CN103365208A - Crude oil blending optimization method with deviation correction function of base oil property - Google Patents
Crude oil blending optimization method with deviation correction function of base oil property Download PDFInfo
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- CN103365208A CN103365208A CN2013102927296A CN201310292729A CN103365208A CN 103365208 A CN103365208 A CN 103365208A CN 2013102927296 A CN2013102927296 A CN 2013102927296A CN 201310292729 A CN201310292729 A CN 201310292729A CN 103365208 A CN103365208 A CN 103365208A
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Abstract
Disclosed is a crude oil blending optimization method with the deviation correction function of a base oil property. The method is about a crude oil blending production process and comprises the steps that component oil in component tanks is blended at blending ends, passes through a buffer tank filled with base oil and is fed into an atmospheric and vacuum plant to be processed. Blending is carried out aiming at base oil property deviation correction and lowest blending cost, the problem of deviation compensation of the buffer-tank base oil property when crude oil is blended is solved, crude oil meeting the processing requirement is provided for a CDU, damage to the CDU and subsequent processing devices by the property deviation of the crude oil is avoided, product quality is ensured, and economic benefits of enterprises are improved.
Description
Technical field
The present invention relates to oil refining enterprise crude oil manufacture field, specifically a kind of crude oil concoction optimization method with end oil nature correction.
Background technology
Current, the on-line automatic blending technology of crude oil has begun at home the application of succeeding of a plurality of refineries.Line blending is often adopted in the on-line automatic blending of crude oil, and namely directly sending into atmospheric and vacuum distillation unit after the blending in the line blending head is that CDU processes.But also there is such a case in Some Enterprises, and namely each component oil in the blending of blending head, is sent into CDU through surge tank again and processed first.
Existing crude oil is concocted online optimizing methods, often for be a blending product but not product in the tank.When bottomless when oil in the surge tank, control the character of a blending product well, just equal to control well the character of surge tank product.And when having the end oily in the surge tank, only control well and concoct a product property, can't solve the end oil nature initial deviation problem in the storage tank, cause oil property and the realistic objective of sending into final CDU to have deviation, and then affect crude oil blending productivity effect.
Summary of the invention
The present invention is directed to the bottom of storage tank oil nature offset issue that exists in the blending of Petrochemical Enterprises crude oil, a kind of crude oil concoction optimization method with end oil nature drift correction has been proposed, under the prerequisite that satisfies apparatus and process constraint condition, minimum with the oil property content deviation, taking into account simultaneously economic optimum is that target is optimized, obtain optimum blending prescription, when guaranteeing product quality, improve Business Economic Benefit.
Technical scheme of the present invention:
A kind of crude oil concoction optimization method with end oil nature drift correction, the method is concocted at the blending head first for the component oil in each component tank, send into the crude oil blending production run that atmospheric and vacuum distillation unit is processed through the surge tank that end oil is housed again, the method may further comprise the steps:
Steps A: be N blending cycle with whole blending Process Decomposition, calculate each blending cycle finish after the blending desired value of oil property data in the surge tank;
Step B: a new blending cycle is when beginning, oil property data in the current surge tank are as initial value, oil property data deviation when finishing take this blending cycle in the surge tank and blending cost minimization are as target, set up objective function and constraint condition, find the solution each the component oil accounting that obtains this blending cycle, i.e. the blending prescription;
Step C: will concoct prescription and send the bottom control system to carry out, the crude oil after the blending head is concocted is sent into surge tank, keeps the blending prescription constant until should concoct end cycle;
Step D: return step B, under new initial value and blending desired value, continue to find the solution objective function, obtain new blending prescription and execution, move in circles until carry out N blending cycle whole blending process end.
