CN1167808A - Method for real-time optimization control of cracking reaction depth in catalytic cracker - Google Patents

Method for real-time optimization control of cracking reaction depth in catalytic cracker Download PDF

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CN1167808A
CN1167808A CN 97100141 CN97100141A CN1167808A CN 1167808 A CN1167808 A CN 1167808A CN 97100141 CN97100141 CN 97100141 CN 97100141 A CN97100141 A CN 97100141A CN 1167808 A CN1167808 A CN 1167808A
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reaction
productive rate
flow
optimizing
product
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CN1063214C (en
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袁璞
孙德祥
左信
黄文伟
林洪泉
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China University of Petroleum Beijing
Sinopec Maoming Co
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China University of Petroleum Beijing
Sinopec Maoming Co
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Abstract

An in-line real-time optimized control method of cracking reaction deepth for catalytic cracker of petroleum features that really measured variables are compensated by dynamically accumulated quantity: for liquid product, the really measured flow is corrected by the changes in liquid levels in stripper and oil-gas separator and in accumulated quantity in main fractionating tower; for gas product, really measured flow is corrected by the accumulated gas quantity in towers and oil-gas separator; and considering that the time delay of raw material flow relative to really measured flow can affect the yield of product, the yield at end of period is corrected by the change rate in yield at the begining of each period.

