CN1422324A - Method and system for controlling a fluid catalytic cracker - Google Patents
Method and system for controlling a fluid catalytic cracker Download PDFInfo
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- CN1422324A CN1422324A CN01806551A CN01806551A CN1422324A CN 1422324 A CN1422324 A CN 1422324A CN 01806551 A CN01806551 A CN 01806551A CN 01806551 A CN01806551 A CN 01806551A CN 1422324 A CN1422324 A CN 1422324A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0033—Optimalisation processes, i.e. processes with adaptive control systems
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00168—Controlling or regulating processes controlling the viscosity
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00186—Controlling or regulating processes controlling the composition of the reactive mixture
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- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N24/00—Investigating or analyzing materials by the use of nuclear magnetic resonance, electron paramagnetic resonance or other spin effects
- G01N24/08—Investigating or analyzing materials by the use of nuclear magnetic resonance, electron paramagnetic resonance or other spin effects by using nuclear magnetic resonance
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- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N24/00—Investigating or analyzing materials by the use of nuclear magnetic resonance, electron paramagnetic resonance or other spin effects
- G01N24/08—Investigating or analyzing materials by the use of nuclear magnetic resonance, electron paramagnetic resonance or other spin effects by using nuclear magnetic resonance
- G01N24/085—Analysis of materials for the purpose of controlling industrial production systems
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- G—PHYSICS
- G01—MEASURING; TESTING
- G01R—MEASURING ELECTRIC VARIABLES; MEASURING MAGNETIC VARIABLES
- G01R33/00—Arrangements or instruments for measuring magnetic variables
- G01R33/20—Arrangements or instruments for measuring magnetic variables involving magnetic resonance
- G01R33/44—Arrangements or instruments for measuring magnetic variables involving magnetic resonance using nuclear magnetic resonance [NMR]
- G01R33/46—NMR spectroscopy
- G01R33/4625—Processing of acquired signals, e.g. elimination of phase errors, baseline fitting, chemometric analysis
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- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Automation & Control Theory (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Feedback Control In General (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A method for controlling the output of a distillation tower fed by a fluid catalytic cracker uses one or more NMR sensors to obtain on-line measurements of values of selected properties of feedstock and/or of distillation tower outputs. The measured values are provided to a multivariate controller. On the basis of the measured values and setpoint information provided by an optimizer, the multivariate controller determines values of manipulated variables for controlling the catalytic cracker to produce products of desired qualities and maximize unit economic return.
Description
Background of invention
The present invention relates to the refining of petroleum field, be specifically related to the system that the petroleum fractions of distillation tower production is controlled.
Crude oil also claims oil, is a kind of hydrocarbon mixture of complexity.In order to produce the petroleum products of commercial value, come the part hydro carbons is separated from one another.Become the various physics of part hydro carbons and chemical process step to be generically and collectively referred to as " refining " crude separation.
Because each hydrocarbon component volatility difference, making its effective ways separated from one another is fractionation.This method is injected a distillation tower that thermograde is arranged in it with the oil of heating, and the distillation tower temperature is from reducing to low temperature by high temperature gradually to cat head at the bottom of the tower.Pass distillation tower by the oil vapour rising that each hydro carbons of its vapour phase becomes to be grouped into.Meet with lower temperature thereon when rising gradually.When temperature equaled a certain height of the coagulation temperature of this steam composition in the oil vapour arrival distillation tower, this composition promptly condensed.Promptly collect the hydrocarbon component that these are condensed at the tower tray that this height of tower is provided with.
Each petroleum fractions relative quantity of distillation tower output depends on the composition of this oil to a great extent.The oil refining worker is restricted the composition control of any various oil of being processed.The oil refining worker must often process those capital stock crude oil or process those crude oil that tempting conclusion of the business may provide according to short-term or spot market.Therefore, the ability of regulating different petroleum fractions productive rates with distillating method is restricted.In addition, lamp all being surpassed these usually with demand oily, the cleaning oil product only can be by the naturally occurring oil product quantity of distillation recovery in crude oil.
When just beginning petroleum refining industry to occur, the electric lighting deficiency causes the petroleum fractions demand of combustion cleaning lam-oil such as kerosene very big.But,, be cost and significantly increasing to reduce heavier petroleum fraction such as kerosene to the demand of low-density oil cut such as gasoline along with the appearance of oil engine.For this reason, the method that increases gasoline yield from various oil has been developed in petroleum refining industry.Catalytic cracking is exactly a kind of method wherein.