Steps A adopt following formula calculate each blending cycle finish after the blending desired value of oil property data in the surge tank:
In the following formula, p
kBe the blending desired value of the oil property data in the surge tank after finishing in k blending cycle, k=1,2...N, N are total number of cycles of whole blending process need; p
fFinish the final goal value of rear surge tank Crude Oil character data for whole blending process; p
0Begin the initial value of end oil nature data in the front surge tank for whole blending process; V
fFinish the total amount of rear surge tank Crude Oil for whole blending process; V
0Begin the total amount of end oil in the front surge tank for whole blending process; V
kIt is the total amount of surge tank Crude Oil when finishing in k blending cycle.
Objective function described in the step B and constraint condition are following formula:
w
kX
k≤t
kB
tB≤U
In the formula, Ψ (X
k) be the objective function in k blending cycle, k=1,2...N, N are total number of cycles of whole blending process need; N represents the component oil number that participates in concocting; X
kBe the component oil accounting in k blending cycle, X
k=[x
K1, x
K2X
Kn]
T, X
k〉=0, x
KiRepresent the accounting of i kind component oil in k blending cycle; λ is the weight of oil property, λ 〉=0; a
iIt is the character data of i kind component oil; d
kBe to begin the front actual surge tank Crude Oil character data that records, d k blending cycle
k〉=0; p
kBe the blending desired value of the oil property data in the surge tank after finishing in k blending cycle, p
k〉=0; c
iBe the procurement price of i kind component oil, c
i〉=0; w
kBe the blending amount in k blending cycle, w
k〉=0; t
kBe the expected time in k blending cycle, t
k〉=0; T is the expected time of whole blending process, t 〉=0; B is that the Oil Blending pipeline is the Peak Flow Rate of component oil, B=[b
1, b
2B
n]
T, B 〉=0, b
iThe Peak Flow Rate that represents i kind component oil; U for mix the component tank that is connected of refining line the total amount of component oil, U=[u can be provided
1, u
2U
n]
T, U 〉=0, u
iThe component tank that i kind component oil is equipped with in expression can provide the total amount of component oil.
Beneficial effect of the present invention:
The present invention has realized a kind of crude oil concoction optimization method with end oil nature drift correction, oil nature deviation compensation problem at the bottom of the surge tank that has existed when having solved the crude oil blending, the crude oil that satisfies processing request is provided for CDU, the infringement of having avoided the oil property deviation to bring to CDU and following process device, guarantee product quality, and improved Business Economic Benefit.
Description of drawings
Fig. 1 has the crude oil blending procedure structure schematic diagram of surge tank.
Fig. 2 has the crude oil mixing process figure of surge tank.
Embodiment
The invention will be further described below in conjunction with drawings and Examples.
The below in the actual performance of certain Petrochemical Enterprises and in conjunction with a concrete example, provides detailed computation process and concrete operating process with the present invention.
As shown in Figure 1, there are 3 oil component tanks in this enterprise, 3 Oil Blending lines, and every Oil Blending line uses a blending component tank.Adopt the blending of line blending head by surge tank, send at last CDU processing.Blending is by batch carrying out, and every batch of total amount that blending is certain is carried out the next batch blending again after this batch blending is finished.The present embodiment is implemented under take technical solution of the present invention as prerequisite, but protection scope of the present invention is not limited to following embodiment.
Suppose this batch blending total amount w=10000t, end oil total amount V in the surge tank
0=2000t estimates total execution time t=16h.1# mixes refining line Peak Flow Rate b
1=400t/h; 2# mixes refining line Peak Flow Rate b
2=500t/h; 3# mixes refining line Peak Flow Rate b
3=600t/h, then B=[400 500 600]
T
1# component tank controlled variable u
1=4000t; 2# component tank controlled variable u
2=8000t; 3# component tank controlled variable u
3=5000t, then U=[4000 8,000 5000]
T
Take the character index of naphtha yield as example, requiring naphtha yield after whole blending process finishes is 24%.Current 1# component oil naphtha yield 14.97%, 80.8 dollars/barrel of costs; 2# component oil naphtha yield 28.2%, 85.7 dollars/barrel of costs; 3# component oil naphtha yield 32.49%, 92.3 dollars/barrel of costs; The end oilstone cerebrol yield of surge tank is 16%.
