CN106118715B - Petroleum fractionator operation conditions observer - Google Patents
Petroleum fractionator operation conditions observer Download PDFInfo
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- CN106118715B CN106118715B CN201610523379.3A CN201610523379A CN106118715B CN 106118715 B CN106118715 B CN 106118715B CN 201610523379 A CN201610523379 A CN 201610523379A CN 106118715 B CN106118715 B CN 106118715B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of real-time observers of petroleum fractionator operation conditions, it is made of with output processor sequence actual measurement variable timely collection device, the flow observer that comes in and goes out, tower internal loading observer, product quality observer, feedstock property observer, result of calculation display storage, institute is functional to be realized on distributed computer control system DCS, every the real-time freshness value in the time less than or equal to 20 seconds, providing no measured value variable；The present invention provides comprehensive real time information of petroleum fractionator operation conditions, the real-time early warnings information such as erosion control tower, liquid-leakage preventing, anti-liquid flooding, anti-dry plate or evacuation, unusual service condition are provided, ensure that fractionating column safe operation；Product quality real-time control is realized in the real-time computed improved operation of product quality, improves high-value product yield；The real-time judge of material property change has adapted to material composition change, quiet run；If fractionating column raw material product distribution in chemical reactor, raw material is the foundation of reactor real-time optimization.
Description
Technical field
The present invention relates to a kind of petroleum fractionator operation conditions observers, belong to production process dynamics application technology neck
Domain.
Background technology
Petroleum fractionator of the present invention refer to tower top and bottom product outside, also with sideline product petroleum fractionating
Tower main body and corresponding peripheral equipment.Material into fractionating column is the feedstock oil for becoming vapour phase under high temperature, is passed through in fractionating column
Mass-and heat-transfer between tens layers column plate is separated into oil gas, gasoline or naphtha, kerosene, diesel oil, the wax of the requirement that meets the specification
The various products such as oil, crude lube stock.
The petroleum fractionator of normal operation is the dynamical system that a multivariable interacts, and reflects the variable of operation conditions
Often change over time.But many variable variables do not have a real-time measurement instrument table, vapour, liquid phase stone in tower on tens layers column plate
The temperature of oil distillate only has a small amount of measuring point, in tower vapour-liquid phase load, feedstock property without real-time measuring data, operation conditions,
Failure and unusual service condition are difficult to be analyzed in time, it is difficult to adapt to material property change, product quality leans on assay, from sampling
One more than hour is usually wanted to data are obtained, it is difficult to controlled in time product quality, it is difficult to realize safety and steady optimization
Operation.
, has there is following two categories side in real time information that is important but can not surveying variable when to provide petroleum fractionator operation
Method：One kind is that the variable metastable state relationship based on petroleum fractionator operation mechanism is calculated, such as grand with Clausius-carat uncle
(Clausius-Clapeyron) the pressure compensation temperature relation provided, the quality of approximate calculation oil product；Or with stable state number
It learns model the gas-liquid phase load in tower such as to calculate, such methods meet state when fractionating column stablizes constant, but inadaptable
Dynamic change when fractionating column is run.Another kind of method is to be returned to calculate with measured data, such as least square method or with certain people
For relationship, such as neuroid, the variable without measured value is estimated；Due to not pressing the operation mechanism of petroleum fractionator, and usually not
Consider dynamic change when fractionating column operation, or assumes that dynamic rule, result of calculation can only adapt to actual measurement and become using artificial
The corresponding small change range of institute, does not adapt to the variation of operating conditions and feedstock property, not can determine that and provide when amount
Result of calculation whether meet fractionating column operation mechanism, or even will appear direction that result of calculation and process mechanism determine on the contrary,
Lead to the operation and control of mistake.
Invention content
The purpose of the present invention is：The observer of dynamic change situation when providing a kind of adaptation petroleum fractionator operation, including
Vapour-liquid phase load, product quality, feedstock property etc. can not survey the instantaneous value of variable in inflow and outflow fractionating column flow, tower, with
Petroleum fractionator is improved to operate horizontal, realization product quality bounder control and energy-saving, adaptation material property change, realize and pacify
Entirely, steady and optimal control.
1, essential characteristic of the invention：
1-1Petroleum fractionator observer：The each section completed by following sequence forms：See Fig. 1
1. petroleum fractionator surveys variable Acquisition Processor：Containing fault detect, it is real-time without actual measurement variable to be that the present invention is provided
The foundation of value.
2. come in and go out flow observer：Instantaneous value of the inflow and outflow fractionating column without measured value flow is provided, to run shape situation
Analysis and following observation provide calculation basis.
3. tower internal loading observer：Provide disengaging tower in each tower section interior return flow and vapour phase oil product flow it is real-time
Value, calculates in real time for operation conditions, product quality in tower and material property change judgement provides real time data, is erosion control tower, anti-
Leakage, anti-liquid flooding, anti-dry plate or evacuation, unusual service condition etc. provide warning information.
4. product quality observer：According to oil and gas partial pressure compensation temperature, the real-time distillation characteristic of oil product and tower internal loading, provide
The instantaneous value of tower top and each sideline product quality, real-time monitoring and control to realize product quality provide foundation.
5. feedstock property observer：It provides and flows into each tower section vapour phase material property change real time information；If raw material is from change
Reactor is learned, the real time information of reactant product form is provided, the foundation as reactor control and sorrow.
6. result of calculation shows, stores and output processor；
The entirety that petroleum fractionator observer is made of above each section can control system in existing distributed computer
It is realized on system DCS；Wherein 1 and 6 can utilize prior art to realize.The result that all observations calculate can be less than or equal to 20 seconds
Real-time freshness value is provided in period.
1-2.The instantaneous value without measured value variable is determined according to dynamic rule and actual measurement variable
Often for the variable of its operation conditions in dynamic change, is reflected when petroleum fractionator is run, regardless of whether there is reality
Measured value all changes over time.When temperature change, the heat of savings changes therewith, when liquid level changes in Ta Nei or container, holds
The inventory put aside in device changes therewith.The rule of dynamic change is dynamic equilibrium, i.e., material savings variable quantity be equal to flow into
The difference of inventory is flowed out, thermal reservoir variable quantity is equal to the difference of inflow and outflow heat；Wherein inflow and outflow heat depends on temperature
With the product of heat carrier flow.