In catalytic cracking, will be heavier than gasoline, the petroleum fractions that is commonly called gas oil adds in the reaction chamber, makes it be vaporizated into hydrocarbon vapour under the high-temperature very much.The spherolite that will contain the firing silicate material of catalyzer is introduced in this hydrocarbon vapour.The catalyzer spherolite that high velocity vapor stream orders about this firing silicate material enters reaction chamber, and it is dispersed in the hydrocarbon vapour fully.The catalyzer that is carried by spherolite has promoted hydrocarbon molecule to be decomposed into light molecule or " cracking " is the chemical reaction than light molecule.These lighter molecules are transferred in the distillation tower by a so-called main fractionating tower and are reclaimed.Because this steam comprises some light hydrocarbon molecules now, through will output other gasoline of distillation and other light hydrocarbons.
Hydrocarbon steam cracking depends in part on hydrocarbon composition and its feeding rate that reaction chamber is provided for the degree of lighter molecules.
In the ordinary method of control catalytic cracking unit operation, adopt charging and product stream periodic sampling and the method for in the laboratory, sample being tested, finish gas oil is formed and from the mensuration of the finished product of main fractionating tower.But this method is costliness but also consuming time not only.The result is difficult to carry out frequent laboratory and detects, and can not obtain abundant relevant charging and by the currency of the selected quality parameter of whole cuts that hydrocarbon mixture produces after the cracking.Therefore, it is not good that this currently known methods causes catalytic cracking process control.
Summary of the invention
The inventive method has overcome the defective of this technology to the method for the selected performance number implementation on-line determination of one or more related hydrocarbon materials of catalytic process.In an example, these materials are the material that is added to catalytic cracking unit, i.e. charging.In another example, these materials that relate to this catalytic process are cuts of at least a main fractionating tower institute output by the fluidized catalytic cracker feed.With these online detected results, the expected value with the selected performance of tested material offers a two-position controller.Measure this controller according to these and calculate the controlled process variate-value, offer fluidized catalytic cracker, to obtain to meet the output cut of selected performance expectation value.Because estimate online carrying out, it is rapid to the variation response of tested material to adopt system of the present invention.
In the most embodiment of the present invention, guarantee two kinds of mensuration, and, be considered to preferred according to two groups of variablees of measuring control process to gas-oil feed and output finished product.But feature of the present invention can extend to the occasion that gas-oil feed is only measured in implementation, or only measures the occasion of one or more output cuts, and regulates one or more controlled process variablees according to this mensuration.According to mensuration regulate process variable, carry out feed forward control and, carry out feedback control according to mensuration regulate process variable to finished product materials to gas-oil feed.
A preferred embodiment of the present invention adopts the nuclear magnetic resonance measuring that combines with the performance number of selected material such as gas-oil feed or one or more finished product cuts.Nuclear magnetic resonance measuring does not rely on optical radiation or ir radiation, therefore is not subjected to the influence of high opaqueness.In addition, nuclear magnetic resonance measuring is as the function of temperature, and is more stable.Therefore, all can measure reliably the gas-oil feed of wide temperature range and the various product cuts of main fractionating tower institute output.
An illustrative embodiment of the present invention comprises the step that the related material of catalytic process such as institute's output hydrocarbon-fraction are applied stabilizing magnetic field.Because stabilizing magnetic field in position, nucleus magnetic resonance (NMR) transmitter produces magnetic field in a flash to this cut, and measures its response to transient magnetic field.Nmr sensor does not generally directly provide the numerical value to the selected performance of cut, and the chemical constitution of cut is provided.Therefore, the inventive method comprises according to the survey step of forming definite material performance value of surveying.Then, utilize optionally control process variable of these numerical value, enter flow rate, revivifier catalyst slide valve position, the reactor dense bed position of fluidized catalytic cracker such as gas oil, revivifier pressure, feeding preheating temperature, air or oxygen blast speed, reactor/regenerator pressure reduction, wet gas compressor suction pressure, main fractionating tower finished product are extracted speed, steam rate of injection, trim the top of column growing amount, overhead product set jar emptying out, are reached the slurries of devaporation producer, thereby produce the product cut that meets selected quality parameter expected value.The concrete configuration of each fluidized catalytic cracker is depended in the accurate set that is fit to the process variable of control.The example of these selected quality parameters comprises aromaticity, boiling point, flash-point, cloud point, viscosity, pour point, api gravity, zero pour, octane value, PIONA value, Reid Vapour Pressure (RVP) and other chemistry or physicals.
