CN1054928C - Optimization control system for catalytic cracking plant - Google Patents
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- CN1054928C CN1054928C CN95115925A CN95115925A CN1054928C CN 1054928 C CN1054928 C CN 1054928C CN 95115925 A CN95115925 A CN 95115925A CN 95115925 A CN95115925 A CN 95115925A CN 1054928 C CN1054928 C CN 1054928C
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Abstract
The present invention relates to an optimization control system for a catalytic cracking process, which comprises a device A, a device B, a device C, a device D, and a controller, wherein the device A is used for respectively outputting the reckoning values of product conversion rate and the discreet values of real-time observation according to the temperature, pressure, liquid level, flow rate, optimization target values and other parameters of a catalytic cracker, the device B is used for outputting characteristic numbers representing raw material properties, the device C is used for outputting target yield values, the device D is used for outputting the optimization values of the conversion rate, and the controller is used for determining the deviation of the device D according to measured values and set values; the devices A, B, C and D and the controller form a two-stage closed-loop optimization regulating control system which uses the conversion rate as principal regulation and control quantity, and changes the method in which a regeneration valve is used to control reaction temperature and reaction heat previously. The present invention has the advantages of high yield of boiled oil, strong anti-jamming ability, stable control performance and stable quality.
Description
The present invention relates to a kind of under the situation that does not have hydrogen, the catalytic cracking process optimal control system of hydrocarbon ils.
Catalytic cracking unit is the important device of crude oil secondary processing, and the optimal control of its technological process is the important means that further improves operant level.
The raw material of refinery catalytic cracking process is the heavy constituent in the crude oil---cured oil and vacuum residuum, under the effect of catalyzer, by cracking reaction the heavy constituent in the oil product are split into light constituent, be converted into gas, gasoline, light diesel fuel and coke, unconverted part is all sent reactor back to and is gone to participate in once more reaction (title recycle stock).Usually, catalytic cracking process mainly comprises steps such as reaction, sedimentation, regeneration, fractionation and absorption be stable.Charging is squeezed into reactor by nozzle, with gasification rapidly after the high temperature of coming (about the 700 ℃) catalyst mix from regenerator, gas entrainment catalyzer after the gasification rises along reactor (as riser), enter settler, finish the cracking reaction of heat absorption when rising, the coke that produces in the reaction is then topped at catalyst surface, and catalyzer is lost activity.Reaction oil gas is in settler and catalyst separation, and oil gas enters fractionator, and catalyzer is then gone into regenerator and burnt.Regenerator is a fluidized-bed reactor, and main air (air) is advanced in the bottom, makes catalyst fluidization, burns reaction, i.e. the topped coke on catalyst surface of burning-off under the effect of oxygen, thus recover activity of such catalysts (so claiming " regeneration ").Catalyzer after the regeneration is gone into riser reactor along pipeline through regeneration valve and is recycled, and the heat that burns generation also takes riser to by catalyzer and uses for cracking reaction.Reacted oil gas separates at fractionator, and gas and gasoline are gone out from cat head, goes into the raw gasoline jar after cooling, is separated into gas (claiming rich gas on the technology) and liquid (raw gasoline) again.To the stable absorption part, isolated light diesel fuel is then directly by extracting out in the tower through pipeline for rich gas and raw gasoline, and unconverted part (recycle stock) part flows to the freshening oil tank from 7 layers of column plate in the oil gas, and a part (forming heavier) drops on (slurry oil at the bottom of the title tower) at the bottom of the tower.Raw gasoline and rich gas finally form products such as dry gas, liquefied gas and stabilized gasoline after the stable absorption of absorbing-stabilizing system.