Suppose each cycle blending amount w
k=1000t has 8 blending cycles, and each concocts expected time in cycle t
k=2h.
As shown in Figure 2, crude oil blending process mainly may further comprise the steps:
At first adopt following formula calculate each blending cycle finish after crude oil naphtha yield desired value;
V=[v in the formula
1, v
2V
8]=[3000,4000 ... 1000,0p
f=24%, p
0=16%, V
f=10000, V
0=2000.Try to achieve p
k=[17% 18% 19% 20% 21% 22% 23% 24%].
Then objective function is optimized, obtains the optimization of C/C composites in each blending cycle;
Objective function:
Constraint condition:
w
kX
k≤t
kB
tB≤U
Wherein, a
1=14.97%, a
2=28.2%, a
3=32.49%; c
1=80.8, c
2=85.7, c
3=92.3, λ is constant, gets 2 * 10
5p
kBe the blending desired value of the oil property data in the surge tank after finishing in k blending cycle, p
k=[17% 18% 19% 20% 21% 22% 23% 24%.] X
kBe the component oil accounting in k blending cycle, X
k=[x
K1, x
K2X
Kn]
T, X
k〉=0, x
KiRepresent the accounting of i kind component oil in k blending cycle.w
kBe the blending amount in k blending cycle, w
k=1000t.t
kBe the expected time in k blending cycle, t
k=2h; T is the expected time of whole blending process, t=16h.B is that the Oil Blending pipeline is the Peak Flow Rate of component oil, and B=[400 500 600]
Tb
iThe Peak Flow Rate that represents i kind component oil, b
1=400t/h, b
2=500t/h, b
3=600t/h.U for mix the component tank that is connected of refining line the total amount of component oil can be provided, U=[4000 8,000 5000]
T, U 〉=0; u
iThe component tank that i kind component oil is equipped with in expression can provide the total amount of component oil, u
1=4000t, u
2=8000t, u
3=5000t.
d
kBe to begin the front actual surge tank Crude Oil character data that records, d k blending cycle
1=16%.
Try to achieve the blending prescription X in first blending cycle
1=[0.69 0.31 0], the blending prescription remains unchanged until first blending cycle blending is finished in this cycle.
Before second blending cycle begins, record surge tank Crude Oil naphtha yield d
2=16.97%, as new surge tank Crude Oil naphtha yield initial value, the objective function that Optimization Solution is new is tried to achieve second blending prescription X that concocts the cycle
2=[0.54 0.46 0], the blending prescription remains unchanged until second blending cycle blending finished in this cycle.
Such as above-mentioned step, when each blending end cycle, record surge tank Crude Oil naphtha yield, as the next one surge tank Crude Oil naphtha yield initial value in blending cycle, and new initial value and the blending desired value under the Optimization Solution objective function, try to achieve accordingly X
3=[0.38 0.62 0], X
4=[0.23 0.77 0], X
5=[0.07 0.93 0], X
6=[0.0 0.77 0.23], X
7=[0 0.33 0.67], X
8=[0 0.08 0.92].
Carry out according to above-mentioned steps, after blending was finished, recording surge tank Crude Oil naphtha yield was 24%, had reached expection blending target.
The invention is not restricted to revise end oilstone cerebrol yield character data, the part that the present invention does not relate to all prior art that maybe can adopt same as the prior art is realized.