According to the present invention, the information that is obtained by nuclear magnetic resonance measuring can be used for transformation efficiency in the obvious controlling flow fluidized catalytic cracking unit and the selectivity of device reaches aspiration level.This embodiment of the present invention relates to the nuclear magnetic resonance measuring to the material that directly relates in the catalyzed conversion, and make measure become online and real-time substantially.
The quality of purpose product is generally by the market competitiveness, legislations of environmental protection and comprise economic factorss such as charging, product price and productive expense and definite.They also may be subjected to the restriction that refinery comprises device configurations and concrete feature such as validity and operational constraints.
Therefore, the inventive method can and be produced each cut to main fractionating tower and select the numerical value of performance The real time measure is provided gas-oil feed.These The real time measure can make the hierarchy of control of the present invention adjust the operation of catalytic cracking unit rapidly, the fluctuation that compensation charging and/or main fractionating tower occur.Because of the inventive method is based on the nucleus magnetic resonance non-optical, technologies, so the accuracy of these mensuration is irrelevant with the opaqueness or the temperature of tested material basically.
Implement system of the present invention and comprise an optimizer, be used to stipulate the permanent expected value of selected fluidized catalytic cracker operational variable, produce the product of desirable quality, take into account wherein charging and process cost and the output value simultaneously this device economical operation is carried out optimizing.This optimizer has also been considered the concrete feature of refinery, comprises device formation, validity and comprises product production ultimate operational constraints.
Implement the transmitter that system of the present invention further comprises a selected product performance value of estimation.These estimated values are offered a controller with the permanent expected value of selected operational variable by this optimizer regulation.This controller, according to these numerical value that come transmitter since then, product performance expected value with from the permanent expected value of optimizer, the necessary operational variable of product that formation is met selected performance expectation value determines currency, and the economic performance to refinery especially catalytic cracking unit carries out optimizing simultaneously.
Embodiment of the present invention also comprise with nucleus magnetic resonance directly to be measured the relevant composition parameter that relates at least a material in the petroleum chemistry process catalytic converter or material, and institute's measurement information is offered the controller of petroleum chemistry process.The material of surveying or material can be a kind of composition of charging or charging, and can be the cut of one or more petroleum chemicals.Preferred embodiment is that charging and product both are measured.This controller is according to an institute's measurement information and a further target information of the relevant expectation of the petrochemical process of storing or accepting parameter, comprise produce or related material, the control signal of decision regulate process is with the set point value of institute's measurement information of reaching relevant target information.
Description of drawings
According to the following detailed description and the accompanying drawings, these and other feature of the present invention and advantage all can be clearly, wherein:
Fig. 1 is the schematic block diagram that embodies a kind of multivariate distillation hierarchy of control of feature of the present invention;
Fig. 2 is the schematic block diagram that shows Fig. 1 distillation system details; And
Fig. 3 is the schematic block diagram that shows according to another distillation system of the present invention.
The description of illustrative embodiment
Fig. 1 shows a kind of multivariable control system 10 that adopts the principle of the invention.This multivariable control system 10 comprises a petroleum chemistry cracking system 12, and it is accepted charging and is communicated with multivariable controller 14 with the signal liaison method.The output products of cracking system 12 comprises each many hydrocarbon products with selected performance numerical representation method.These numerical value of representing with the output vector y that feeds back to multivariable controller 14 in Fig. 1 all are the controlled variablees of this multivariable control system 10.
Shown in the validity of controller 14 also by it being provided input vector z be enhanced, input vector z represents to characterize the selected performance number of input gas-oil feed.Multivariable control system 10 comprises an optimizer 16, is used for the selected operational variable of producing purpose product quality is formed permanent expected value, simultaneously economical operation is carried out optimizing.These expected values represent with set(ting)value vector r that in Fig. 1 set(ting)value vector r is produced by optimizer 16, and is provided for multivariable controller 14.Stipulate vectorial r element, the concrete feature of refinery of wherein having taken into account charging and process cost, product economy value and having comprised device configurations, validity and comprise the operating limit constraint.