Existing Hydrocarbon Content by Catalytic Cracking Operation control method has regeneration valve → temperature of reaction (riser outlet temperature) to control method automatically, valve to be generated (operation valve on the catalyst line from the settler to the regenerator) → settler material level is controlled method automatically, refluxed with slurry oil extraction amount adjustment regenerator temperature method at the bottom of the tower with fractionator and control fractionator temperature method etc.And some off-line tuning systems and online micro computer monitoring or optimal control system are proposed, for example multivariable control system and simulation tuning system etc., Qin Ruiqi etc. are at " China's THE DEVELOPMENT OF COMPUTERS PROCESS CONTROL OF FCC IN " (petroleum refining and chemical industry, 1994,25 (5): summarized the characteristics of these systems 1～12), its core is that existing these catalytic cracking controls and tuning scheme are based on the control temperature of reaction.Because catalytic cracking is a course of reaction, to full device operation and product distribution influence maximum is reaction depth but in fact.Temperature of reaction is influenced by various factors, can not represent reaction depth fully, therefore is actually a kind of indirect method with the temperature tuning, and effect is also just little desirable.For addressing this problem, (petroleum refining such as Yuan Pu, 1992 (9): 23～27) propose a kind of reaction heat controlling schemes, it has changed original method for controlling reaction temperature, be that regeneration valve is no longer directly controlled temperature, but control reaction heat, concrete grammar is that each section of riser temperature and regeneration valve flow characteristics are delivered to computing machine, calculate reaction heat according to certain method, input as the regeneration valve controller, according to the output of Prediction Control algorithm computation controller, adjust the regeneration valve aperture and make reaction heat steady again.Though under the certain condition of feedstock property, reaction heat can be used as a kind of tolerance of reaction depth, because reaction heat itself is related with feedstock property, so this scheme is not suitable for the frequent device of feedstock property variation.Can not survey because of reaction heat simultaneously, also more abstract, so the enforcement difficulty of scheme is bigger.
The object of the present invention is to provide catalytic cracking unit a kind of is the closed loop tuning control system of main regulation and control amount with conversion rate of products.
Catalytic cracking unit generally includes the relevant measurement mechanism of operation valve, reaction-regeneration system, fractionating system, absorbing-stabilizing system and each system and the control system of catalytic cracking unit.The optimal control system that is a kind of catalytic cracking unit provided by the invention.
The present invention includes: according to the temperature signal of catalytic cracking unit reactive system, advance the catalyst flow measuring and calculating signal of catalytic cracking unit reactor and advance the catalytic cracking unit reactor the combined feed flow measuring-signal and export the feedstock property observation device (hereinafter to be referred as device B) of the characteristic number that characterizes catalytically cracked material character, the output terminal of the measurement mechanism of the input termination catalytic cracking unit reaction-regeneration system (feed system that comprises reactor, regenerator, reactor) of device B; Temperature according to catalyst cracker, pressure and be arranged on regenerator to the flow measuring-signal of operation valve (hereinafter to be referred as the regeneration valve) valve position on the pipeline of the catalyzer of reactor, advance the measuring-signal of the fresh feed flow of reactor, the catalytic cracking unit fractionating system (comprises fractionator, recycle stock accumulates and withdrawing device, raw gasoline jar and diesel oil air-lift device) flow, the feedstock property characteristic number of level gauging signal and device B output and export the conversion rate of products observation estimating device (hereinafter to be referred as device A) of the real-time monitored discreet value of the measuring and calculating value of catalytic cracking reaction conversion rate of products (hereinafter to be referred as conversion rate of products) and conversion rate of products, the input end of device A connects catalytic cracking unit reaction-regeneration system measurement mechanism output terminal respectively, the output terminal of the measurement mechanism output terminal of fractionating system and device B; According to the product flow measuring-signal of catalytic cracking unit fractionation, absorbing-stabilizing system and advance the fresh feed flow measurement signal of reactor and export the target productive rate measuring and calculating device (hereinafter to be referred as device C) of optimization aim productive rate measuring and calculating value, the input end of device C connects the output terminal of catalytic cracking unit reaction-regeneration system measurement mechanism output terminal, catalytic cracking unit fractionating system measurement mechanism output terminal and catalytic cracking device absorption stabilizing system measurement mechanism respectively; Export the optimization means (hereinafter to be referred as device D) of the conversion rate of products optimization setting value (hereinafter to be referred as setting value) under certain material condition according to the optimization aim of the target productive rate measuring and calculating signal of the feedstock property characteristic number of the conversion rate of products measuring and calculating signal of device A output, device B output and device C output and setting, the input end of device D is hinged with the conversion rate of products measuring and calculating signal output part of putting A, the feedstock property characteristic number output terminal of device B and the target productive rate measuring and calculating signal output part of device C respectively; According to the conversion rate of products observation discreet value that will install A output as measured value with will install the conversion rate of products optimization setting value that D exports and determine deviation as setting value, and export the conversion rate of products closed loop controller (hereinafter to be referred as controller) that makes the regeneration valve valve position control signal that deviation eliminates with this, the conversion rate of products real-time monitored of the measurement of the input end of controller (PV) terminating set A is estimated the output terminal of signal, the output terminal of the setting of controller input end (SV) terminating set D, the output terminal output regeneration valve valve position control signal of controller is to regeneration valve, thereby adjust the regeneration valve valve position, change the catalyst flow that advances the catalytic cracking unit reactor, finally eliminate the deviation between measured value and the setting value.
