embodiment 4

The described control method for petrochemical industry processing of the present embodiment, on the basis of above-described embodiment 3, when adopting the distribution recursive algorithm to solve described control parameter, the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}\×Q_{i,b,u}+Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1)};$

Q _uspan be $[\min (Q_{i,b,u},Q_u^{p-1}),\max (Q_{i,b,u},Q_u^{p-1})].$

Further, when adopting the distribution recursive algorithm to solve described control parameter, the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min \left(Q_{d,m,}{Q}_m^{p-1}\right),\max \left(Q_{d,m,}{Q}_m^{p-1}\right)].$

Above-mentioned Q _u, Q _mspan can carry out value according to the actual conditions of material, by the setting of span, be convenient to the constringent raising of result, thereby reduced calculated amount.Concrete example is many cover processing scheme (such as diesel oil scheme and gasoline scheme etc.) oil that all steams as, one of secondary processing device catalytic cracking exists, and the initial guess of oil properties that this device steams (such as sulfur content) can be expressed as above formula.Wherein, d means processing scheme, W _{d, m}mean the processing scheme d oily yield that steams, Q _{d, m}mean lower oil properties of steaming of processing scheme d,

the character that means the initial stock of this gasoline.Lower oil properties Q that steams of each scheme _{d, m}with numerical value corresponding minimum and maximum restriction respectively minimum and maximum in stock's character.

In addition, when adopting the distribution recursive algorithm to solve described control parameter, for each, carry out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is 1/dd, and for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.Concrete as, certain discharging u of crude(oil)unit may flow to four kinds of work flows of secondary processing device, and all there is not the constraint that processing capacity is 0 in these four kinds of work flows, for this quadruplet processing scheme, the initial value of the error distribution coefficient that material u introduces is 0.25.

Embodiment 5

The present embodiment, on the basis of embodiment 3 or embodiment 4, has carried out further improvement, refinement the generation of described control parameter, specific as follows:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, in each time quantum, the fluctuation of all manufacturing parameters is not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

In the present embodiment, fluctuation to the manufacturing parameter that receives or gather in is at the appointed time judged, when fluctuation at the appointed time occurs in scope in manufacturing parameter, it is divided into to several time quantums successively according to time sequencing, data in each unit are not fluctuateed, and between each adjacent cells, partial data fluctuates, the optimization problem built thus is to optimize the multicycle, the convenient generation for the control parameter in each time period, improve the precision of controlling.

In addition, the present embodiment also provides a kind of constraint condition that product oil is in harmonious proportion of simulating:

Specific as follows: $Q_{o\min }\≤\frac{\underset{n}{\mathrm{\Σ}}{F}_{n,o}*Q_n}{\underset{n}{\mathrm{\Σ}}{F}_{n,o}}\≤Q_{o\max }$ Formula (A)

This formula has characterized the character constraint of reconciliation scheme o.The product property of reconciliation scheme is obtained through weighted mean by the character of each blend component.Wherein, Q _nthe property value of blend component n, F _{n, o}the flow of component n for being in harmonious proportion,

it is the property value of product.Q _ominand Q _omaxminimum value and the maximal value that product property allows.

Especially, if there is in twos reciprocation in blend component between component, the physical property that is potpourri is not that the linear weighted function of each component physical property is average, but has on this basis extra modified value, and the formula (A) that characterizes the constraint of mediation the physical property of product can be expressed as:

$Q_{o\min }\≤\frac{\underset{n}{\mathrm{\Σ}}{F}_{n,o}*Q_n+\underset{r,s\∈n}{\underset{r\≠s}{\mathrm{\Σ}}}{Y}_{\mathrm{rs}}*F_{s,o}}{\underset{n}{\mathrm{\Σ}}{f}_{n,o}}\≤Q_{o\max }$ Formula (B)

Wherein, Y _rsthe reciprocal effect produced while being blend component r and s mixing.

$F_{n,o}=X_{n,o}*\underset{n}{\mathrm{\Σ}}{F}_{n,o}$ Formula (C)

Formula (C) is for characterizing the flow proportional of blend component.Wherein,

the total amount that means product, X _{n, o}mean that blend component n accounts for the ratio of product population.Charging n is one or more in raw material i, distillation scheme discharging u, secondary processing scheme discharging m.