Fig. 2 shows, shown in cracking system 12 comprise an intake pipeline 18 that leads to reaction chamber 20.Pump 33 connects input channels 18, orders about the gas-oil feed mixture and passes control valve 26 and enter reaction chamber 20, and control valve 26 is opened and closed by valve acutator 28 under the control of multivariable controller 14.Reaction chamber 20 also is communicated with regeneration room 32 fluids by catalyst charge pipe 34 and catalyzer fairlead 36.This regeneration room 32 is provided with 38 and venting ports 40 of air or oxygen inlet, is used for catalyst regeneration process.Control valve 22 in the catalyst feed pipeline 34 is subjected to valve acutator 23 controls according to the control signal action of controller 14 inputs.Red-hot regeneration firing silicate material catalyst particle from regeneration room 32 by catalyst charge pipe 34, was added to before reactor chamber 20 in the gas-oil feed in the riser tube.The heat of granules of catalyst causes the gas-oil feed vaporization, and gained high velocity vapor stream delivery granules of catalyst enters reactor chamber 20.
Nucleus magnetic resonance (NMR) transmitter 42 links to each other with the different select segments of cracking system 12, to measure the chemical property of this process select segment material.Transmitter 42 shown in Figure 2 links to each other with input channel 18, with to charging sampling, and distillates a mouthful 31a-d with each tower and links to each other, samples with each product or cut to main fractionating tower 30 outputs.Although cracking system 12 shown in Figure 2 has only a nmr sensor 42, for example, its each bull input is responded by time sharing system, obviously still can provide one or more other nmr sensors that each sampling material is responded.Heat transfer agent by nmr sensor 42 outputs is provided for calibrator 44, and calibrator 44 is transformed to the form that is fit to multivariable controller 14 with it.
A kind of preferred sensor adopts the technology of I/A Series Process (I/A series technology) nuclear magnetic resonance equipment, by the Foxboro Company (Foxboro of company, Massachusetts) provide, still, also can use various nmr sensors to carry out chemical analysis.
Preferably a kind of stoichiometry analogue unit of suitable calibrator.Calibrator 44 and suitable enforcement stoichiometry analogue unit of the present invention have been assembled a kind of digital processing unit, and stoichiometric chemistry is carried out the valuation instruction to selected physicals per sample, and nmr sensor is determined as using.The well-known program of persons skilled in the art is carried out in these instructions.These programs comprise: formulate look-up table, carry out interpolation by look-up table between numerical value, and implement mathematical model selected performance is carried out valuation.For distinct, Fig. 3 is shown as a kind of independent component with calibrator 44, but also calibrator 44 can be integrated into arbitrary position of system software.
Optimizer 16 and multivariable controller 14 boths preferably are provided at the instruction of carrying out on the programmable digital treater with software.In one embodiment, these instructions are carried out on universal digital computer.Yet especially for satisfying the requirement of desired properties, application examples such as application specific integrated circuit can be in hardware, in the software or optimizer 16 and multivariable controller 14 be provided in combination of hardware.Implement suitable optimizer of the present invention and multivariable controller and be by Simulation Scienceof Brea (California, USA) company sells, its trade mark is respectively ROMeo
TMAnd Connoisseur
TMSpecifically giving particulars of multivariable controller 14 and optimizer 16 belongs to those of ordinary skills' known range, do not influence scope of the present invention.
In the operation of system shown in Fig. 1 and 2, pump 33 orders about gas-oil feed and passes control valve 26, enters reaction chamber 20.Add on a small quantity red-hot spherolite by catalyst charge pipe 34 and guiding valve 22 simultaneously from the catalyst feed of regeneration room 32.The heat of this granules of catalyst causes the gas-oil feed vaporization, and gained high velocity vapor stream orders about granules of catalyst and enters reaction chamber 20.This catalyzer generally belongs to a kind of firing silicate material, such as zeolite (Zeolyte).But known some other catalyzer also can be used in combination in fluid catalytic cracking.Existence at reaction chamber 20 inner catalysts has promoted the covalent linkage of gas oil mixture molecule to rupture, and produces low-molecular-weight hydro carbons.