Device A can comprise the measuring and calculating device (hereinafter to be referred as device A1) of exporting the recycle ratio signal according to the recycle stock that advances the catalytic cracking unit reactor (comprising reprocessed oil slurry) flow and fresh feed flow measurement signal, and the input end of device A1 taps into catalytic cracking unit reaction-regeneration system measurement mechanism output terminal and the catalytic cracking unit fractionating system measurement mechanism output terminal of device A respectively; According to recycle stock in the fresh feed flow measurement signal that advances reactor, the fractionating system accumulate with withdrawing device and fractionator at the bottom of liquid level, extract out measuring mass flow signal or fractionator products of separated flow measurement signal or according to the oil gas sampling analysis signal that advances fractionator the conversion rate of products measuring and calculating device (hereinafter to be referred as device A2) of output products conversion ratio measuring and calculating signal, the input end of device A2 taps into the fractionating system measurement mechanism output terminal of device A and the output terminal of reaction-regeneration system measurement mechanism respectively; The output products conversion ratio is estimated the conversion rate of products estimating device (hereinafter to be referred as device A3) of signal according to the output signal of catalytic cracking unit temperature of reactor, pressure measurement signal, regeneration valve valve position measuring-signal and device A1, device B, and the input end of device A3 taps into the output terminal of the catalytic cracking unit reaction-regeneration system measurement mechanism output terminal of device A, device B and the output terminal of device A1 respectively; Estimate signal and the output products conversion ratio is estimated the means for correcting (hereinafter to be referred as device A4) of correction signal, the input terminating set A2 of device A4, the output terminal of A3 according to the conversion rate of products of the conversion rate of products measuring and calculating signal of device A2 and device A3; A totalizer, totalizer input end are hinged with the conversion rate of products of putting A3 output respectively and estimate the conversion rate of products of signal and device A4 output and estimate correction signal, and the real-time monitored of totalizer output products conversion ratio is estimated signal to controller and measured (PV) end; The input end of D is put in the measuring and calculating signal tipping of the conversion rate of products of device A2 output.
In fact, regeneration valve, controller, conversion rate of products observation estimating device (promptly installing A) and optimization means (promptly installing D) are formed the control device of whole catalytic cracking unit reaction depth, it provides with the catalytic cracking conversion rate of products is the closed-loop optimization system and the optimization method of the catalytic cracking unit of main regulation and control amount, its core comprises feedstock property observation counting system, a conversion rate of products measuring and calculating and estimates system, the closed loop controller of target productive rate measuring and calculating and a conversion rate of products optimization setting system and a conversion rate of products.The present invention has changed the mode of operation of regeneration valve control temperature of reaction in the past or reaction heat, and makes regeneration valve directly control the reaction depth of catalytic cracking reaction, has fundamentally improved the technological operation of catalytic cracking unit.