In the inventory or heat that flow in and out, some have measured value, some are provided without measured value, online calculate in real time
Instantaneous value without measured value variable, it is necessary to calculate dynamic savings variable quantity, referred to as observer.Dynamic puts aside the general table of variable quantity
It is up to formula：
Common savings variable quantity is as follows in fractionating column：
To thermal reservoir variable quantity:X=T=temperature,
Heat needed for one unit of C=temperature changes, referred to as thermal capacity
Variable quantity is put aside to liquid phase material in container：X=HL=liquid level
C=liquid levels change liquid phase object doses, referred to as material capacity needed for a unit
Vapor-phase material puts aside variable quantity in container:X=P=container pressures
Vapor-phase material amount needed for one unit of C=pressure changes, referred to as material capacity
When state variable has measured value, amount of savings variable quantity can be calculated with following formula：
T=current time TS=calculating cycle, it is proposed that TS≤ 20 seconds；
X (t), x (t-TS)=current and the previous cycle moment actual measurement state variable value.
The present invention uses again after being filtered to state variable measured value(1-2)Formula calculates.Existing filtering method can be selected to carry out
Filtering, such as：First-order filtering, moving weighted average filtering, speed limit filtering, the filtering of adaptive speed limit etc., optional one of which, or with
The combination of upper filtering method, such as adaptive speed limit filtering are connected with first-order filtering.
When state variable is without measured value, need first to be observed calculating to no measured value state variable, then press(1-2)Formula calculates
Dynamic savings variable quantity, refers to tower internal loading observer explanation.
1-3The real-time inspection of ornamental and ornamental
Utilize dynamic rule and possessed actual measurement variable, if can calculate and provide the real-time of no measured value variable
Value, is exactly considerable sex chromosome mosaicism.
For petroleum fractionator, there is apparent thermal reservoir amount when vapour phase and liquid phase oil product temperature change on every layer of column plate
Variation, i.e., per on laminate liquidus temperature and gas phase temperature be state variable, but the phase temperature on many layer column plates
Without measured value, the vapour-liquid phase flow rate of each layer column plate of inflow and outflow is also without measured value, therefore, it is not possible to be provided by the calculating of actual measurement variable
The instantaneous value of each relevant variable, i.e., do not have ornamental on every layer of column plate.Phase oil product temperature on every laminate is all arranged
Measuring instrumentss be it is unpractical, it is also unnecessary.
The observation that the present invention is carried out vapour-liquid phase load in tower by tower section calculates, as long as the phase oil product temperature of disengaging tower section
With measured value, entering out each flow of fractionating column has instantaneous value, forms ornamental, observer method is used in combination to provide each layer in tower section
Phase oil product accumulated heat variable quantity on plate, to provide the phase oil product flow of each tower section of inflow and outflow, i.e. tower internal loading
Instantaneous value, meet the requirement that operation conditions is observed in real time, be the present invention feature.
When any one occurrences failure in actual measurement variable used in observation calculating, ornamental is just lost.If going out
Inbound traffics observer loses ornamental, and each observer of postorder also loses ornamental.Therefore, the present invention examines ornamental in real time
It tests, provides inconsiderable information, prevent problem.
1-4It is calculated by oil property under fractionating column operation conditions
Oil is complex system, can not be analyzed it and be calculated with each pure component of its composition, in petroleum fractionator
When actual motion is with operation, usually analyzed with the weight of oil product, or analyzed with the product form of raw material, therefore,
Observation provides real time information related to this in calculating.
In the design and operation of petroleum fractionator, true boiling point distillation characteristic, Engler distillation and equilibrium evaporation data are commonly used,
These distillation characteristics all obtain under given conditions, it is impossible to be used in the real-time calculating under actual operating state.The present invention
Common distillation data are modified by fractionating column actual operating state, form real-time distillation characteristic, as the foundation of calculating,
Refer to product quality observer.
A kind of petroleum fractionator operation conditions observer of the present invention, dynamic change when according to petroleum fractionator operation
Rule and actual measurement variable, provide method of the determining petroleum fractionator without measured value variable instantaneous value and implement structure, to ornamental
Real-time inspection is carried out, inconsiderable information is provided, prevents problem.
After implementing the present invention, comprehensive real-time letter of petroleum fractionator operation conditions will be provided for production management and operating personnel
Breath provides the real-time early warnings information such as erosion control tower, liquid-leakage preventing, anti-liquid flooding, anti-dry plate or evacuation, unusual service condition, is fractionating column safety
The important measures of operation；The real-time calculating of product quality is to improve operation, realize product quality real-time control, improves high value production
The basis of product yield；The real-time judge of material property change be adapt to material composition change, quiet run important information；If fractionating column
Raw material product distribution in chemical reactor, raw material is the foundation of reactor real-time optimization.These effects, have been practical application
It is confirmed.
Description of the drawings
Fig. 1 petroleum fractionator operation conditions observer schematic diagrames.
Fig. 2 atmospheric fractional towers bottom schematic diagram, wherein：
T* indicates that temperature measuring instrument, L* indicate level gauging instrument
F* indicates that flow measurement instrument, P* indicate pressure measuring instruments
Fig. 3 catalytic cracking unit main fractionating towers bottom schematic diagram, wherein：
T* indicates that temperature measuring instrument, L* indicate level gauging instrument
F* indicates that flow measurement instrument, P* indicate pressure measuring instruments
Fig. 4 delayed coking unit main fractionating towers bottom schematic diagram, wherein：
T* indicates that temperature measuring instrument, L* indicate level gauging instrument
F* indicates that flow measurement instrument, P* indicate pressure measuring instruments
Fig. 5 tower section schematic diagrames, wherein：
T*:Indicate temperature measuring instrument, L*:Indicate liquid phase oil product flow in tower, i.e., interior return flow
F*:Indicate measured discharge instrument, V*:Indicate vapour phase oil product flow in tower, G:Indicate product flow
Subscript i：Tower section serial number from bottom to top
Subscript:V- vapour phase oil products, L- liquid phase oil products, W- water vapours, A- add oil product, R- circulating refluxs.