In addition, in the embodiment of the present invention 1 to embodiment 5, the relation according to the tank farm stock of material also may meet following constraint: ${\mathrm{INV}}_{z\min }^P\≤{\mathrm{INV}}_z^P\≤{\mathrm{INV}}_{z\max }^P$

Wherein,

the tank farm stock of material z when producing end,

with

minimum value and the maximal value of material z tank farm stock of permission when producing end.

In the embodiment of the present invention, the flow of related all materials can be both volumetric flow rate, can be also mass rate; The character that relates to material can be both the volume type, can be also mass type.But the product of flow and character must be based on same standard, and volumetric flow rate and volume type character multiply each other, or mass rate and mass type character multiply each other.When standard is inconsistent, the conversion relation between volumetric flow rate and mass rate is as follows:

F _w，z=F _x，z*S _z

Wherein, F _{w, z}the mass rate of material z, F _{v, z}the volumetric flow rate of material z, S _zdensity (quality of unit volume) for material z.

The flow F of the material z related in above-mentioned model _zmay there is following constraint:

F _zmin≤F _z≤F _zmax

Wherein, F _zminand F _zmaxminimum and the maximum constrained value of material z flow.

Comprehensively above-mentioned, it is a kind of by the processing of simulation petrochemical industry that embodiment 1 to embodiment 5 provides, and automatically generates the control parameter by watch-dogs such as computing machines and realize the method to the control of concrete processing.Adopt said method to have and control the advantages such as accurate, that production efficiency is high, production cost is low.

Embodiment 6:

As shown in Figure 2, the present embodiment comprises manufacturing parameter harvester 1, controls parameter generating apparatus 2, steering order generating apparatus 3 and controller 4 for the control system of petrochemical industry;

Described harvester 1, gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Described control parameter generating apparatus 2, in order at simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding, be in harmonious proportion and the constraint condition of shipment under, adopt linearity or nonlinear optimization to solve described manufacturing parameter, thereby generate, control parameter;

Described steering order generating apparatus 3, receive described control parameter and according to the instruction of described control parameter formation control;

Described controller 4, in order to receive and to control according to described steering order the production procedure of refinery processing.

The control system of the petrochemical industry described in the present embodiment, relatively traditional system has been set up described control parameter generating apparatus 2, can produce and control parameter according to the manufacturing parameter that gathers or receive voluntarily, and without input after deriving manually, thereby intellectuality is higher, also more efficient and convenient with respect to deriving manually, the control parameter simultaneously formed is production control more accurately, thereby be conducive to reduce the waste of producing Raw, the generation of inferior oil product, improved production efficiency and reduced production cost.

Embodiment 7:

The present embodiment comprises manufacturing parameter harvester 1, controls parameter generating apparatus 2, steering order generating apparatus 3 and controller 4 for the control system of petrochemical industry;

Described harvester 1, gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Described control parameter generating apparatus 2, in order at simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding, be in harmonious proportion and the constraint condition of shipment under, adopt linearity or nonlinear optimization to solve described manufacturing parameter, thereby generate, control parameter;

Described steering order generating apparatus 3, receive described control parameter and according to the instruction of described control parameter formation control;

Described controller 4, in order to receive and to control according to described steering order the production procedure of refinery processing.

Concrete described control parameter generating apparatus 3 adopts following formula to carry out in order to simulate the secondary processing that described secondary processing device is corresponding:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _d?min≤Q _d≤Q _d?max，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{W}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{W}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d,

the initial tank farm stock of the mixed feeding of secondary processing scheme d,

initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _{d min}the feed properties that is the secondary processing scheme d allows the minimum value reached, Q _{d max}the feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream, the tank farm stock of secondary discharging m when production is initial,

the tank farm stock of secondary discharging m when producing end, Δ Q _dq _dthe difference that departs from basic value,

for Q _dw while often departing from a unit of basic value _{d, m}modified value, Δ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m,

the initial stock's of secondary discharging m property value,

for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l q _{d min}, Q _{d max}, W _{d, m},

q _{d, m} and

all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{l, d}, Q _d, F _d, F _{m, e},

Δ Q _d, Δ T _d, and Q _m.