As everyone knows, the bad optimal control of closing of catalytic cracking unit is that a difficulty is worked greatly.The operation index of catalytic cracking mainly contains light receipts, liquid receipts, raw gasoline is done and diesel oil 95% solidifying point, the economic benefit of preceding two index direct relation auto levelizers, then index quality, especially raw gasoline of being related to oil product done and also directly had influence on the stable of gasoline output.And the directly distribution of influence reaction finished product of the size of conversion ratio (being reaction depth), reaction depth has decisive influence to the operation of full device, that is to say that it is the key of having caught whole operation for the control conversion ratio that the present invention changes conventional in the past control temperature of reaction.In fact temperature has mainly reflected thermal equilibrium, and (this also is a kind of unavoidable selection, because when not having conversion ratio measuring and calculating and estimating means, in can measuring to be subjected to multiple factor affecting, temperature of reaction is the amount that can reflect reaction depth), can not reflect reaction depth fully.Though catalytic cracking is an interactive complication system of multivariate, reaction depth is maximum to the influence of each link (as reaction, regeneration, fractionation, stable absorption).The control reaction depth is steady, also makes full device reach steady easily.Secondly, the present invention has increased feedstock property online observation system, makes original immesurable feedstock property can introduce online observation and tuning method, thereby realize the line closed loop tuning, improved automaticity, need not the operative employee basically and intervene, operation, maintenance are more prone to carry out.In addition, adopt conversion ratio control, though some fluctuation of temperature, gasoline endpoint and fractionator are very steady, guarantee product quality, have improved the variation adaptive faculty of controller to feedstock property.Simultaneously, because optimization system itself has a complete fault diagnosis system and an a series of safety precautions, so fortuitous event occurs when device,, host computer sudden power malfunctioning as instrument etc. all can switch to the routine control of slave computer, assurance safety in time.And owing to estimate accurately, the controller adjustment is suitable, and the control performance of device is good, and antijamming capability is strong, and light oil yield increases, steady quality.
Fig. 1 is a structured flowchart of the present invention.
Fig. 2 is a conversion rate of products observation estimating device example structure block diagram of the present invention.
The present invention is further illustrated below in conjunction with a kind of embodiment and control procedure thereof.
As shown in Figure 1, the reaction-regeneration system (S of catalytic cracking unit (S)
1) measurement mechanism (S
10) the output terminal conversion ratio observation estimating device (A), feedstock property observation device (B) and the target productive rate that are connected to the optimal control system respectively calculate device (C).Fractionating system (the S of catalytic cracking unit (S)
2) measurement mechanism (S
20) output terminal is connected to conversion ratio observation estimating device (A) respectively and the target productive rate is calculated device (C).Absorbing-stabilizing system (the S of catalytic cracking unit (S)
3) measurement mechanism (S
30) output terminal is connected to target productive rate measuring and calculating device (C).The conversion rate of products measuring and calculating signal output of conversion ratio observation estimating device (A), the feedstock property characteristic number output of feedstock property observation device (B), the target productive rate measuring and calculating signal output of target productive rate measuring and calculating device (C) and the optimization aim of system are connected to optimization means (D).The feedstock property characteristic number output of feedstock property observation device (B) also is connected to conversion ratio observation estimating device (A).The conversion rate of products observation discreet value signal output of conversion ratio observation estimating device (A) connects measurement (PV) end of controller (E) input end, the conversion rate of products optimization setting value output of optimization means (D) connects setting (SV) end of controller (E) input end, and the output terminal output regeneration valve valve position of controller (E) controls signal to regeneration valve (S
4), forming a closed loop thus, the adjustment of regeneration valve valve position has changed the catalyst flow that advances reactor, finally eliminates the deviation between measured value and the setting value.Controller can adopt the PID controller.
