CN109248541A - Hydrogen recovery system cooperative optimization method and system - Google Patents
Hydrogen recovery system cooperative optimization method and system Download PDFInfo
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- CN109248541A CN109248541A CN201710563835.1A CN201710563835A CN109248541A CN 109248541 A CN109248541 A CN 109248541A CN 201710563835 A CN201710563835 A CN 201710563835A CN 109248541 A CN109248541 A CN 109248541A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B01D—SEPARATION
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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Abstract
The present invention provides a kind of hydrogen recovery system cooperative optimization method and system, method includes: to establish the mathematical simulation model of hydrogen recovery system, and hydrogen recovery system includes psa unit and film separation unit；Mathematical is carried out to the mathematical simulation model of hydrogen recovery system, obtains the product hydrogen composition and flow of the hydrogen recovery system output；Judge whether product hydrogen composition and flow in solving result meet default calculate and require, if meeting default calculate to require, the global optimization model of the hydrogen recovery system is then established, and establishes the subsystem Optimized model of psa unit and film separation unit in the hydrogen recovery system respectively；The subsystem Optimized model of psa unit and film separation unit is optimized respectively, and determines the Optimization Solution result of global optimization model according to the Optimization Solution result of subsystems Optimized model.The present invention being capable of maximum hydrogen recycling benefit.
Description
Technical field
The present invention relates to refinery hydrogen resource optimization studying technological domains, and in particular to a kind of hydrogen recovery system collaboration is excellent
Change method and system.
Background technique
As the heaviness of processing crude oil, the aggravation of in poor quality trend and product quality upgrading require to reinforce, hydrogen is in refinery
In for ensure qualified products production become more and more important, and high production hydrogen cost and hydrogen production bioreactor investment so that hydrogen return
It receives particularly important.
For refinery, common hydrogen retrieval technology mainly has pressure swing adsorption and membrane separation technique.Pressure-variable adsorption
Method is using solid absorbents such as silica gel, active carbon, the molecular sieves being mounted in vertical pressure vessel, to various in mixed gas
Impurity carries out selective absorption, to achieve the purpose that gas separates.It is to push away that membrane separation process, which is with the partial pressure difference of film two sides,
Power makes it realize the process of separation in two lateral enrichment of film using the difference of gas with various infiltration rate in film.
Current refinery hydrogen recovery unit optimizing research mainly has following several respects:
(1) in production run, technical staff rule of thumb and theoretical direction hydrogen recovery unit that it is responsible for carry out it is excellent
Change operation.Under normal conditions, in their less further investigation companies other hydrogen recovery units performance characteristics, cannot be from system angle
Degree, which sets out, considers that the collaboration in entire firm-wide between hydrogen recovery unit optimizes, and cannot give full play to effective conjunction of hydrogen recovery unit
Power.
(2) optimizing research of all kinds of hydrogen recovery units.The optimization of device itself is primarily focused on, does not study hydrogen retrieval sufficiently
Combinatorial Optimization, feedstock optimization between device etc., not from efficient, the economic recovery of entire hydrogen recovery system orientation optimization hydrogen.
(3) refinery's hydrogen resource system optimizing research.Its hydrogen retrieval part primarily focuses on hydrogen recovery unit energy consumption, hydrogen returns
The simple measuring and calculating for rate of producing effects not can be carried out and cooperate with optimizing research, device charging suitable between hydrogen recovery unit Analysis of Optimized Operation, device
Answering property analysis etc..
Therefore, how prior art problem to be solved, and a kind of efficient hydrogen retrieval system optimization research side is provided
Method is the research direction place of those skilled in the art.
Summary of the invention
For the defects in the prior art, the present invention provides a kind of hydrogen recovery system cooperative optimization method and system, this
Invention can maximum hydrogen recycle benefit, improve Business Economic Benefit.