The constraint condition that described control parameter generating apparatus 3 specific implementations are simulated described secondary processing can have multiple, and the present embodiment provides one group of constraint condition of particularly, preferably simulating secondary processing with respect to embodiment 1.The constraint condition that adopts above-mentioned formula to form, taken into full account the character of material (as parameter Q _l), also introduced Q _d, Δ Q _dand

etc. parameter, when departing from basic value, material properties revised controlling parameter.Concrete is as follows: Δ Q wherein _dfor feed properties Q under scheme d _ddepart from basic value q _ddifference, i.e. Δ Q _d=Q _d-q _d;

for character Q _doften depart from basic value q _dyield W during a unit _{d, m}modified value.

flow process closing to reality situation more, also more reasonable, the control parameter obtained is also more reasonable, thus during production control, production procedure product property compliance rate more smooth and easy, that produce is higher, thereby again suboptimization production.

Embodiment 8:

The present embodiment on the basis of above-described embodiment 6 and embodiment 7, described control parameter generating apparatus, simulate time processing corresponding to described crude(oil)unit and adopt following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _b?min≤Q _b≤Q _b?max，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}{\×Q}_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max ,}$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max },$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _{b min}that under distillation processing scheme b, feed properties allows the minimum value reached, Q _{b max}that under distillation processing scheme b, feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b,

that distillation discharging u is producing initial tank farm stock,

the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TRmin}the least commitment value of atmospheric tower machining load in TR, C _{aTM, TRmax}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TRmin}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TRmax}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _bmin, Q _bmax, W _{i, b, u},

q _{i, b, u},

c _{aTM, TRmin}c _{aTM, TRmax}c _{vTM, TRmin}c _{vTM, TRmax}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c}, and Q _u.

Embodiment 9:

The described control system for petrochemical industry of the present embodiment, on the basis of above-described embodiment 6-embodiment 8, further stipulated that described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter.

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}\×Q_{i,b,u}+Q_u^{p-1}}{\left(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1\right)};$

Q _uspan be $[\min (Q_{i,b,u},Q_u^{p-1}),\max (Q_{i,b,u},Q_u^{p-1})].$

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min (Q_{d,m},Q_m^{p-1}),\max (Q_{d,m},Q_m^{p-1})].$

Further, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, for each carries out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is 1/dd, and for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.

Further, described control parameter generating apparatus specifically in order to:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, in each time quantum, the fluctuation of all manufacturing parameters is not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

Comprehensively above-mentioned, the described control system for petrochemical industry of embodiment 6-embodiment 9, corresponding complete the control method for petrochemical industry of the present invention.

The concrete structure of the described control system for petrochemical industry of another one also is provided in addition, as shown in Figure 3:

The described control system for petrochemical industry comprise at least one processor 7 (for example: CPU), at least one interface 6 or other communication interfaces, storer 5 and at least one communication bus 8, for realizing the connection communication between these devices.Processor 7 for example, for the executable module of execute store 5 storages: computer program.Storer 5 may comprise high-speed random access memory (Random Access Memory, RAM), ROM (read-only memory) (ROM) also may also comprise non-unsettled storer (non-volatile memory), for example: at least one magnetic disk memory.Realize the communication connection between this system gateway and at least one other network element by least one network interface (can be wired or wireless), can use internet, wide area network, local network, Metropolitan Area Network (MAN) etc.

In some embodiments, storer 5 has been stored program, and program can be carried out by processor 7, and this program operation at least can realize following functions:

Gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, adopt linear or non-linear optimizing to solve described manufacturing parameter, control parameter thereby generate;

According to the instruction of described control parameter formation control;

Control the production procedure of refinery processing according to described steering order.

In concrete implementation process, corresponding each implementation step comprises the device of an independent structure as described in Figure 3.

The described base station maintenance device of the present embodiment, have advantages of simple in structure, realize easy, hardware cost is low.

Above embodiment is only for illustrating the present invention; and be not limitation of the present invention; the those of ordinary skill in relevant technologies field; without departing from the spirit and scope of the present invention; can also make a variety of changes and modification; therefore all technical schemes that are equal to also belong to category of the present invention, and scope of patent protection of the present invention should be defined by the claims.