Description

The method for real-time optimization control of cracking reaction depth in catalytic cracker
The present invention relates to oil catalytic cracking unit cracking reaction degree of depth online in real time optimizing and controlling method, belong to production process control and optimization field.
Prior art is all utilized mathematics model of stable state, and the tight rate of each product in prediction (calculating) reaction product is carried out optimizing to the optimization aim based on productive rate, is main tuning means to change temperature of reaction; As: the BDL model of China (Petroleum Chemical Engineering Institute, Daqing Petroleum Institute, Lanzhou oil-refining chemical head factory), 13 lumped models (Luoyang Petrochemical engineering corporation); Abroad have: the FCC-ONONPT of Profimatic Inc, the RTOPT of SETPIONTInc, the MPFCC of Maxprofit, [DMO] of DMC Corp etc.
The prior art weak point is: just can carry out after must waiting for stable production process based on the calculating of steady-state model, make the optimizing cycle longer, be generally 2-8 hour, be difficult to adapt to the production process that often is in dynamic change; Model Calculation desired raw material character laboratory analysis of data and activity of such catalysts data also are difficult to measure in real time; Optimization aim usually is to improve about 1% productive rate, because the precision of the process variable of the used actual measurement of calculating and model is limited, is difficult to realize optimizing accurately; Adopting temperature of reaction is the tuning means, because reaction depth also is subjected to a lot of other factor affecting except that temperature, keeps the temperature of reaction that optimizing provides, and can not keep the cracking reaction degree of depth optimized, is difficult to adapt to produce and the variation of site environment.Therefore, these methods can be played a role for offline optimization, but seldom see the example of real-time application success.
The objective of the invention is, at prior art application number 90108193.0 (CN1060490A), provide a kind of feedstock property and catalyst activity data of not needing on the basis of application number 95101183.9, do not require the metrical instrument absolutely accurate, the optimizing cycle can foreshorten to 10 minutes, can adapt to the method for real-time optimization control of dynamic change.
The technical scheme that adopted of achieving the above object is as follows:
The method for real-time optimization control of cracking reaction depth in catalytic cracker:
A) according to feed rate, feeding temperature, temperature of reaction, catalyst temperature and internal circulating load, the unit's of calculating charging institute's heat requirement (reaction heat) in reaction process represents reaction depth, is up to optimization aim with target productive rate or economic benefit, adjusts reaction heat and realizes optimal control;
B) actual measurement main fractionating tower top catch pot outlet rich gas flow, raw gasline flow, diesel oil go out the device flow, efflux the slurry oil flow; It is characterized in that,
C) in the line computation reaction product, during various product productive rate, the actual measurement variable is added dynamic amount of savings compensation with above-mentioned each flow;
C1) for liquid product, take into account the stripping tower liquid level, the savings quantitative changeization is revised above-mentioned measured discharge in catch pot liquid level and the main fractionating tower;
C2) taking into account in tower and the catch pot gas amount of savings for gas products changes above-mentioned actual measurement gas flow is revised;
C3) determine that with temperature, pressure, the flow (internal reflux that comprises tower) of actual measurement separation column main fractionating tower distillates the actual boiling spread of oil product (doing and initial boiling point), revises the flow of product by the normal boiling point scope of oil product;
C4) take into account material flow and arrive the productive rate of the time lag of above-mentioned measured discharge by above-mentioned revised flow rate calculation product;
D) judge next cycle tuning direction with the mean value increase and decrease (change direction) of productive rate in adjacent two cycles and the change direction of reaction depth, consider pure retardation time and the dynamic relationship of productive rate to the reaction depth response, the rate of change of productive rate is revised the productive rate in the end of term in week when beginning with each cycle.
The present invention relates to the problem of following three aspects:
One, optimization aim determines in real time
Characteristics of the present invention are: with the separation column distilled gas of actual measurement, liquid hydrocarbon (rich gas), gasoline, diesel oil, effluxing slurry oil is foundation, utilize separation column, cold exchange device, the dynamic mathematical models of container and revivifier, the productive rate of corresponding product in line computation reaction product (main fractionating tower ingress), as the basis of determining optimization aim (the target product productive rate is the highest or economic benefit is the highest), avoid a series of problems (need feedstock property and catalyst activity data, model accuracy is not enough etc.) of bringing with the steady-state model predict yield.
The present invention during various product productive rate, has following characteristics in the line computation reaction product:
1, the actual measurement variable being added dynamic savings is compensation, and liquid product is comprised: liquid level change causes that amount of savings changes at the bottom of main fractionating tower and the catch pot, generally can calculate by following differential equation: AdH / dt = Q 1 L - Q 2 L
Or by following time discretization Equation for Calculating: Q 1 L ( k ) = [ H ( k + 1 ) - H ( k ) ] A / T S + Q 2 L ( k )
Wherein:
The H-liquid level
The A-container section is long-pending
The t-time
Q 1 LThe flow (normally to be calculated) of-inflow container
Q 2 LThe flow of-flow container (normally can survey)
T S-computation period