Specific implementation mode
2, petroleum fractionator is come in and gone out without measured value flow observer (2. in Fig. 1)
Vapour phase oil of the inflow and outflow fractionating column without measured value flow containing each product flow of fractionating column and into fractionating tower tray
Product flow, the characteristics of calculating these flow instantaneous values in real time online be：Consider to become with the dynamic savings in fractionating column relevant device
Change amount, the specific method is as follows.
Embodiment 1
2-1.：The observation that tower top distillates product flow calculates
Tower top, which distillates product, naphtha or gasoline or petrol vapour, is vapour phase at the tower top place of distillating, after cooling gasoline
Or naphtha be liquid phase, into knockout drum after the two is detached, from knockout drum flow out natural gas and liquid-phase product flow have
Measuring instrumentss, it is to consider dynamically to put aside variable quantity in oil and gas knockout drum that observation, which calculates the characteristics of tower top distillates each product flow,.
Tower top distillates vapor-phase product flowObservation calculates as follows in real time：
T=current times
Ptop=actual measurement tower top separation pressure tank Ts=calculating cycle
Tower top distillates gasoline or naphtha product flowInstantaneous value calculate it is as follows:
Ao=tower top knockout drum fuel head and corresponding sectional area
When tower top knockout drum is sleeping tank, AoIt is the function of liquid level
Aw=tower top knockout drum oil-water interfaces height and corresponding sectional area
ρo=liquid-phase product severe TS=calculating cycle≤20 second
The total flow that tower top distillates the oil product in vapour phase is：
Embodiment 2
2-2：Side line distillates the real-time calculating of product flow
The characteristics of observation calculates is to consider product dynamic savings variable quantity in sideline product stripper
Wherein：J=sideline product serial numbers, usually sort from up to down
ρj,Aj=product severe and stripper sectional area
Embodiment 3
2-3：Into atmospheric tower lowest level column plate phase feed flow
To the flow of atmospheric tower bottom of tower shown in Fig. 2, the gas of rectifying tower section lowest level plate is entered according to materials at bottom of tower EQUILIBRIUM CALCULATION FOR PROCESS
The instantaneous value of phase flow rate：
Wherein：F0(t)=actual measurement current time is worth after entering the filtering of tower raw material oil stream amount；
Fb(t) it is worth after=actual measurement current time bottom of tower extraction flow filtering；
F1(t)=actual measurement current time lowest level column plate is worth after flowing into the filtering of bottom of tower flow；
Lb(t) it is worth after=actual measurement current time bottom of tower liquid level filtering；
Lb(t-TSValue after)=actual measurement previous moment bottom of tower liquid level is filtered；
ρbThe severe of=bottom of tower oil；Ab=bottom of tower liquid level sectional area.
Embodiment 4
2-4：Into the observation of catalytic cracking unit main fractionating tower lowest level plate vapour phase flow and reaction product flow.It is flowed
Journey is shown in Fig. 3.Vapour-phase reaction product enters fractionating column from bottom of tower, upwards through herringbone plate washer, by returning the recycle oil of bottom of tower and above returning tower
After cycle slurry oil takes heat, the vapour phase raw material flow V into first layer rectifiying plate is formed0, but V0With reaction product flow F0Equal nothing
Measuring point, by materials at bottom of tower and heat dynamic equilibrium calculation：
Collapser material balance：V0=F0+F2-Fb (2-7a)
Materials at bottom of tower balances：
F2=recycle oil returns bottom of tower flow F3Extract slurry oil flow out in=bottom of tower
Lb=bottom of tower liquid level Ab,ρb=bottom of tower sectional area and oil product severe
Herringbone plate part thermal balance:
T1Vapour phase oil product and tower wall thermal capacity and temperature on=collapser
Cex,T6=collapser and tower wall thermal capacity and temperature
QR(t)=F4[h(T7)-h(T4)]=above return tower cycle slurry oil take heat
H (T), the vapour phase enthalpy of oil product and liquid phase enthalpy when h (T)=temperature is T
Simultaneous solution (2-7b) and (2-8) formula, you can obtain V0And F0Instantaneous value.
Embodiment 5
2-5：Into the observation of delayed coking unit main fractionating tower reaction oil gas flow and the vapour phase flow of lowest level column plate
It calculates
Delayed coking unit main fractionating tower underflow journey is shown in Fig. 5.
It is calculated by materials at bottom of tower and heat dynamic equilibrium：
Material balance：V0=F2+F0-Fb (2-9)
ρb,AbThe respectively severe of bottom of tower liquid phase oil product and bottom of tower sectional area
Lb=bottom of tower liquid level measured value F2,F3:See Fig. 4
F5=into coking furnace raw material flow measured value F4=freshening oil stream amount measured value
Thermal balance：By heat Balance Calculation F0=enter fractionating column pyrogenetic reaction product flow：
Qw=F6[Hw(T0)-Hw(T2)]=water vapour brings heat into
By (2-9) (2-11) formula：
Wherein：
Q1=F2[H(T2)-h(T1)] Q2=Fb[H(T2)-h(T6)]
H (T), vapour phase enthalpy of h (the T)=oil product when temperature is T, liquid phase enthalpy
Embodiment 6
3, the real-time observer of vapour-liquid phase load in petroleum fractionator
3-1Tower section divides and ornamental
According to 1-4 section ornamental explanations, calculating is observed by tower section material and heat dynamic equilibrium.The present invention is by following
Principle divides tower section：It is a tower section to take the adjacent tray of heat with circulating reflux, as top pumparound tower section and each stage casing are returned
Stream takes thermal tower section.If sideline product extracts layer out and its dried layer column plate forms a tower section above.Tower plate structure ruler in each tower section
It is very little identical.The column plate number of plies for including in tower section should not be excessive.