Claims (16)

1. the control method for petrochemical industry, is characterized in that, comprising:

Gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding be in harmonious proportion and the constraint condition of shipment under, adopt linear or non-linear optimizing to solve described manufacturing parameter, control parameter thereby generate;

According to the instruction of described control parameter formation control;

Control the production procedure of refinery processing according to described steering order.

2. method according to claim 1, is characterized in that,

Simulating the secondary processing that described secondary processing device is corresponding adopts following formula to carry out:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _d?min≤Q _d≤Q _d?max，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{W}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{W}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d,

the initial tank farm stock of the mixed feeding of secondary processing scheme d, initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _{d min}the feed properties that is the secondary processing scheme d allows the minimum value reached, Q _{d max}the feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream,

the tank farm stock of secondary discharging m when production is initial,

the tank farm stock of secondary discharging m when producing end, △ Q _dq _dthe difference that departs from basic value, for Q _dw while often departing from a unit of basic value _{d, m}modified value, △ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m,

the initial stock's of secondary discharging m property value,

for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l,

q _{d min}, Q _{d max}, W _{d, m},

q _{d, m}, and

all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{l, d}, Q _d, F _d, F _{m, e},

△ Q _d, △ T _d, and Q _m.

3. method according to claim 2, is characterized in that, simulates the time processing that described crude(oil)unit is corresponding and adopt following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _b?min≤Q _b≤Q _b?max，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}\×Q_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max },$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max },$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _{b min}that under distillation processing scheme b, feed properties allows the minimum value reached, Q _{b max}that under distillation processing scheme b, feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b, that distillation discharging u is producing initial tank farm stock, the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TR min}the least commitment value of atmospheric tower machining load in TR, C _{aTM, TR max}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TR min}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TR max}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _{b min}, Q _{b max}, W _{i, b, u},

q _{i, b, u},

c _{aTM, TR min}, C _{aTM, TR max}, C _{vTM, TR min}, C _{vTM, TR max}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c},

and Q _u.

4. method according to claim 3, is characterized in that, adopts the distribution recursive algorithm to solve described control parameter.

5. method according to claim 4, is characterized in that, when adopting the distribution recursive algorithm to solve described control parameter, and the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}\×Q_{i,b,u}+Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1)};$

Q _uspan be $[\min (Q_{i,b,u},Q_u^{p-1}),\max (Q_{i,b,u},Q_u^{p-1})].$

6. method according to claim 5, is characterized in that, when adopting the distribution recursive algorithm to solve described control parameter, and the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min (Q_{d,m},Q_m^{p-1}),\max (Q_{d,m},Q_m^{p-1})].$

7. according to right 4,5 or 6 described methods, it is characterized in that, when adopting the distribution recursive algorithm to solve described control parameter, for each carries out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and, for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is l/dd, for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.

8. according to claim 4,5 or 6 described methods, it is characterized in that, generate described control parameter and specifically comprise:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, in each time quantum, the fluctuation of all manufacturing parameters is not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

9. the control system for petrochemical industry, is characterized in that, comprises the manufacturing parameter harvester, controls parameter generating apparatus, steering order generating apparatus and controller;

Described harvester, gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Described control parameter generating apparatus, in order at simulation charging, time processing that crude(oil)unit is corresponding, secondary processing, product oil that the secondary processing device is corresponding, be in harmonious proportion and the constraint condition of shipment under, adopt linearity or nonlinear optimization to solve described manufacturing parameter, thereby generate, control parameter;

Described steering order generating apparatus, receive described control parameter and according to the instruction of described control parameter formation control;

Described controller, in order to receive and to control according to described steering order the production procedure of refinery processing.

10. system according to claim 9, is characterized in that,

Described control parameter generating apparatus adopts following formula to carry out in order to simulate the secondary processing that described secondary processing device is corresponding:

$\frac{\underset{l}{\mathrm{\Σ}}{F}_{l,d}\×Q_l+{\mathrm{INV}}_d^{p-1}\×Q_d^{p-1}}{\underset{l}{\mathrm{\Σ}}{F}_{l,d}+{\mathrm{INV}}_d^{p-1}}=Q_d,$