For the variation of gas amount of savings in the gas products consideration tower, calculate with following differential equation: C v dp / dt = Q 1 v - Q 2 v
Or by following time discretization Equation for Calculating: Q 1 v ( k ) = [ P ( k + 1 ) - P ( k ) ] C v / T S = Q 2 v . ( k )
Wherein:
C v-tower air-capacitor amount;
The atmospheric pressure of P-tower;
Q 1 v, Q 2 v-be respectively inflow, go out the flow of tower
2, the correction of oil product boiling spread
Determine that with observed temperature, pressure, flow (internal reflux that comprises tower) separation column distillates the actual boiling spread of oil product (doing and initial boiling point), the flow of product revised, adopt following method (seeing 95101183.9) by the normal boiling point scope of oil product: Q s = Q 1 [ 1 + K i ( T i - T i s ) + k e ( T e s - T e ) ]
T i s, T e s-be respectively oil product the standard initial boiling point and do
T i, T e-be respectively oil product actual initial boiling point and do
Q 1Flow before the-correction
Q s-revised flow
3, introduce the former time lag of expecting above-mentioned measured discharge, be calculated as follows productive rate:
Y i＝Q si/Q o(t-τ i)
Wherein: Y iIt is the productive rate of i product
Q oBe the stock oil flow
Q SiBe flow through compensation and revised i product
τ iIt is the time lag of i flow to raw material
Two, dynamic self-optimization method, its characteristics are:
1, judges next cycle tuning direction with the mean value increase and decrease (change direction) of productive rate in adjacent two cycles and the change direction of reaction depth, do not require that metrical instrument is absolutely correct.
2, introduce dynamically correction and time lag, judge when productive rate changes, consider pure retardation time and the dynamic relationship of productive rate to the reaction depth response, the rate of change of productive rate is revised the productive rate in all end of term when beginning with each cycle, and method is as follows: Y i c ( K ) = Y i ( K ) + β [ Y i ( k - n + 1 ) - Y i ( k - n ) ]
Y i c(K)-dynamic revised productive rate
Y i(K)-end of term in week productive rate constantly before revising
Y i(k-n)-productive rate when the cycle begins
Y i(k-n+1)-cycle begins the productive rate of a back computation period
β-correction factor
3, stop voluntarily and start automatically
At any time measure productive rate and continuous tuning number of times, when productive rate changes not quite, or when the tuning number of times reached regulation numerical value continuously, optimizing stopped voluntarily, keeps steady running.
At any time measure productive rate, reaction depth and recycle ratio when feedstock property (containing recycle ratio), productive rate or reaction depth change when excessive, optimizing stops; Steadily,, start optimizing voluntarily at certain hour through timer control.
4, not super constraint
The variation of liquid level, pneumatic press and main air blower load (main air flow) at the bottom of forecast reaction depth, temperature of reaction, reaction pressure, regeneration temperature, regeneration oxygen level, freshening oil tank level and the tower, when it will transfinite, reaction depth can only be towards the direction adjustment of not transfiniting.
5, has sfgd.
When measuring point has fault, when calculation of yield was unreasonable or contradictory, optimizing can stop automatically, and showed error message.
Three, optimizing result execution, its characteristics are:
1, the reaction heat that is used in line computation is weighed and control reaction depth (existing patent application 90108193.0).
2, be main tuning means to change reaction heat, have the bound protection.
When 3, adjusting reaction heat, temperature of reaction, preheating temperature, regeneration guiding valve aperture and pressure drop are not transfinited.
4, have sfgd.: when above-mentioned reaction heat calculates and reaction depth Controlling System when breaking down, but the optimizing automatic opening.
In conjunction with the accompanying drawings the present invention is described in further detail below by embodiment.
Fig. 1 is a catalytic cracking unit part synoptic diagram;
Fig. 2 is the cracking reaction degree of depth method for real-time optimization control embodiment that the present invention realizes with DCS (Distributed Computer System);
Fig. 3 is the block diagram that reaction product calculation of yield observer calculates the product productive rate;
Fig. 4 is the tuning block diagram of reaction depth real-time optimization device;
Fig. 1 is a catalytic cracking unit part synoptic diagram, stock oil 11 is through pipeline 12 input riser reactors 13, catalyzer 14 is heated to 700 ℃ through pipeline 15 input riser reactors 13, reaction product is through settling vessel 16 and pipeline 17 input main fractionating towers 18, the rich gas outlet 20 of main fractionating tower 18 top catch pots 19 and raw gasline outlet 21, the diesel oil outlet 23,24 of stripping tower 22 is for effluxing the slurry oil mouth.25 is reflux line.Revivifier and pneumatic press are not shown in Fig. 1, and the textbook in the relevant petroleum catalytic cracking technical field of its principle of work all has argumentation.This synoptic diagram is just done simple declaration in order better to understand method for real-time optimization control of the present invention.
The present invention can realize on the catalytic cracking unit with production process control computer; Can go up at DCS (Distributed Computer System) and realize, can realize on the host computer of DCS that also Fig. 2 is the embodiment on DCS, comprise following content:
(1) data gathering and processing
(2) conventional controller and variable valve and guiding valve
(3) the online calculating observation device of reaction heat
(above is prior art, shows with empty frame table)
(4) the reaction depth multivariate is coordinated predictor controller
(5) reaction product calculation of yield observer
(6) reaction depth real-time optimization device
(7) setting apparatus
(above is relevant technologies of the present invention, shows with real frame table)
(4) the reaction depth multivariate is coordinated predictor controller
This controller utilizes the existing technology of weighing the control of the reaction depth realization response degree of depth with reaction heat; Application number 90108193.0, publication number 1060490A, characteristics of the present invention:
(a) in control reaction heat, take into account temperature of reaction and do not fluctuate excessively, do not transfinite, for this is provided with unsteady bound to temperature of reaction, the central value of the bound of floating is that the reaction heat that comes into operation is controlled temperature of reaction into or set by the operator.Press the weighted deviation of reaction heat and temperature of reaction, adjust given control of popular response temperature regulator by the model pre-estimating control algolithm.
Weighted deviation E=qE t+ (1-q) E h
E tBe the deviation of temperature of reaction with the limit central value of floating
E hFor the deviation of reaction heat and its set-point is worked as | E t|＜δ 1Q=0 (only reaction heat being controlled) δ 1L B≤ | E t|≤100%L BQ=(| E t|-δ 1L B)/(1-δ 1) L B(coordination) | E t|＞100%L BQ=1 (only temperature of reaction being controlled)
(b) if conditions permit when Et is non-vanishing, can be adjusted raw material preheating temperature, end agent flux or regenerated catalyst temperature, make the deviation of temperature of reaction and floating neutral limit less.
(c) adopting multicycle control is T to the control cycle of reaction heat 1Control cycle to temperature of reaction is T 2Control cycle to preheating temperature is T 3
The general T that selects 1＜T 2＜T 3
(d) guiding valve pressure drop, valve position, the not super constraint of variablees such as reaction pressure
(5) reaction product calculation of yield observer
This observer by actual measurement main fractionating tower outlet rich gas, gasoline, diesel oil, efflux slurry oil (clarified oil) flow with corresponding product productive rate in the following method calculating reaction product; By actual measurement regenerator temperature, main air flow; Catalyst inventory and oxygen content of smoke gas calculate the coke productive rate.See Fig. 3.
Dynamic compensation:
(a) catch pot, liquid level change is to the correction of flow at the bottom of stripping tower and the main fractionating tower;
(b) correction of savings quantitative changeization in the main fractionating tower
(each section of the separation column internal reflux flow that utilizes the existing online calculating observation device of petroleum products boiling range to provide compensates)
(c) compensation that changes of the gas amount of savings that causes of pressure change
(d) calculate (product) the burnt amount of burning by revivifier oxygen level and dynamic mathematical models
The correction of petroleum products boiling spread:
(a) the standard boiling range of gasoline is pressed 30-205 ℃ of calculating; If at the Gep that does of line computation, then gasoline and diesel oil (be respectively+,-) correction is during actual motion:
Δ F g=a g(205-G Ep) a gBe adjustable correction factor
(b) actual measurement catch pot pressure P g, temperature T gGasoline and rich gas (be respectively (+,-) are revised, and correction is: F w=a Wt(z-T g)-a Wp(P g-P G0) P G0Be rated pressure
(c) by at line computation diesel oil 90% point (D 90) diesel oil is revised F d=a d(D 90 0-D 90) D 90Be 90% compensation time lag of standard diesel oil
Calculate rich gas, gasoline, diesel oil, coke, efflux the pure retardation time of slurry oil (clarified oil) by model and measured data, revised when calculating productive rate the stock oil fluctuations in discharge.
(6) reaction depth real-time optimization device and (7) setting apparatus
This optimizer is according to the optimization aim of setting, the online calculating observation value of calculation of yield result and reaction heat, (be called the optimizing cycle) at regular intervals and adjust reaction depth (heat) once given, as the tuning means.Its step is as follows: see Fig. 4
The calculation of yield product test
(a) fluctuating range of the yield value of operating mode and calculating can not exceed rational set(ting)value;
(b) the productive rate pace of change does not exceed set(ting)value;
(c) (gasoline+diesel oil+rich gas+coke+efflux) productive rate and 100% deviation are less than set(ting)value;
(d) deviation of (gasoline+diesel oil+rich gas) productive rate and (100%-effluxes-coke) is less than set(ting)value.
When not satisfying above-mentioned condition, provide the defective signal of calculation of yield
Optimizing is calculated
(a) when calculation of yield is qualified, by the calculation of yield optimization target values;
(b) relatively the object variations (Δ J) in two optimizing cycles and reaction heat change (Δ H), determine the tuning direction by following logic:
If the two change direction is identical, then increase reaction depth;
If the two change direction is inequality, then reduce reaction depth.
As Δ J and Δ H during, just think to change greater than set(ting)value;
As Δ J with Δ H is little, during in set(ting)value, think to stop tuning by no change;
(c) in the calculating of Δ J, add dynamic compensation, promptly calculate the rate of change R of each optimizing cycle target when beginning 1Adding-rR 1Modified value, wherein r is an adjustable parameter.
Constraint is handled
Whether transfinite with model pre-estimating temperature of reaction, reaction pressure, regeneration temperature, regenerated flue gas oxygen level, pneumatic press load, freshening oil tank level etc.If transfinite, the tuning direction can only be adjusted towards the constraint relief direction.
The optimizing start-stop is judged
(a) reach set(ting)value less than set(ting)value or optimizing cycle life when object variations, stop optimizing.
(b) change greater than set(ting)value when recycle ratio (intermingled dregs ratio), or productive rate and reaction heat calculation result stop optimizing when defective; In case recycle ratio (intermingled dregs ratio) does not change, or calculated value recovers normal, or reaction heat no change and productive rate can start optimizing voluntarily through all after dates of two optimizing when changing greatly.
(c) stop time that optimizing reaching after, start optimizing voluntarily.
(d) be provided with the manual manual operation switch, can start or stop optimizing at any time.
(e) come into operation for the first time after the real-time optimizing system, start optimizing voluntarily.