Fig. 5 is tower section schematic diagram.The column plate that this explanation is entered with vapour phase raw material, i.e. tower section where lowest level rectifiying plate
Serial number 1, above pushes away successively, and tower top section serial number is maximum.Variable wherein in solid box, including the liquid phase of each tower section of inflow and outflow and
Temperature, the circulating reflux of vapour phase oil product take heat and additional oil product flow and temperature, steam rates etc. to have measured value, flow into stream
Going out fractionating column flow has observation, and being tower section has the needed point layout of ornamental.Variable in dot-dash wire frame is not surveyed
Value, i.e. the vapour phase flow V of inflow and outflow tower sectioni-1,ViWith liquid phase flow Li+1,Li, i.e., vapour-liquid phase load in tower need to be by observer
Its instantaneous value is provided.
Explanation is all made of the variable symbol provided in Fig. 5 and upper subscript below：
T=temperature (DEG C) V=vapour phase oil product flow L=liquid phase oil product flows
F=surveys fluid flow G=product flows
Subscript：I=tower sections serial number (is incremented by) from bottom to top
Subscript：V=vapour phase oil product L=liquid phase oil product W=water vapours
A=additional liquid phases oil product R=circulating refluxs
The default units of variable are：Temperature T (DEG C), flow F, G, V, L (ton/when).
3-2The dynamic balance type of tower section phase carry calculation
Tower section material balance (ignores the variation of material amount of savings)：I=tower section serial numbers
Tower section thermal balance：
(save and illustrate see 3-5)
H (T), h (T)=it is respectively vapour phase enthalpy of the oil product when temperature is T, liquid phase enthalpy
Following two recurrence calculation methods are provided by (3-1) (3-2) (3-3) derivation.
3-3By the 1st rectifying tower section of bottom of tower piecewise recurrence calculation upwards
By the vapour phase raw material oil temperature and flow V that enter the first tower section0, the first tower section outflow interior return flow L1Reality
Duration carries out recurrence calculation；
By i=1, it is known that Vi-1=V0,L1, start recurrence calculation：
The first step：Return flow L in calculatingi+1, by (3-1) formula, (3-3) formula is substituted into, is obtained：
Wherein：
For liquid phase oil product specific heat at constant pressure under corresponding mean temperature；
HV(T) the latent heat of vaporization of=oil product when temperature is T；
See (3-3) formula explanation；
Subscript "+" indicates to press tower section serial number recurrence calculation.
Second step：According to (3-1) (3-2) formula, outflow tower section vapour phase oil product flow V is calculatedi：
The V that above two step calculates i=2 is pressed again2And L3, so piecewise upward recursion, until tower top section.
Note：It also can first step calculating vapour phase oil product flow Vi, the interior return flow L of second step calculatingi+1。
Result of calculation is identical as the result that (3-4a) (3-4b) is provided, and omits its calculating formula herein.
3-4By tower top downward recurrence calculation paragraph by paragraph
The instantaneous value that product temperature and flow are distillated by known tower top cold reflux flow and temperature, tower top, by tower top section i=
nsStart downward recurrence calculation paragraph by paragraph, until i=1, that is, lowest level tower section:
The first step：Regurgitant volume in calculating
See (3-3) formula explanation；
HV(T) the latent heat of vaporization of=oil product when temperature is T；
As defined above, subscript "-" is indicated from the downward recurrence calculation of tower top section
Second step：Calculate Vi-1
Ibid, V also can first be calculatedi-1, then be calculated by (3-1) (3-2) formulaAnd Li。
3-5The real-time calculating of tower section accumulated heat variable quantity：
Tower section accumulated heatIt is the sum of each laminate liquid and vapor capacity oil product accumulated heat in section.But tower section only has top layer's stream
Going out vapour phase oil product temperature and lowest level plate liquid phase oil product temperature, there is measured value, the present invention to provide tower section whole by the following method
The Real-time monitored value of accumulated heat variable quantity：
3-5-1Vapour phase oil product and tower casing accumulated heat variable quantity are flowed out in tower section top layer：
Tower section top layer distillates vapour phase oil product temperatureWith measured value, therefore：
TS=observation calculating cycle
Subscript：I=tower section serial numbers ni=the i-th tower section top layer column plate serial number
3-5-2Tower section top layer plate liquid phase oil product and column plate accumulated heat variable quantity：
Tower section top layer plate liquid phase temperatureUsually without measuring point, but there is following relationship：
Vi,
There was only top plate liquid phase temperature in (3-8) formulaIt is unknown, therefore have：
It will(3-9)Formula substitutes into(3-7)Formula is to get top layer plate liquid phase and column plate accumulated heat variable quantity.
3-5-3Lowest level plate liquid phase oil product accumulated heat variable quantity
Lowest level plate liquid phase temperatureThere are the measured value, accumulated heat variable quantity to be：
If lowest level plate liquid phase flows out after collecting mailbox, and temperature point is mutually exported in philatelic, then need to be by oil sump tank dynamic
Model calculates provide in real timeObservation：
3-5-4Vapour phase accumulated heat variable quantity on tower section lowest level plate：
WithThere is measured value, it will be assumed thatInitial value, with actual measurement variable and(3-12)Formula carries out recursion
It calculates, makes after suitable calculating cycleApproach its true value.Dynamic accumulated heat variable quantity is calculated as follows again.
3-5-5The total accumulated heat variable quantity of tower section
niColumn plate quantity in=tower section
3-6Operating condition transfinites in tower or unusual service condition is alarmed
3-6-1I-th tower section outflow gas phase oil product linear speed calculates in real time：
Vi,Fi w=it is respectively the i-th tower section outlet gas phase oil product flow and steam rates (kg/h)
Ai=the i-th tower section sectional area (m2) P0Pressure (absolute pressure) under=standard state
The lower i-th section of gas phase oil product of atmospheric pressure, the severe (kg/m of water vapour3)
Ti, Pi=the i-th tower section exports observed temperature (DEG C) and pressure (absolute pressure)
3-6-2Operating condition transfinites judgement and early warning
WhenProvide the super upper limit of gas phase linear speedAlarm signal, erosion control tower；
WhenProvide the super lower limit of gas phase linear speedAlarm signal, liquid-leakage preventing；
WhenProvide overload alarm signal, anti-liquid flooding；
WhenProvide overload alarm signal, anti-dry plate or evacuation；
3-6-3Tower section unusual service condition judges：When there is following situations, abnormity early warning signal is provided：
The phase temperature differenceSuper bound；
Pass in and out tower section vapour phase difference in flow (Vi-1-Vi) super bound；
Pass in and out the poor (L of return flow in tower sectioni-Li+1) super bound；
The a certain variable of tower section has significant change, and other variables are without significant change.