Carbon in the burning-off revivifier 32 on the catalyzer produces heat.This heat is transferred in the reactor through catalyst charge pipe 34, and the heating gas-oil feed reaches that to be enough to make the gas oil catalytic cracking be the temperature of lighter molecules.This just causes producing the vapourous mixture of generally low than the fed hydrocarbon many hydro carbons of its molecular weight.The vapourous mixture of these low molecular weight hydrocarbons flows into main fractionating tower 30 and is separated into multiple product.These products Figure 2 shows that by a plurality of mouthful outflow main fractionating towers that distillate of this tower four distillate mouth.
The by product of cracking process is the carbon laydown on the catalyzer spherolite.These carbon laydowns have been contained the interaction between catalyzer and gas oil steam, thereby have reduced the efficient of catalyzer.Its result, granules of catalyst is constantly drawn from reaction chamber 20, purges through catalyzer downstream line 36, returns regeneration room 32.Inject air or oxygen by intake 38, the carbon on the burning-off catalyzer spherolite recovers catalytic activity, and the generation heat is kept this cracking process.The gaseous by-product of regenerative process is discharged from regeneration room through venting port 40.
As mentioned above, shown in nmr sensor charging is sampled, also from the sampling of the 30 pairs of products of main fractionating tower.42 pairs of each samples of nmr sensor apply a stabilizing magnetic field, aim at the magnetic dipole moment with the sample associated molecule.Because stabilizing magnetic field in position, nmr sensor 42 produces magnetic field in a flash, and its direction is different from and is preferably perpendicular to this stabilizing magnetic field.This transient magnetic field is temporarily aimed at its direction and is different from the sample dipole that the dipole direction is aimed in this static-magnetic place.When cutting off this transient magnetic field, this sample dipole rebounds and by stabilizing magnetic field the aligning that it produced is located.Just because of this, this dipole has produced a RF (radio frequency) signal.The concrete dipole localized speed of stabilizing magnetic field of rebounding, and the frequency of consequent RF signal all are the features of this sample molecule structure.Gained RF spectrogram is exactly the response that this sample chemical is formed, thus a kind of method that provides definite sample chemical to form.
Therefore, this nmr sensor provides the material of directly relevant cracking system 12 process-streams or the chemical constitution information of material.As described, these materials comprise formed cut in charging and the main fractionating tower 30.By the respective value of calculating its selected performance of forming that sample is surveyed, be known in this area.In Fig. 2 embodiment, it is to finish by being communicated with both calibrators 44 of multivariable controller 14 and nmr sensor 42 that institute test sample product are formed the operation that is transformed to selected performance numerical value.The input information of calibrator 44 is comprised chemical constitution by 42 test sample product of nmr sensor.The output of calibrator 44 is correspondence set of the selected performance measured value of one group of each institute's test sample product.These selected performances can comprise aromaticity, boiling point, flash-point, cloud point, viscosity, pour point, api gravity, zero pour, octane value, PIONA value, Reid Vapour Pressure (RVP), reach other chemistry or physicals.
The data that provided according to nmr sensor 42, with other routine data together, conventional and known as this area, such as data from other transmitter (not shown), as liquid level, pressure, pressure reduction, temperature, time and flow rate, the numerical value of multivariable controller 14 decision operational variables makes product quality expected value and corresponding selected product quality value differences reduce to minimum, as being provided by nmr sensor.Taken into account by controller 14 by the permanent expected value of the operational variable that optimizer 16 determined.Controller 14 utilizes means known in the art decision operational variable value.These methods comprise the mathematical model of using look-up table and implementation experience to derive.These operational variables comprise flow rate, revivifier catalyst slide valve position, reactor dense bed position, revivifier pressure, feeding preheating temperature, air or oxygen blast speed, reactor/regenerator pressure reduction, wet gas compressor suction pressure, main fractionating tower finished product extraction speed, steam rate of injection, trim the top of column growing amount, the overhead product set jar emptying of gas oil injection reaction chamber and remove to take place the slurries of steam.The concrete configuration of each fluidized catalytic cracker is depended in the accurate process variable set that is fit to operation.