The conversion ratio observation estimating device of optimal control system as shown in Figure 2, can be by measuring and calculating device A
1, A
2, conversion rate of products estimating device A
3, means for correcting A
4, totalizer A
5Form.Fractionating system measurement mechanism (S by catalytic cracking unit
20) output be connected to device A
1Reaction-regeneration system measurement mechanism (S by catalytic cracking unit
10) output be connected to device A
1, A
2, A
3Output by device B is connected to device A
3Device A
2The conversion rate of products measuring and calculating value signal output of output is connected to device D and means for correcting A
4Device A
1The recycle ratio of output is connected to device A
3, device A
3Conversion rate of products estimate signal and export means for correcting A to
4With totalizer A
5Input end, means for correcting A
4Conversion rate of products estimate correction signal and export totalizer A to
5Another input end.Totalizer A
5The conversion rate of products real-time monitored of output is estimated measurement (PV) end that signal is connected to controller E.
Device B can constitute as follows: with the temperature distributing measuring signal of catalytic cracking unit reaction-regeneration system (1), advance the catalyst flow measuring and calculating signal and the combined feed flow measurement signal feeder B of catalyst cracker, and by following equation output feedstock property characteristic number:
YX(t)＝F(β(t)，ΔTra(t)，Tra(t))
Wherein, YX (t) is the characteristic number of t sign feedstock property constantly, and β (t) advances the catalyst flow of reactor and the ratio of combined feed flow constantly for t, and the catalyst flow that wherein advances reactor is by special soft measurement mechanism measuring and calculating.If there is not this device, then can according to regenerator temperature distribution signal and the estimation of regenerator thermal balance equation, also can estimate by method commonly used on the technology according to the regeneration valve flow characteristics.Δ Tra (t) and Tra (t) are respectively t temperature of reactor difference signal and temperature signal constantly.F is a nonlinear function, and its concrete form can push away by the reactional equation of reactor, or presses the nonlinear function approach method, adopts various nonlinear function forms to form.
Under situation with good conditionsi, also can utilize on-line analysis instrument real-time online measuring raw material to form.
Device A can realize by Fig. 2: concrete grammar is with the temperature of catalyst cracker, pressure measurement signal, fresh feed flow signal and regeneration valve valve position measuring-signal, the output signal of device B, the recycle stock of fractionating system extract out and accumulate device liquid level, extract liquid level at the bottom of measuring mass flow signal, the fractionator out, extract the input end that the measuring mass flow signal halves is heated up in a steamer systems measures signal feeder A out.Wherein install the actual conversion of A2 measuring and calculating catalytic cracking product, one of method is at first to estimate the actual recycle stock total amount of t catalytic cracking unit constantly by following formula
H(t)＝F1(t)+F2(t)+f1(Δh1(t))+f2(Δh2(t))
Wherein, F1 (t) is for accumulating the recycle stock flow that device is extracted out from recycle stock, F2 (t) is the slurry oil flow of extracting out at the bottom of the fractionator, and f1 (Δ h1 (t)) and f2 (Δ h2 (t)) are respectively the recycle stock relevant with liquid level change (Δ h2) at the bottom of recycle stock accumulates device liquid level change (Δ h1) and fractionator and the dynamic amount of savings of slurry oil.
Then, can estimate t conversion rate of products constantly by following formula:
CON (t)=(1-H (t)/F0 (t) * 100% or CON (t)=(1-H (t)/F0 (t)+F1 (t)+F2 (t) * 100%
Wherein F0 (t) is the fresh feed amount flow of into reactor.
Reactor product amount (raw gasoline amount, diesel oil amount, the rich gas amount) measuring and calculating that the product actual conversion CON (t) of device A2 output also can separate according to fractionating system or directly use the on-line analysis instrument measurement.
In device A1, press following formula measuring and calculating recycle ratio
R(t)＝(F1(t)+F2(t))/(F0(t)+F1(t)+F2(t))
Device A3 is a prediction device, can utilize neural network or prediction model structure, temperature of reaction, reaction pressure and the regeneration valve valve position signal of device B, the device output of A1 and the output of catalytic cracking unit reaction-regeneration system measurement mechanism are delivered to the input end of A3, then can export the conversion rate of products CONP (t) that estimates in real time at the output terminal of device A3.The output CONP (t) of device A3 and output CON (t) the feeder A4 of device A2 are also stored, can estimate the signal correction value by following formula output products conversion ratio
Δ CONP (t)=CON (t)-CONP (t-τ) wherein τ is the retardation time of the conversion rate of products measuring and calculating of device A2 output.