Embodiment 7
4, petroleum fractionator product quality observer
Petroleum fractionator product quality is mainly doing for gasoline, 95% point or 90% point of navigate coal and diesel oil, Yi Jiyu
This related solidification point or pour point, flash-point, freezing point etc..These quality marks need to usually be sampled, be obtained through assay at the scene,
From sample obtain result usually at one more than hour, existing on-line quality instrument, lag time generally 5 minutes with
On, and sampled point does not distillate mouth in fractionating column product, cannot provide the instantaneous value of product quality, when actual motion, often with control
Temperature is means, but temperature can not accurately reflect product quality.
The present invention is based on oil properties, consider oil and gas partial pressure compensation temperature, oil property and tower internal loading to product quality
Influence, provide the instantaneous value that product evaporates exit product quality.
4-1One of Factors Affecting Product Quality：The real-time calculating of oil gas partial pressure
From principle, Clausius-carat uncle grand (Clausius-Clapeyron) gives pressure compensation temperature relation,
But for what petroleum fractionator, product, which distillates mouth not only, has this to distillate the product of mouth, also water vapour and other products, needs to use
Product evaporates the partial pressure compensation temperature of exit product, and relational expression is as follows：
J=0 is tower top liquid-phase product, and j=1,2,3,4 be one, two, three, four, sideline product
To sideline product, extracts vapour phase oil product temperature under layer out for product and is divided with product,
It is absolute pressure that product, which divides unit,；
Pa=atmospheric pressure
Product oil gas partial pressure is calculated as follows：
Pj=actual measurement calculates pressure (gauge pressure) under gained jth product extraction layer；
Lj=jth product extracts the interior return flow of layer out；
Fwi,Mw=jth product extracts steam rates and stream molecule amount under layer out；
The flow observer that respectively comes in and goes out provides each product flow and each molecular weight product.
4-2The two of Factors Affecting Product Quality：Real-time distillation characteristic and oil property
4-2-1Real-time distillation characteristic is temperature and liquid phase oil product evaporating capacity relationship, with temperature under fractionating column actual operating state
Degree is abscissa, and evaporating capacity is ordinate, indicates oil property.
Evaporating capacity uses unit of weight, and it is unit of weight not only to adapt to the flow value provided when production process operation often,
The slope of distillation characteristic is changed, temperature is higher, and the severe for vaporizing oil product increases therewith, and distillation characteristic slope increases, convenient for weighing apparatus
Measure oil property variation.
If within the scope of boiling point 10-90%, the distillation characteristic coefficient of evaporating capacity is measured for 1, with weight stream with volume flow
When gauge amount evaporating capacity, if the severe of vaporization oil product is directly proportional to vapourizing temperature, real-time distillation characteristic coefficient variation with temperature
Relationship is：
To gasoline：Diesel oil：
Interior return flow L is calculated by real-time distillation characteristici+1Vaporization flow in the i-th tower section：
aR,bR=adjustable parameter
It is to enter the i-th tower section to add oil product respectively
Real-time boiling range characteristic coefficient, boiling spread and initial boiling point
When actual motion, temperature, flow, heat all change at any time, and real-time distillation characteristic coefficient is also to become at any time
Change.
4-2-2Into the online real-time calculating of tower section vapour phase oil product distillation characteristic coefficient
Vi 0=enter the i-th tower section vapour phase oil product in not condensing flow
ClaimTo enter the real-time distillation characteristic coefficient of tower section vapour phase oil product, numerical value increases, and shows that vapour phase oil product becomes weight,
Being should be to a factor of the product end point of distillation.
The online real-time calculating of the 4-3 product end points of distillation：
4-3-1Fractionating column product evaporates the product end point of distillation at mouth and calculates in real time：
Except pressure compensation temperature and vapour phase oil distillation characteristic coefficientOutside, tower internal loading is also to influence product quality
Another factor, the product end point of distillation is online as the following formula to be calculated in real time：
For adjustable parameter；
4-3-2Simplifying for the end point of distillation calculates
Each variable not big variation when petroleum fractionator is run, can be used to lower simplified formula：
It is the adjustable parameter being calculated by rated value；
For zero adjusting parameter.
4-4The online real-time calculating of other products quality
4-4-1Navigate coal or diesel oil pour point TppOr the calculating of solidification point
Tpp=CppTi ep+Tpp0 (4-13)
Ti epThe end point of distillation (90% point or 95% point) of=aviation kerosine or diesel oil
CppFor adjustable parameter；Tpp0For zero adjusted value.
Adjustable parameter value is different because of product (kerosene or diesel oil) and quality index (solidification point or pour point).
4-4-2Coal freezing point of navigating TfzReal-time calculating：
Ti ep=boat coal the end point of distillation or solidification point；Adjustable parameter；
Tfz0=zero adjusts.
4-4-3Navigate coal or Flash Point of Diesel Tfs
Wherein：For adjustable parameter；Tfs0It is adjusted for zero；
Fd=stripper stripped vapor flow；Or the heat flow that stripper provides.
4-5Assay sampled point product quality instantaneous value calculates：
Through locating in what dynamic change, the product quality difference what product fractionating column of assay sampled point distillates a little fractionating column
Product quality, real-time control and material property change are required for distillating product quality a little using fractionating column product, to compare
What observation calculating provided distillates a little with sampled point product quality, and the real-time calculated value for providing sampled point product quality is as follows：
Sampled point product quality calculated valueIt is compared with same time sampling assay value, when the two deviation is larger, is
Adjust the parameter foundation in each product quality calculating formula.