Claims (3)
1. crude oil concoction optimization method with end oil nature drift correction, the method is concocted at the blending head first for the component oil in each component tank, send into the crude oil blending production run that atmospheric and vacuum distillation unit is processed through the surge tank that end oil is housed again, it is characterized in that the method may further comprise the steps:
Steps A: be N blending cycle with whole blending Process Decomposition, calculate each blending cycle finish after the blending desired value of oil property data in the surge tank;
Step B: a new blending cycle is when beginning, oil property data in the current surge tank are as initial value, oil property data deviation when finishing take this blending cycle in the surge tank and blending cost minimization are as target, set up objective function and constraint condition, find the solution each the component oil accounting that obtains this blending cycle, i.e. the blending prescription;
Step C: will concoct prescription and send the bottom control system to carry out, the crude oil after the blending head is concocted is sent into surge tank, keeps the blending prescription constant until should concoct end cycle;
Step D: return step B, under new initial value and blending desired value, continue to find the solution objective function, obtain new blending prescription and execution, move in circles until carry out N blending cycle whole blending process end.
2. a kind of crude oil concoction optimization method with end oil nature drift correction according to claim 1, it is characterized in that steps A adopt following formula calculate each blending cycle finish after the blending desired value of oil property data in the surge tank:
In the following formula, p
kBe the blending desired value of the oil property data in the surge tank after finishing in k blending cycle, k=1,2...N, N are total number of cycles of whole blending process need; p
fFinish the final goal value of rear surge tank Crude Oil character data for whole blending process; p
0Begin the initial value of end oil nature data in the front surge tank for whole blending process; V
fFinish the total amount of rear surge tank Crude Oil for whole blending process; V
0Begin the total amount of end oil in the front surge tank for whole blending process; V
kIt is the total amount of surge tank Crude Oil when finishing in k blending cycle.
3. a kind of crude oil concoction optimization method with end oil nature drift correction according to claim 1 is characterized in that the objective function described in the step B and constraint condition are following formula:
w
kX
k≤t
kB
tB≤U
In the formula, Ψ (X
k) be the objective function in k blending cycle, k=1,2...N, N are total number of cycles of whole blending process need; N represents the component oil number that participates in concocting; X
kBe the component oil accounting in k blending cycle, X
k=[x
K1, x
K2X
Kn]
T, X
k〉=0, x
KiRepresent the accounting of i kind component oil in k blending cycle; λ is the weight of oil property, λ 〉=0; a
iIt is the character data of i kind component oil; d
kBe to begin the front actual surge tank Crude Oil character data that records, d k blending cycle
k〉=0; p
kBe the blending desired value of the oil property data in the surge tank after finishing in k blending cycle, p
k〉=0; c
iBe the procurement price of i kind component oil, c
i〉=0; w
kBe the blending amount in k blending cycle, w
k〉=0; t
kBe the expected time in k blending cycle, t
k〉=0; T is the expected time of whole blending process, t 〉=0; B is that the Oil Blending pipeline is the Peak Flow Rate of component oil, B=[b
1, b
2B
n]
T, B 〉=0, b
iThe Peak Flow Rate that represents i kind component oil; U for mix the component tank that is connected of refining line the total amount of component oil, U=[u can be provided
1, u
2U
n]
T, U 〉=0, u
iThe component tank that i kind component oil is equipped with in expression can provide the total amount of component oil.
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Cited By (8)
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CN104007658A (en) * | 2014-06-13 | 2014-08-27 | 南京富岛信息工程有限公司 | Gasoline online blending method with dual-circulation optimization |
CN104267602A (en) * | 2014-09-24 | 2015-01-07 | 南京富岛信息工程有限公司 | On-line gasoline double blending head coordination and optimization method supporting multiple common components |
CN106054950A (en) * | 2016-06-07 | 2016-10-26 | 河海大学 | Crude oil blending double-closed-loop control method |
CN104007658B (en) * | 2014-06-13 | 2016-11-30 | 南京富岛信息工程有限公司 | A kind of have the gasoline online blending method that double circulation optimizes |
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CN109765788B (en) * | 2019-03-29 | 2022-03-04 | 华东理工大学 | Multi-target crude oil blending online optimization method |
CN109994160B (en) * | 2019-03-29 | 2023-08-15 | 华东理工大学 | Calculation method of blending effect parameters of crude oil blending |
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Application publication date: 20131023 |