Claims (8)

1, the method for real-time optimization control of cracking reaction depth in catalytic cracker:
A) according to feed rate, feeding temperature, temperature of reaction, catalyst temperature and internal circulating load, the unit's of calculating charging institute's heat requirement (reaction heat) in reaction process represents reaction depth, is up to optimization aim with target productive rate or economic benefit, adjusts reaction heat and realizes optimal control;
B) actual measurement main fractionating tower top catch pot outlet rich gas flow, raw gasline flow, diesel oil go out the device flow, efflux the slurry oil flow; It is characterized in that,
C) in the line computation reaction product, during various product productive rate, the actual measurement variable is added dynamic amount of savings compensation with above-mentioned each flow;
C1) for liquid product, take into account the stripping tower liquid level, the savings quantitative changeization is revised above-mentioned measured discharge in catch pot liquid level and the main fractionating tower;
C2) taking into account in tower and the catch pot gas amount of savings for gas products changes above-mentioned actual measurement gas flow is revised;
C3) determine that with temperature, pressure, the flow (internal reflux that comprises tower) of actual measurement separation column main fractionating tower distillates the actual boiling spread of oil product (doing and initial boiling point), revises the flow of product by the normal boiling point scope of oil product;
C4) take into account material flow and arrive the productive rate of the time lag of above-mentioned measured discharge by above-mentioned revised flow rate calculation product;
D) judge next cycle tuning direction with the mean value increase and decrease (change direction) of productive rate in adjacent two cycles and the change direction of reaction depth, consider pure retardation time and the dynamic relationship of productive rate to the reaction depth response, the rate of change of productive rate is revised the productive rate in the end of term in week when beginning with each cycle.
2, method according to claim 1 is characterized in that, when the productive rate variation was not more than prescribed value, optimizing stopped voluntarily, kept steady running.
3, method according to claim 1 is characterized in that, when continuous tuning number of times reached regulation numerical value, optimizing stopped voluntarily, keeps steady running.
4, method according to claim 1 is characterized in that, when recycle ratio, productive rate or reaction depth change greater than prescribed value, suspends optimizing, starts optimizing voluntarily after steadily.
5, method according to claim 1 is characterized in that, measuring point has fault, and calculation of yield is unreasonable, and optimizing stops automatically, and shows error message.
6, method according to claim 1 is characterized in that, after optimizing stops, through timer control, starts optimizing voluntarily behind certain hour.
7, method according to claim 1, it is characterized in that, liquid level, separation column and pneumatic press load transfinite at the bottom of regeneration temperature, oxygen level, main air amount, reaction pressure, freshening oil tank level, main fractionating tower, adjust the reaction heat set-point, make its constraint relief.
8, method according to claim 1 is characterized in that, by adjusting the reaction heat set-point, realize optimizing, and make temperature of reaction, and raw material preheating temperature, regeneration guiding valve (26) aperture and pressure drop are not transfinited.
CN97100141A 1997-01-09 1997-01-09 Method for real-time optimization control of cracking reaction depth in catalytic cracker Expired - Fee Related CN1063214C (en)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1619447B (en) * 2003-07-30 2010-09-29 费舍-柔斯芒特系统股份有限公司 Economic calculation in process control system
CN101859103A (en) * 2010-06-02 2010-10-13 清华大学 On-line calculation and self-adaptation nonlinear prediction control method of catalytic cracking reaction depth
CN108398965A (en) * 2017-02-07 2018-08-14 何巨堂 Erosion material dual or multi runner control system serial combination depressurizing system and reducing transformer
CN113176767A (en) * 2021-04-30 2021-07-27 北京瑞飞华亿科技有限公司 Propylene recovery control system

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1060490A (en) * 1990-10-12 1992-04-22 中国石油化工总公司 The observation of catalytic cracking reaction depth and control method
CN1050150C (en) * 1995-01-19 2000-03-08 中国石油化工总公司 In-line determining method for quality index of gasoline and diesel oil
CN1054928C (en) * 1995-09-21 2000-07-26 厦门大学 Optimization control system for catalytic cracking plant

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1619447B (en) * 2003-07-30 2010-09-29 费舍-柔斯芒特系统股份有限公司 Economic calculation in process control system
CN101937224B (en) * 2003-07-30 2013-03-13 费舍-柔斯芒特系统股份有限公司 Method used in process plant
CN101937225B (en) * 2003-07-30 2014-09-03 费舍-柔斯芒特系统股份有限公司 System used for process plant having controller connected with a plurality of field devices
CN101859103A (en) * 2010-06-02 2010-10-13 清华大学 On-line calculation and self-adaptation nonlinear prediction control method of catalytic cracking reaction depth
CN108398965A (en) * 2017-02-07 2018-08-14 何巨堂 Erosion material dual or multi runner control system serial combination depressurizing system and reducing transformer
CN113176767A (en) * 2021-04-30 2021-07-27 北京瑞飞华亿科技有限公司 Propylene recovery control system

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