To install A4 output valve and device A3 output send into totalizer A5 do " with " computing after, just be total output of device A, it is sent into the measuring junction of controller, as the measured value (PV value) of controller.
The catalytic cracking final products flow signal of the fractionating system products of separated flow signal of fractionating system measurement mechanism output and the output of absorbing-stabilizing system measurement mechanism, the fresh feed flow measurement signal that advances reactor are delivered among the device C, in device C, can calculate target productive rate J (t) respectively by products of separated raw gasoline, rich gas, the diesel oil equivalent of fractionator, also can be accustomed to, press the measuring and calculating target productive rates such as final products stabilized gasoline, liquefied gas, light diesel fuel, dry gas of absorbing-stabilizing system by technology.Productive rate is pressed the following formula measuring and calculating:
J(t)＝(C(t)/F0(t))×100％
Wherein C (t) has gasoline, light oil (gasoline+diesel oil), liquid receipts (gasoline+diesel oil+liquefied gas) etc. multiple for by the selected product flow of optimization aim, and F0 (t) is the fresh feed flow.
Output YX (t) with device B, the output CON (t) of device A2 among the device A, optimization aim J reaches the input end of being sent into optimization means by the target yield value J (t) of device D output, optimization means can be according to neural network configuration, also can be according to the Optimization Model structure of releasing according to the catalytic cracking process mathematics model of stable state, optimization setting value CONS (t) at the output terminal output products conversion ratio that installs, this optimization setting value is sent into the setting end of conversion rate of products controller, as the setting value (SV value) of controller, controller output by the regenerator of catalytic cracking unit to the flow valve position signal of the operation valve (regeneration valve) on the pipeline of the catalyzer of reactor.Promptly regulate the into catalytic amount of riser reactor, reach the purpose of control conversion rate of products (being reaction depth) balance by control regeneration valve valve position.Controller can adopt PID controller commonly used, and can adopt the parameter of the real-time correcting controller of adaptive algorithm, and control performance is reached the set quota.Control conversion rate of products balance, thus reach the target of optimizing product distribution and product quality.
The collection of each measuring-signal in the above-mentioned embodiment and filtering and each observation, measuring and calculating device, estimating device, means for correcting and controller can be realized by Distributed Control System (DCS) (DCS) and host computer thereof.Also can realize by single chip microcomputer, electronic instrument and electronic circuit.
Claims (3)
1. optimization control system for catalytic cracking plant is characterized in that: comprise
1). according to the temperature signal of catalytic cracking unit reactive system, advance the catalyst flow measuring and calculating signal of catalytic cracking unit reactor and advance the catalytic cracking unit reactor the combined feed flow measuring-signal and export the feedstock property observation device (hereinafter to be referred as device B) of the characteristic number that characterizes catalytically cracked material character, the output terminal of the measurement mechanism of the input termination catalytic cracking unit reaction-regeneration system of device B;
2). according to the temperature of catalyst cracker, pressure and be arranged on regenerator to the flow measuring-signal of operation valve (hereinafter to be referred as the regeneration valve) valve position on the pipeline of the catalyzer of reactor, advance the measuring-signal of the fresh feed flow of reactor, the flow of catalytic cracking unit fractionating system, the feedstock property characteristic number of level gauging signal and device B output and export the conversion rate of products observation estimating device (hereinafter to be referred as device A) of the real-time monitored discreet value of the measuring and calculating value of catalytic cracking reaction conversion rate of products (hereinafter to be referred as conversion rate of products) and conversion rate of products, the input end of device A connects catalytic cracking unit reaction-regeneration system measurement mechanism output terminal respectively, the output terminal of the measurement mechanism output terminal of fractionating system and device B;
3). according to the product flow measuring-signal of catalytic cracking unit fractionation, absorbing-stabilizing system and advance the fresh feed flow measurement signal of reactor and export the target productive rate measuring and calculating device (hereinafter to be referred as device C) of optimization aim productive rate measuring and calculating value, the input end of device C connects the output terminal of catalytic cracking unit reaction-regeneration system measurement mechanism output terminal, catalytic cracking unit fractionating system measurement mechanism output terminal and catalytic cracking device absorption stabilizing system measurement mechanism respectively;