After the decision operational variable value, multivariable controller 14 offers valve acutator 28 with control signal, disconnects more or less or closed control valve 26, to adjust the gas oil flow rate of injecting reaction chamber 20.Same signal also is transmitted controls other operational variables.
Because 44 pairs of multivariable controllers 14 of nmr sensor 42 and calibrator provide relevant process-stream information rapid, the response of the performance inconsistency of 14 pairs of chargings of this controller and distillate also can be quick.Can make controller 14 change the set(ting)value relevant like this with catalytic cracking process, reduce the difference between the performance of surveying and the corresponding expected performance.
Fig. 3 show a kind of nucleus magnetic resonance station 42 ', can be used for Fig. 2 system and replace nucleus magnetic resonance 42 among its figure.Shown in nucleus magnetic resonance station 42 ' a group of a plurality of nmr sensor 42a, 42a are arranged, each transmitter all is communicated with the information that receives relevant variant production sample.The input of each nmr sensor 42a, 42a is output 31a, the 31b... of tower separately among Fig. 2 all.Come the output signal of nmr sensor since then be provided for Fig. 2 in the interface selector switch 42b of multivariable controller 14 connection operations.Shown in interface selector switch 42b will offer calibrator 44 from the output of arbitrary selected nmr sensor 42a, it is generally the calibrator 44 of Fig. 2.
Also as shown in Figure 3, the station of nucleus magnetic resonance shown in this 42 ' another nmr sensor 42c is arranged, its output is provided for input selector 42b.Shown in nmr sensor 42c by sampling pipeline 43a and 43b and a may command selector switch 42d, receive from two kinds of information that feed sample is arbitrary.These two input line 43a and 43b only are the explanations for embodiment, and the invention process also can be used to from a plurality of products measure information with from the information of multiple feed sample.Shown in nucleus magnetic resonance station 42 ' also explanation, the invention process can receive from simple sample or any information from two or more material samples with one or more nmr sensors, and this depends on the best instrument collocation strategy that is used for concrete petrochemical conversions equipment.
The system configuration has illustrated chemical cracking technology described here as mentioned above.But various other configurations also can utilize these technology.
After having described a present invention and one preferred embodiment, the new scope that requires patent protection is as follows.
Claims (21)
1, a kind of control method that is equipped with by the petroleum chemistry cracking system of the distillation tower of catalytic converter feed, described method comprises step:
The handled at least a material of cracking system is carried out online nuclear magnetic resonance measuring, with definite measured value to the selected performance of surveyed material,
To the selected performance provision expected value of tested material, and
In order to control selected performance,, determine the numerical value of this cracking system operational variable according to selected performance measured value from least a output cut of distillation tower.
2, according to the process of claim 1 wherein that the described step of decision operational variable value comprises decision those obvious control cracking system transformation efficiency and selectivity, to reach the operational variable value of expected value.
3, according to the method for claim 1,
In this cracking system of the step measurements of wherein said implementation nuclear magnetic resonance measuring at least a feed material and
Wherein said deciding step determines this cracking system operational variable value of feed forward control at least.
4, according to the method for claim 1,
In this cracking system of the step measurements of wherein said implementation nuclear magnetic resonance measuring at least a output product material and
Wherein said deciding step determines this cracking system operational variable value of feedback control at least.
5, the equipment that distillation tower is controlled by the petroleum chemistry cracking system of catalytic converter charging, described equipment comprises
The nucleus magnetic resonance of a configuration (NMR) transmitter, be used to measure the handled at least a material of cracking system performance and
A multivariable controller that is communicated with described nmr sensor, mensuration-the response message that provides according to described nmr sensor, described multivariable controller produces the control signal that this cracking system operation is regulated, to obtain the expected value that at least a output cut reaches selected performance.
6, according to the equipment of claim 5, wherein
Described nmr sensor measure at least a charging of this cracking system performance and
Wherein said controller produces the control signal of feed forward control at least to this cracking system.
7, according to the equipment of claim 5, wherein
Described nmr sensor measure at least a output product material in this cracking system performance and
Wherein said controller produces the control signal of feedback control at least to this cracking system.