Embodiment 8
5, petroleum fractionator feedstock property observer:
5-1The real-time observation of each product form in raw material
When the raw material of petroleum fractionator is the reaction product of reactor, the composition of petroleum fractionator raw material is exactly reaction production
The composition of object, instantaneous value is controlled reactor and real-time optimization is very important.
The product quality instantaneous value that the product flow instantaneous value and claim eight that claim five provides provide, is real-time
It calculates product form in raw material and provides real time data, the present invention is further following in product form in calculating raw material in real time
Practical problem:
5-1-1Product flow under standardized product quality：When petroleum fractionator is run, to ensure qualified product, production
Quality and standardized product quality are constantly present deviation, be based on standardized product quality in product form in calculating raw material
It calculates, for this purpose, need to be the flow under standard quality index by actual product flow rate conversion, the present invention provides following algorithm：
Wherein：
The respectively standard value of the jth product end point of distillation and initial boiling point；
The respectively observation of the jth product end point of distillation and initial boiling point；
ξj=initial boiling point correction factor.
5-1-2The real-time calculating of product form percentage in raw material
Flow under each product standard quality of petroleum fractionator has time lag and dynamic response to material composition change, to the
J products, relationship are calculated with following dynamic relationships：
Wherein：
τ0jFlowing time of=raw material oil stream amount the measuring point to jth product extraction point；
WjThe amount of savings of jth product in=tower.
The product form of raw material is indicated with the percentage of product in the feed：
The real-time calculated value of each product form has different lag time and dynamic response.Obviously, overhead product is to original
The variation of material is lagged with maximum duration, about 2 minutes or so.Time lag value can be obtained by fractionating column real-time recorded data.
5-2The real-time measurement of tower section vapour phase feed properties
To obtain the variation of feedstock property as early as possible, the real-time distillation characteristic coefficient of oil product is provided using (4-9) formulaWith
Following result of calculation is weighed：
Rated value
See (4-5), (4-6) formula
Increase, shows that the vapour phase oil product into tower section becomes weight.
Claims (5)
1. a kind of real-time observer of petroleum fractionator operation conditions, it is characterised in that：
1-1 by actual measurement variable timely collection device, come in and go out flow observer, tower internal loading observer, product quality observer,
Feedstock property observer, result of calculation display storage are formed with output processor sequence, and institute is functional in distributed computer control
It is realized on system DCS processed, every the real-time freshness value in the time less than or equal to 20 seconds, providing no measured value variable；
1-2 is calculated in real time according to the dynamic material balance and thermal balance of fractionating column and its relevant device, that is, consider material with
The variation of thermal reservoir amount, online real-time computing technique are as follows；
xi, Ci=i-th state variable and its capacity, the capacity containing equipment and material；
T=current timesIt is recommended that TS≤ 20 seconds；
X (t), x (t-TS) be current and the previous cycle moment it is filtered after state variable value；If state variable is without measured value,
Using its observation；
1-3 is carried out the real-time observation calculating of tower internal loading by tower section according to the ornamental of actual capabilities：Provide the vapour of disengaging tower section
The instantaneous value of phase and liquid phase oil product flow, and on this basis, calculate the instantaneous value of product quality and feedstock property, be also erosion control
Tower, liquid-leakage preventing, anti-liquid flooding, anti-dry plate, anti-evacuation and unusual service condition provide real time information；
1-4. product quality observers：According to oil and gas partial pressure compensation temperature, the real-time distillation characteristic of oil product and tower internal loading, tower is provided
The instantaneous value on top and each sideline product quality, real-time monitoring and control to realize product quality provide foundation；
1-5. feedstock property observers：It provides and flows into each tower section vapour phase material property change real time information；If raw material is from chemistry
Reactor provides the real time information of reactant product form, the foundation for controlling and optimizing as reactor.
2. the real-time observer of petroleum fractionator operation conditions according to claim 1, it is characterised in that：Based on relevant device
Dynamic characteristic, real-time calculating of the inflow and outflow column plate without measured value flow：
2-1 tower tops distillate vapor-phase product flowObservation calculates as follows in real time：
T=current times
Ptop=actual measurement tower top separation pressure tank Ts=calculating cycle
Tower top distillates gasoline or naphtha product flowInstantaneous value calculate it is as follows：
When tower top knockout drum is sleeping tank, AoIt is the function of liquid level
ρo=liquid-phase product severe TS=calculating cycle≤20 second
The total flow that tower top distillates the oil product in vapour phase is：
2-2：Side line distillates the real-time calculating of product flow
The characteristics of observation calculates is to consider product dynamic savings variable quantity in sideline product stripper
Wherein：J=sideline product serial numbers, usually sort from up to down
ρj, Aj=product severe and stripper sectional area
2-3：Into atmospheric tower lowest level column plate phase feed flow
Atmospheric tower bottom of tower flow enters the real-time of the gas phase flow rate of rectifying tower section lowest level plate according to materials at bottom of tower EQUILIBRIUM CALCULATION FOR PROCESS
Value：
Wherein：F0(t)=actual measurement current time is worth after entering the filtering of tower raw material oil stream amount；
Fb(t) it is worth after=actual measurement current time bottom of tower extraction flow filtering；
F1(t)=actual measurement current time lowest level column plate is worth after flowing into the filtering of bottom of tower flow；
Lb(t) it is worth after=actual measurement current time bottom of tower liquid level filtering；
Lb(t-TSValue after)=actual measurement previous moment bottom of tower liquid level is filtered；
ρbThe severe of=bottom of tower oil；Ab=bottom of tower liquid level sectional area；
2-4：Into the observation of catalytic cracking unit main fractionating tower lowest level plate vapour phase flow and reaction product flow, vapour-phase reaction
Product enters fractionating column from bottom of tower, upwards through herringbone plate washer, by returning the recycle oil of bottom of tower and above returning after tower cycle slurry oil takes heat, shape
At the vapour phase raw material flow V for entering first layer rectifiying plate0, but V0With reaction product flow F0Without measuring point, by materials at bottom of tower and
Heat dynamic equilibrium calculation：
Collapser material balance：V0=F0+F2-Fb (2-7a)
Materials at bottom of tower balances：
∴
F2=recycle oil returns bottom of tower flow F3Extract slurry oil flow out in=bottom of tower
Lb=bottom of tower liquid level Ab,ρb=bottom of tower sectional area and oil product severe
Herringbone plate part thermal balance:
Cex,T6=collapser and tower wall thermal capacity and temperature
QR(t)=F4[h(T7)-h(T4)]=above return tower cycle slurry oil take heat
H (T), the vapour phase enthalpy of oil product and liquid phase enthalpy when h (T)=temperature is T
Simultaneous solution (2-7b) and (2-8) formula, you can obtain V0And F0Instantaneous value；
2-5：Observation into delayed coking unit main fractionating tower reaction oil gas flow and the vapour phase flow of lowest level column plate calculates
Delayed coking unit main fractionating tower underflow journey
It is calculated by materials at bottom of tower and heat dynamic equilibrium：
Material balance：V0=F2+F0-Fb (2-9)
ρb, AbThe respectively severe of bottom of tower liquid phase oil product and bottom of tower sectional area
Lb=bottom of tower liquid level measured value F2, F3
F5=into coking furnace raw material flow measured value F4=freshening oil stream amount measured value
Thermal balance：By heat Balance Calculation F0=enter fractionating column pyrogenetic reaction product flow：
Qw=F6[Hw(T0)-Hw(T2)]=water vapour brings heat into
By (2-9) (2-11) formula：
Wherein：
H (T), vapour phase enthalpy of h (the T)=oil product when temperature is T, liquid phase enthalpy.