4). according to the conversion rate of products measuring and calculating signal of device A output, feedstock property characteristic number and the target productive rate measuring and calculating signal of device C output and the optimization means (hereinafter to be referred as device D) of being exported the conversion rate of products optimization setting value (hereinafter to be referred as setting value) under certain material condition by the optimization aim of technology personnel setting of device B output, the input end of device D is hinged with the conversion rate of products measuring and calculating signal output part of putting A, the feedstock property characteristic number output terminal of device B and the target productive rate measuring and calculating signal output part of device C respectively;
5). according to installing A output products conversion ratio observation discreet value as measured value with will install the conversion rate of products optimization setting value that D exports and determine deviation as setting value, and export the conversion rate of products closed loop controller (hereinafter to be referred as controller) that makes the regeneration valve valve position control signal that deviation eliminates with this, the conversion rate of products real-time monitored of the measurement of the input end of controller (PV) terminating set A is estimated the output terminal of signal, the output terminal of the setting of controller input end (SV) terminating set D, the output terminal output regeneration valve valve position control signal of controller is to regeneration valve.
2. optimization control system for catalytic cracking plant as claimed in claim 1 is characterized in that said device A comprises
1). export the measurement mechanism (hereinafter to be referred as device A1) of recycle ratio signal according to the recycle stock flow that advances catalyst cracker and fresh feed flow measurement signal, the input end of device A1 taps into catalytic cracking unit reaction-regeneration system measurement mechanism output terminal and the catalytic cracking unit fractionating system measurement mechanism output terminal of device A respectively;
2). according to recycle stock in the fresh feed flow measurement signal that advances reactor, the fractionating system accumulate with withdrawing device and fractionator at the bottom of liquid level, extract out measuring mass flow signal or fractionator products of separated flow measurement signal or according to the oil gas sampling analysis signal that advances fractionator the conversion rate of products measurement mechanism (hereinafter to be referred as device A2) of output products conversion ratio measuring-signal, the input end of device A2 taps into the fractionating system measurement mechanism output terminal of device A and the output terminal of reaction-regeneration system measurement mechanism respectively;
3). the output products conversion ratio is estimated the conversion rate of products estimating device (hereinafter to be referred as device A3) of signal according to the output signal of catalyst cracker temperature, pressure measurement signal, regeneration valve valve position measuring-signal and device A1, device B, and the input end of device A3 taps into the output terminal of the catalytic cracking unit reaction-regeneration system measurement mechanism output terminal of device A, device B and the output terminal of device A1 respectively;
4). estimate signal and the output products conversion ratio is estimated the means for correcting (hereinafter to be referred as device A4) of correction signal, the input terminating set A2 of device A4, the output terminal of A3 according to the conversion rate of products of the conversion rate of products measuring and calculating signal of device A2 and device A3;
5). a totalizer, the input end of totalizer is hinged with the conversion rate of products of putting A3 output respectively and estimates the conversion rate of products of signal and device A4 output and estimate correction signal, and the real-time monitored of totalizer output products conversion ratio is estimated measurement (PV) end of signal to controller;
6). the input end of D is put in the measuring and calculating signal tipping of the conversion rate of products of device A2 output.
3. optimization control system for catalytic cracking plant as claimed in claim 1 is characterized in that said controller adopts the PID controller.
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| CN106647285B (en) * | 2017-02-10 | 2019-08-09 | 泉州装备制造研究所 | A kind of catalyst activity detection method based on soft-measuring technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2050189U (en) * | 1988-05-10 | 1989-12-27 | 中国石油化工总公司科技装备公司 | Miniature reaction device controlled by microcomputer |
| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2050189U (en) * | 1988-05-10 | 1989-12-27 | 中国石油化工总公司科技装备公司 | Miniature reaction device controlled by microcomputer |
| 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 |
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