8, a kind of method that the petroleum chemistry process of its catalytic converter production petrochemical fraction is controlled, described process comprises step:
The online nuclear magnetic resonance measuring of relevant composition parameter is carried out at least a charging that drops into this petroleum chemistry process,
To carrying out the online nuclear magnetic resonance measuring of relevant composition parameter by at least a petrochemical fraction of catalytic converter output,
Measured information is offered a controller of this petroleum chemistry process,
The target information of the expectation parameter of identification this petroleum chemistry process at least a cut is offered this controller, and
According to measured information and target information, by the control signal of this this process of controller generation adjusting, to realize the set point value of the institute measurement information relevant with target information.
9, a kind of method to controlling by at least a output cut of the distillation tower of catalytic converter feed, described method comprises step:
Carry out following (i) and (ii) one of at least: (i) this petroleum chemistry charging of online nuclear magnetic resonance measuring, to determine the measured value of the selected performance of this charging, at least a output cut of (ii) online nuclear magnetic resonance measuring is with the measured value of the selected performance of determining described at least a output cut
Stipulate described at least a output cut selected performance expectation value and
For the measured value of the selected performance of controlling described at least a output cut, according to the measured value of selected performance, the numerical value of decision operational variable.
10, according to the method for claim 9, the step of the online nuclear magnetic resonance measuring of wherein said implementation comprises step:
Tested material is applied a stabilizing magnetic field,, and measure the response of tested material described of short duration magnetic field to the described stabilizing magnetic field of short duration magnetic field that superposes.
11, according to the method for claim 9, wherein said selected performance is selected from aromaticity, boiling point, flash-point, cloud point, viscosity, pour point, api gravity, zero pour, octane value, PIONA value, Reid Vapour Pressure (RVP).
12,, further comprise step according to economic condition regulation catalytic cracking unit operational condition according to the method for claim 9.
13, according to the method for claim 9, further comprise select described to comprise the step of one of following at least operational variable: the feed flow rates of described fluidized catalytic conversion device, revivifier catalyst slide valve position, reactor dense bed position, revivifier pressure, feeding preheating temperature, blow air or oxygen blast speed, reactor/regenerator pressure reduction, wet gas compressor suction pressure, main fractionating tower finished product extract speed, steam rate of injection, trim the top of column growing amount, an overhead product set jar emptying out, and to the slurries of vapour generator.
14,, comprise that further selection is described to comprise the step of the operational variable that forms this output cut temperature range according to the method for claim 9.
15, a kind of equipment in system for handling, controlling by at least a output cut of the distillation tower of catalytic converter feed, described equipment comprises:
The nmr sensor of a configuration is used in the mensuration system (i) and (ii) one of at least: (i) performance of petroleum chemistry charging and (ii) at least a output cut and
A multivariable controller that is communicated with described nmr sensor, mensuration-the response message that provides according to described nmr sensor, described multivariable controller produces the control signal of regulating this system for handling operation, to obtain the expected value to the selected various performances of at least a output cut of this system.
16, according to the equipment of claim 15, wherein this multivariable controller is accepted the one or more set(ting)values from optimizer.
17, according to the equipment of claim 16, wherein one or more set(ting)values comprise the numerical value of determining according to one of following at least: incoming charge, process cost, the product production limit and oil refinery equipment constitute.
18, a kind of system that is used to process petroleum chemicals, this system comprises:
A kind of petroleum chemistry cracking system, this system have at least one input channel and at least one of accepting gas-oil feed discharges by the pipeline of the charging of being accepted through the overhead product of catalytic cracking output,
A feedback control loop that is used to control this petroleum chemistry cracking system, this feedback control loop is accepted the signal from the nmr sensor of at least one configuration, to measure at least one output cut, this feedback control loop basis mensuration of nmr sensor is at least regulated this petroleum chemistry cracking system.
19, according to the system of claim 18, wherein feedback control loop is controlled this petroleum chemistry cracking system by stipulating following at least one parameter:
Hydrocarbon vapour enters flow rate, revivifier catalyst slide valve position, the reactor dense bed position of reaction chamber, and revivifier pressure, feeding preheating temperature, air or oxygen blast speed, reactor/regenerator pressure reduction, wet gas compressor suction pressure, main fractionating tower finished product are extracted speed, steam rate of injection, trim the top of column growing amount, overhead product set jar emptying out and removed to take place the slurries of steam.
20, according to the system of claim 18, wherein this petroleum chemistry cracking system comprises a distillation tower by the catalytic converter feed.