3. the real-time observer of petroleum fractionator operation conditions according to claim 1, it is characterised in that：Vapour-liquid phase load in tower
Real-time observation calculate：
Tower internal loading refers to liquid-phase reflux flow and vapour phase oil product flow in the tower that can not be surveyed；
Tower internal loading is calculated by tower section, there is following characteristics：
3-1 tower sections divide and ornamental：All adjacent trays that circulating reflux takes heat to include are a tower section, sideline product extraction
Column plate and thereon several layers of column plate are a tower section；Ornamental requires：Vapour phase oil product and the disengaging for passing in and out each tower section are each
There is tower section liquid phase oil product temperature point, circulating reflux to take heat flow with temperature and the liquid phase oil product flow and temperature that are added into tower
Degree has measured value；
3-2 tower section material and heat balance formulas
Tower section material balance ignores the variation of material amount of savings：The tower section serial numbers of i=from bottom to top
Tower section thermal balance：
Containing vapour phase oil product and tower wall between each laminate and its liquid phase oil product and two layers of column plate in tower section
Accumulated heat variable quantity,
H (T), h (T)=it is respectively vapour phase enthalpy of the oil product when temperature is T, liquid phase enthalpy
3-3 is by the 1st tower section each tower section vapour-liquid phase load of piecewise recurrence calculation upwards
According to the first tower section vapour phase flow V of inflowi-1=V0With flow downward out the first tower section liquid phase flow L1There is any discrepancy, and flow is seen
Survey instantaneous value or measured value that device provides, the recurrence calculation by i=1：
Return flow L in calculating firsti+1, by (3-1) (3-3) formula, export following calculating formula：
Wherein：
For liquid phase oil product specific heat at constant pressure under corresponding mean temperature；
HV(T) the latent heat of vaporization of=oil product when temperature is T；
See (3-3) formula explanation；
Subscript "+" indicates to press tower section serial number recurrence calculation；
The vapour phase flow for calculating outflow tower section again, according to mass balance type：
Piecewise recurrence calculation, until tower top section；
It also can first step calculating vapour phase oil product flow Vi, the interior return flow L of second step calculatingi+1；
3-4 is by tower top section downward recurrence calculation paragraph by paragraph
Tower top is provided by discrepancy flow observer and distillates vapour phase flow and the tower top cold reflux flow of inflow, from tower top section paragraph by paragraph to
Lower recurrence calculation：
Tower section lowest level plate efflux phase flow rate is calculated first takes heat flow without circulating reflux：
HV(T):See (3-4a) formula explanation；
As defined above, subscript "-" indicates to calculate V again from the downward recurrence calculation of tower top sectioni-1
Also V can first be calculatedi-1, then be calculated by (3-1) (3-2) formulaAnd Li；
The real-time calculating of 3-5 tower section accumulated heat variable quantities：
Gas phase oil product and tower casing accumulated heat variable quantity on 3-5-1 sections of top layer plates：
TS=observation calculating cycle ni=the i-th tower section column plate quantity or top layer plate serial number
3-5-2 tower sections top layer plate liquid phase oil product and column plate accumulated heat variable quantity：
Usually without measuring point, but：
Vi,Fi w=it is tower section outlet gas phase oil product flow and steam rates respectively
There was only top plate liquid phase temperature in (3-8) formulaIt is unknown, therefore have：
(3-9) formula is substituted into (3-7) formula to get top layer plate liquid phase and column plate accumulated heat variable quantity；
3-5-3 lowest level plate liquid phase oil product accumulated heat variable quantities, observed temperature areTherefore：
If lowest level plate liquid phase flows out after oil sump tank, and temperature point is exported in oil sump tank,
It then need in real time be calculated and be provided by oil sump tank dynamic modelObservation：
Ti b(t)=oil sump tank temperature measured value
Gas phase accumulated heat variable quantity on 3-5-4 tower section lowest level plates：
WithThere is measured value, it will be assumed thatInitial value, with actual measurement variable and (3-12) formula carry out recursion meter
It calculates, makes after suitable calculating cycleApproach its true value；Dynamic accumulated heat variable quantity is calculated as follows again；
3-5-5 tower section accumulated heat variable quantities
niThe quantity of column plate in=the i-th tower section
3-6 fractionating column operating conditions transfinite or damage judges and alarm
The i-th tower sections of 3-6-1 outflow gas phase oil product linear speed calculates in real time：
Vi, Fi w=it is respectively the i-th tower section outlet gas phase oil product flow and steam rates kg/h
Ai=the i-th tower section sectional area m2 P0Absolute pressure under=standard state
The lower i-th section of gas phase oil product of atmospheric pressure, the severe kg/m of water vapour3
Ti, Pi=the i-th tower section exports observed temperature DEG C and absolute pressure
Operation conditions pre-warning signal in 3-6-2 towers
The super bound of tower section vapour phase linear speed：Rush tower and leakage early warning
The interior super bound of return flow：Liquid flooding, dry plate and evacuation early warning；
3-6-3 unusual service conditions judge：When there is following situations, abnormity early warning signal is provided：
The phase temperature differenceSuper bound；
Pass in and out tower section vapour phase difference in flow (Vi-1-Vi) super bound；
Pass in and out the poor (L of return flow in tower sectioni-Li+1) super bound；
The a certain variable of tower section has significant change, and other variables are without significant change.