Q _dmin≤Q _d≤Q _dmax，

$\underset{e}{\mathrm{\Σ}}{F}_{m,e}=\underset{d}{\mathrm{\Σ}}{F}_d\×(W_{d,m}+\underset{Q_d}{\mathrm{\Σ}}{\mathrm{\ΔQ}}_d\×{\mathrm{\ΔW}}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}{\mathrm{\ΔT}}_d\×{\mathrm{\ΔW}}_{T_d,d,m})+({\mathrm{INV}}_m^{p-1}-{\mathrm{INV}}_m^p),$

$\frac{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}\×(Q_{d,m}+\underset{Q_d}{\mathrm{\Σ}}\mathrm{\Δ}{Q}_d\×\mathrm{\Δ}{Q}_{Q_d,d,m}+\underset{T_d}{\mathrm{\Σ}}\mathrm{\Δ}{T}_d\×\mathrm{\Δ}{Q}_{T_d,d,m})+{\mathrm{INV}}_m^{p-1}\×Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{F}_d\×W_{d,m}+{\mathrm{INV}}_m^{p-1}}=Q_m,$

Wherein, Q _lthe property value of charging l, F _{l, d}the flow of charging l under the secondary processing scheme d, the initial tank farm stock of the mixed feeding of secondary processing scheme d,

initial stock's property value, Q _dthe property value of secondary processing scheme d mixed feeding, Q _dminthe feed properties that is the secondary processing scheme d allows the minimum value reached, Q _dmaxthe feed properties that is the secondary processing scheme d allows the maximal value reached;

F _dthe inlet amount of secondary processing scheme d, W _{d, m}the yield of the secondary discharging m of secondary processing scheme d, F _{m, e}the amount of the processing scheme e consumption secondary discharging m in secondary processing scheme d downstream,

the tank farm stock of secondary discharging m when production is initial,

the tank farm stock of secondary discharging m when producing end, Δ Q _dq _dthe difference that departs from basic value, for Q _dw while often departing from a unit of basic value _{d, m}modified value, Δ T _dfor machined parameters T under the secondary processing scheme d _dthe difference that departs from basic value,

for machined parameters T _dw while often departing from a unit of basic value _{d, m}modified value;

Q _{d, m}the property value of secondary discharging m,

the initial stock's of secondary discharging m property value,

for Q _dq while often departing from a unit of basic value _{d, m}modified value,

for machined parameters T _dq while often departing from a unit of basic value _{d, m}modified value, Q _mthe character that means secondary discharging m;

Processing scheme e comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme;

Described Q _l

q _dmin, Q _dmax, W _{d, m},

${\mathrm{\ΔW}}_{T_d,d,m},$ Q _d，m $Q_m^{p-1},{\mathrm{\ΔQ}}_{Q_d,d,m}$ And ${\mathrm{\ΔQ}}_{T_d,d,m}$ All to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{l, d}, Q _d, F _d, F _{m, e},

Δ Q _d, Δ T _d, and Q _m.

11. system according to claim 10, is characterized in that,

Described control parameter generating apparatus, simulate the time processing that described crude(oil)unit is corresponding and adopt following formula to carry out:

$\frac{\underset{i}{\mathrm{\Σ}}{F}_{i,b}\×Q_i}{\underset{i}{\mathrm{\Σ}}{F}_{i,b}}=Q_b,$

Q _bmin≤Q _b≤Q _bmax，

$\underset{c}{\mathrm{\Σ}}{F}_{u,c}=\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+({\mathrm{INV}}_u^{p-1}-{\mathrm{INV}}_u^p),$

$\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}\×Q_{i,b,u}+{\mathrm{INV}}_u^{p-1}\×Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{F}_{i,b}\×W_{i,b,u}+{\mathrm{INV}}_u^{p-1})}=Q_u,$

$C_{\mathrm{ATM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}\≤C_{\mathrm{ATM},\mathrm{TR}\max },$

$C_{\mathrm{VTM},\mathrm{TR}\min }\≤\underset{b\∈\mathrm{TRB}}{\mathrm{\Σ}}\underset{i}{\mathrm{\Σ}}{F}_{i,b}*V_{i,b}\≤C_{\mathrm{VTM},\mathrm{TR}\max ,}$