21, according to the system of claim 18, further comprise at least one nmr sensor, be configured in order to measure at least one performance of this gas-oil feed; Wherein this feedback control loop comprises that a basis regulates the feedback control loop of this petroleum chemistry cracking system to the mensuration of at least one nmr sensor of input charging.
Applications Claiming Priority (10)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US17634200P | 2000-01-14 | 2000-01-14 | |
| US60/176,342 | 2000-01-14 | ||
| US17876200P | 2000-01-28 | 2000-01-28 | |
| US60/178,762 | 2000-01-28 | ||
| US53198900A | 2000-03-20 | 2000-03-20 | |
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| US63361200A | 2000-08-07 | 2000-08-07 | |
| US63343900A | 2000-08-07 | 2000-08-07 | |
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| US09/633,612 | 2000-08-07 |
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| CN1422324A true CN1422324A (en) | 2003-06-04 |
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| CN01806551A Pending CN1422324A (en) | 2000-01-14 | 2001-01-12 | Method and system for controlling a fluid catalytic cracker |
| CN01806559A Pending CN1427877A (en) | 2000-01-14 | 2001-01-12 | Petroleum distillation method and system |
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| CN01806559A Pending CN1427877A (en) | 2000-01-14 | 2001-01-12 | Petroleum distillation method and system |
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| EP (2) | EP1254197A1 (en) |
| CN (2) | CN1422324A (en) |
| AU (2) | AU2001229408A1 (en) |
| CA (2) | CA2397566A1 (en) |
| WO (2) | WO2001051588A1 (en) |
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| CN101520645B (en) * | 2007-06-28 | 2013-06-19 | 霍尼韦尔国际公司 | Multivariable process controller and methodology for controlling a catalyzed chemical reaction |
| CN106353355A (en) * | 2015-07-15 | 2017-01-25 | 艾斯拜克特国际（2015）私人有限公司 | NMR-based system for crude oil lifting, and method thereof |
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| DE10121194A1 (en) * | 2001-04-30 | 2002-10-31 | Basf Ag | Device for controlling chemical synthesis processes |
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| US5580531A (en) * | 1995-06-07 | 1996-12-03 | Twenty-First Century Research Corporation | Devices for making reaction products by controlling transient conversion in an atomized liquid |
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- 2001-01-12 EP EP01942374A patent/EP1254197A1/en not_active Withdrawn
- 2001-01-12 CA CA002397566A patent/CA2397566A1/en not_active Abandoned
- 2001-01-12 WO PCT/US2001/001049 patent/WO2001051588A1/en not_active Application Discontinuation
- 2001-01-12 CN CN01806551A patent/CN1422324A/en active Pending
- 2001-01-12 AU AU2001229408A patent/AU2001229408A1/en not_active Abandoned
- 2001-01-12 CA CA002397555A patent/CA2397555A1/en not_active Abandoned
- 2001-01-12 WO PCT/US2001/001068 patent/WO2001051589A1/en active Search and Examination
- 2001-01-12 CN CN01806559A patent/CN1427877A/en active Pending
- 2001-01-12 AU AU2001230919A patent/AU2001230919A1/en not_active Abandoned
- 2001-01-12 EP EP01903049A patent/EP1257614A1/en not_active Withdrawn
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| CN101520645B (en) * | 2007-06-28 | 2013-06-19 | 霍尼韦尔国际公司 | Multivariable process controller and methodology for controlling a catalyzed chemical reaction |
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| US10655996B2 (en) | 2016-04-12 | 2020-05-19 | Aspect Imaging Ltd. | System and method for measuring velocity profiles |
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Also Published As
| Publication number | Publication date |
|---|---|
| CA2397555A1 (en) | 2001-07-19 |
| AU2001229408A1 (en) | 2001-07-24 |
| EP1257614A1 (en) | 2002-11-20 |
| CA2397566A1 (en) | 2001-07-19 |
| WO2001051588A8 (en) | 2001-11-01 |
| WO2001051589A8 (en) | 2002-02-21 |
| WO2001051588A1 (en) | 2001-07-19 |
| WO2001051589A1 (en) | 2001-07-19 |
| AU2001230919A1 (en) | 2001-07-24 |
| CN1427877A (en) | 2003-07-02 |
| EP1254197A1 (en) | 2002-11-06 |
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