4. the real-time observer of petroleum fractionator operation conditions according to claim 1, it is characterised in that：The reality of product quality
When observation calculate
One of 4-1 Factors Affecting Product Qualities：Oil gas divides compensation temperature
4-1-1 oil and gas partial pressure compensation temperature is calculated as follows：
J=0 is overhead product, and j=1,2,3,4 be one, two, three, four, sideline product
It is divided for overhead vapor phase oil product temperature and product
To sideline product, extracts the temperature of vapour phase oil product under layer out for product and divided with product；
PaIt is absolute pressure that=air die pressing product, which divides unit,
The instantaneous value of 4-1-2 products partial pressure calculates
J=0,1,2,3,4 is respectively tower top and side line liquid-phase product serial number；
Lj=jth product extracts the interior return flow of layer out；
Fwi,Mw=jth product extracts steam rates and stream molecule amount under layer out；
The flow observer that respectively comes in and goes out provides each product flow and each molecular weight product；Real-time distillation characteristic coefficient is with temperature
Variation relation be：
The two of 4-2 Factors Affecting Product Qualities：Real-time distillation characteristic and oil property
The real-time distillation characteristics of 4-2-1 are under fractionating column actual operating state, and temperature and liquid phase oil product evaporating capacity relationship are with temperature
Abscissa, evaporating capacity are ordinate, indicate oil property；
Evaporating capacity uses unit of weight, and it is unit of weight not only to adapt to the flow value provided when production process operation often, is also changed
The slope of distillation characteristic, temperature is higher, the severe for vaporizing oil product increases therewith, and distillation characteristic slope increases, convenient for weighing oil
Product change of properties；
If within the scope of boiling point 10-90%, the distillation characteristic coefficient of evaporating capacity is measured for 1, in terms of weight flow with volume flow
When measuring evaporating capacity, if the severe of vaporization oil product is directly proportional to vapourizing temperature, real-time distillation characteristic coefficient variation with temperature relationship
For：
To gasoline：Diesel oil：
4-2-1 calculates reflux in tower amount L by real-time distillation characteristici+1Evaporating capacity in the i-th tower section：
aR,bR=adjustable parameter
It is the real-time boiling range characteristic coefficient for entering the i-th tower section and adding oil product, boiling spread and initial boiling point respectively
4-2-2 enters tower section vapour phase oil distillation characteristic coefficientOnline real-time calculating
Vi 0=enter the i-th tower section vapour phase oil product in not condensing flow
Numerical value increases, and the vapour phase oil product for indicating entry into tower section becomes weight, is a factor for influencing the product end point of distillation；By (4-
5) (4-9) (4-10) formula can be calculated
The online real-time calculating of the 4-3 product end points of distillation：
In addition to factors above, influence of the vapour phase load to product quality in tower is considered：
4-3-1 fractionating columns evaporate the real-time calculating of the exit product end point of distillation：
Or 90% point or 95% point
See (4-1)-(4-3) formula；
For adjustable parameter；For zero adjusting parameter；
Simplifying for the 4-3-2 end points of distillation calculates
Petroleum fractionator transports the not big variation of state, and following simplified formula can be used：
It is the adjustable parameter being calculated by rated value；
For zero adjusting parameter；
The online real-time calculating of 4-4 other products quality
4-4-1Navigate coal or diesel oil pour point TppOr the calculating of solidification point
CppFor adjustable parameter；Tpp0For zero adjusted value；
Adjustable parameter value is different because of product kerosene or diesel oil and quality index solidification point or pour point；
4-4-2Coal freezing point of navigating TfzReal-time calculating：
Ti ep=boat coal the end point of distillation or solidification point；Adjustable parameter；
Tfz0=zero adjusts；
4-4-3Navigate coal or Flash Point of Diesel Tfs
Wherein：For adjustable parameter；Tfs0It is adjusted for zero；
Fd=stripper stripped vapor flow；Or the heat flow that stripper provides；
4-5Assay sampled point product quality instantaneous value calculates：
For adjustable parameter；
Sampled point product quality calculated valueIt is compared with same time sampling assay value, when the two deviation is larger, adjustment is each according to this
Parameter in product quality calculating formula.
5. the real-time observer of petroleum fractionator operation conditions according to claim 1, it is characterised in that：Petroleum fractionator is former
Expect the real-time observation of property:
The real-time calculating of product yield under 5-1 standard qualities
Wherein：
The respectively standard value of the jth product end point of distillation and initial boiling point；
The respectively observation of the jth product end point of distillation and initial boiling point；
The real-time calculating of product form percentage in 5-2 raw materials
Fractionating column product variations are with dynamic response, relationship caused by raw material composition variation：
Wherein：
τ0jFlowing time of=raw material oil stream amount the measuring point to jth product extraction point；
WjThe amount of savings of jth product in=tower；
The percentage of each product in raw material:
The real-time measurement of 5-3 tower section vapour phase feedstock characteristics
See (4-5), (4-6) formula
Increase, shows that the vapour phase oil product into tower section becomes weight.
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