Wherein, Q _ithe property value of crude oil i, F _{i, b}the consumption of crude oil i in distillation processing scheme b, Q _bthe property value of all crude oil mixing rear feedings under distillation processing scheme b, Q _bminthat under distillation processing scheme b, feed properties allows the minimum value reached, Q _bmaxthat under distillation processing scheme b, feed properties allows the maximal value reached;

W _{i, b, u}the yield of crude oil i at the distillation discharging u of distillation processing scheme b, F _{u, c}the consumption of distillation discharging u in the Downstream processing scheme c of distillation processing scheme b,

that distillation discharging u is producing initial tank farm stock,

the tank farm stock of distillation discharging u when producing end;

Q _{i, b, u}the property value of crude oil i at the distillation discharging u of distillation processing scheme b,

the initial stock's of distillation discharging u property value, Q _uit is the property value of distillation discharging u;

TR is crude(oil)unit, and ATM is the atmospheric tower in crude(oil)unit, and TRB is the set of the corresponding processing scheme of crude(oil)unit, C _{aTM, TRmin}the least commitment value of atmospheric tower machining load in TR, C _{aTM, TRmax}it is the maximum constrained value of atmospheric tower machining load in TR;

VTM is the vacuum distillation tower in crude(oil)unit TR, V _{i, b}that crude oil i produces the yield of long residuum, C under distillation processing scheme b _{vTM, TRmin}the least commitment value of vacuum distillation tower machining load in TR, C _{vTM, TRmax}it is the maximum constrained value of vacuum distillation tower machining load in TR;

Processing scheme c comprises: secondary processing scheme d, reconciliation scheme o and shipment scheme.

Described Q _i, Q _bmin, Q _bmax, W _{i, b, u},

q _{i, b, u},

c _{aTM, TRmin}, C _{aTM, TRmax}c _{vTM, TRmin}c _{vTM, TRmax}and V _{i, b}all to gather or receive the at the appointed time manufacturing parameter of interior processing of refinery;

Comprise F by the above-mentioned control parameter calculated _{i, b}, Q _b, F _{u, c},

and Q _u.

12. system according to claim 11, is characterized in that, described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter.

13. system according to claim 12, is characterized in that, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, and the property value Q of described distillation discharging u _uinitial value Q _u0by following formula, solve:

$Q_{u0}=\frac{\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u\×Q_{i,b,u}}+Q_u^{p-1}}{(\underset{i}{\mathrm{\Σ}}\underset{b}{\mathrm{\Σ}}{W}_{i,b,u}+1)};$

Q _uspan be $[\min \left(Q_{i,b,u,}{Q}_u^{p-1}\right),\max \left(Q_{i,b,u,}{Q}_u^{p-1}\right)].$

14. system according to claim 13, is characterized in that, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, and the character Q of secondary discharging m _minitial value Q _m0by following formula, solve:

$Q_{m0}=\frac{\underset{d}{\mathrm{\Σ}}{W}_{d,m}\×Q_{d,m}+Q_m^{p-1}}{\underset{d}{\mathrm{\Σ}}{W}_{d,m}+1}$

Q _mscope be $[\min \left(Q_{d,m,}{Q}_m^{p-1}\right),\max \left(Q_{d,m,}{Q}_m^{p-1}\right)].$

15. according to claim 12,13 or 14 described systems, it is characterized in that, when described control parameter generating apparatus adopts the distribution recursive algorithm to solve described control parameter, for each carries out the material statistics whereabouts number dd of character recursive calculation, there is the processing scheme that amount of restraint is 0 in described whereabouts number dd eliminating, and for the processing scheme that does not exist amount of restraint to be 0, the initial value of error distribution coefficient is 1/dd, for the processing scheme that exists amount of restraint to be 0, the initial value of error distribution coefficient is 0.

16. according to claim 12,13 or 14 described systems, it is characterized in that, described control parameter generating apparatus specifically in order to:

Whether the fluctuation that judges in the fixed time manufacturing parameter that gathers or receive is greater than threshold value,

If be greater than, according to time sequencing, the described fixed time be divided into at least two time quantums, then calculate out described control parameter according to the manufacturing parameter in each time quantum;

Wherein, when carrying out the division of time quantum, make the fluctuation of manufacturing parameters all in each time quantum be not more than threshold value; And have at least the fluctuation of a manufacturing parameter to be greater than threshold value in two adjacent time quantums.

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