Specifically, the present invention provides following technical schemes:
In a first aspect, the present invention provides a kind of hydrogen recovery system cooperative optimization methods, comprising:
Step S1: establishing the mathematical simulation model of hydrogen recovery system, and the hydrogen recovery system includes: pressure-variable adsorption list
At least one unit in member and film separation unit；The psa unit includes at least one pressure-swing absorption apparatus, described
Film separation unit includes at least one membrane separation device, and basis presets need in the pressure-swing absorption apparatus and the membrane separation device
It is selectively provided with compressor module；
Step S2: according to the design parameter and operation of psa unit and film separation unit in the hydrogen recovery system
Parameter is set into each pressure-swing absorption apparatus in the psa unit and enters each UF membrane in the film separation unit
The uninterrupted of the hydrogeneous stream stock of device, sets the adsorption equilibrium dynamics of each pressure-swing absorption apparatus in the psa unit
The component infiltration rate initial parameter value of each membrane separation device in initial parameter value, and the setting film separation unit；Wherein,
Hydrogeneous stream stock in the hydrogen recovery system includes the hydrogeneous stream stock for passing in and out psa unit, film separation unit, Yi Jipai
It puts to the hydrogeneous stream stock of oil refining gas stream system；
Step S3: carrying out Mathematical to the mathematical simulation model of the hydrogen recovery system, obtains the hydrogen recycling
The product hydrogen composition and flow of system output；
Step S4: whether product hydrogen composition and flow in judgment step S3 solving result, which meet default calculate, requires, if
Meet default calculate to require, thens follow the steps S5；If not meeting, pre-designed calculation is required and the number of iterations is not up to preset limit
Number, then in amendment step S2 into each pressure-swing absorption apparatus in the psa unit and enter the film separation unit
In the uninterrupted of hydrogeneous stream stock of each membrane separation device, in the psa unit each pressure-swing absorption apparatus adsorption equilibrium
In kinetic parameter initial value and the film separation unit in the component infiltration rate initial parameter value of each membrane separation device
It is one or more, and return step S3；If not meeting, pre-designed calculation is required and the number of iterations has reached preset limit number, is held
Row step S5；
Step S5: establishing the global optimization model of the hydrogen recovery system, and establishes hydrogen recycling system respectively
The subsystem Optimized model of psa unit and film separation unit in system；
Step S6: the global optimization model of the hydrogen recovery system is initialized, and respectively to pressure-variable adsorption
The subsystem Optimized model of unit and film separation unit is initialized；Wherein, to the global optimization of the hydrogen recovery system
It includes: the first the number of iterations upper limit of global optimization model to be arranged, and enter the pressure-variable adsorption list that model, which carries out initialization,
Each pressure-swing absorption apparatus and the uninterrupted into the hydrogeneous stream stock of each membrane separation device in the film separation unit in member；Its
In, carrying out initialization to the subsystem Optimized model of psa unit and film separation unit includes: that each subsystem of setting optimizes
The secondary iteration maximum number of times of model, and receive the global optimization model specification into each in the psa unit
Pressure-swing absorption apparatus and the uninterrupted for entering the hydrogeneous stream stock of each membrane separation device in the film separation unit；
Step S7: respectively optimizing the subsystem Optimized model of psa unit and film separation unit, and
The Optimization Solution result of global optimization model is determined according to the Optimization Solution result of subsystems Optimized model；
Wherein, the objective function of the global optimization model are as follows: the maximization product hydrogen retrieval benefit of hydrogen recovery system,
Wherein, the product hydrogen retrieval benefit of the hydrogen recovery system is equal to the production of the psa unit and the film separation unit
The sum of product hydrogen retrieval benefit；
The constraint condition of the global optimization model includes: scheduled into psa unit in hydrogen recovery system
The difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and psa unit actual treatment is less than default relaxation factor and hydrogen
The hydrogeneous stream plume of the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment in recovery system
The difference of amount is less than default relaxation factor；The constraint condition of the global optimization model further include: the hydrogeneous stream stock of hydrogen recovery system
In pure hydrogen amount be greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen recycling system
The hydrogeneous pure hydrogen amount flowed in stock of uniting is equal to psa unit and pure hydrogen amount and row in the product hydrogen of film separation unit acquisition
The sum of pure hydrogen content is put into the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter change
Press the minimum difference of the hydrogeneous stream plume amount of absorbing unit and the hydrogeneous stream plume amount of psa unit actual treatment；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter film point
The minimum difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and film separation unit actual treatment from unit；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-variable adsorption in psa unit
The inlet and outlet of device meet conservation of matter, component conservation, and raw gas pressure, which is greater than or equal to pressure-swing absorption apparatus inlet pressure, to be wanted
It asks, the machining load of pressure-swing absorption apparatus is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or waits
Predetermined component gas cannot penetrate predetermined adsorption layer in default Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: each membrane separation device in film separation unit
Inlet and outlet meet conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, UF membrane
The machining load of device is within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient；
Step S8: judging whether the Optimization Solution result of global optimization model restrains, if convergence, terminates the hydrogen and returns
The Optimization Solution process of receipts system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminates the hydrogen and return
The Optimization Solution process of receipts system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, return step S7 after
It is continuous to optimize until each subsystem Optimized model reaches secondary iteration maximum number of times.
Further, the design parameter of psa unit and film separation unit includes: each in the hydrogen recovery system
Height, internal diameter, temperature, pressure, processing capacity, adsorbent inventory, classification, Kong Rong and the specific surface of a pressure-swing absorption apparatus
Product；Design temperature, pressure, selectivity and the processing capacity of each membrane separation device；Compressor mould in each pressure-swing absorption apparatus
The processing load of block limits；The processing load limitation of compressor module in each membrane separation device；
The operating parameter of psa unit and film separation unit includes: each pressure-variable adsorption in the hydrogen recovery system
Operation temperature, pressure and the adsorption time of device；The operation temperature and pressure of each membrane separation device；The flow of hydrogeneous stream stock,
Composition and pressure.
Further, the mathematical simulation model of hydrogen recovery system is established, comprising:
The mathematical simulation model of each pressure-swing absorption apparatus in psa unit, each film point in film separation unit are established respectively
Mathematical simulation model and each UF membrane from compressor module in the mathematical simulation model of device, each pressure-swing absorption apparatus
The mathematical simulation model of compressor module in device.
Further, the mathematical simulation model of each pressure-swing absorption apparatus in psa unit is established, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixing to be determined
The equilibrium adsorption capacity of gas component i on the sorbent in gas；qmax,iIndicate that gas component i is being adsorbed in mixed gas to be determined
Maximal absorptive capacity in agent；BiIndicate Langmuir absorption constant of the gas component i on the adsorbent；BjIndicate gas group
Divide Langmuir absorption constant of the j on the adsorbent；PiIndicate the partial pressure of gas component i in mixed gas to be determined；PjTable
Show the partial pressure of gas component j in mixed gas to be determined.
Further, the mathematical simulation model of each pressure-swing absorption apparatus in psa unit is established, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIt indicates wait inhale
In attached mixed gas, the partial pressure of gas component i；BiIndicate that Langmuir absorption of the gas component i on this layer of adsorbent is normal
Number；BijIndicate Langmuir absorption of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j
Constant；KijIndicate that the component j when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j inhales component i
The influence degree of attached effect；Ki,mixIndicate suction-operated of all gas component to gas component i in mixed gas to be adsorbed
Affecting parameters.
Second aspect, the present invention also provides a kind of hydrogen recovery systems to cooperate with optimization system, comprising:
First modeling unit, for establishing the mathematical simulation model of hydrogen recovery system, the hydrogen recovery system includes:
At least one unit in psa unit and film separation unit；The psa unit includes at least one pressure-variable adsorption
Device, the film separation unit include at least one membrane separation device, in the pressure-swing absorption apparatus and the membrane separation device
It needs to be selectively provided with compressor module according to default；
First initial value setup unit, for according to psa unit and film separation unit in the hydrogen recovery system
Design parameter and operating parameter, be set into the psa unit each pressure-swing absorption apparatus and enter the film point
The uninterrupted of hydrogeneous stream stock from membrane separation device each in unit, sets each pressure-swing absorption apparatus in the psa unit
Adsorption equilibrium kinetic parameter initial value, and in the setting film separation unit each membrane separation device component infiltration rate
Initial parameter value；Wherein, the hydrogeneous stream stock in the hydrogen recovery system includes disengaging psa unit, film separation unit
Hydrogeneous stream stock, and it is emitted into the hydrogeneous stream stock of oil refining gas stream system；
First solves unit, carries out Mathematical for the mathematical simulation model to the hydrogen recovery system, obtains institute
State the product hydrogen composition and flow of hydrogen recovery system output；
First judging unit, the product hydrogen composition in solving result for judging the first solution unit are with flow
Default calculate of no satisfaction requires, and requires if meeting and presetting to calculate, executes the second modeling unit；If not meeting pre-designed calculation requirement
And the number of iterations is not up to preset limit number, then correct in the first initial value setup unit into the pressure-variable adsorption
In unit each pressure-swing absorption apparatus and enter the film separation unit in each membrane separation device hydrogeneous stream stock uninterrupted,
The adsorption equilibrium kinetic parameter initial value and the film separation unit of each pressure-swing absorption apparatus in the psa unit
In each membrane separation device one of component infiltration rate initial parameter value or a variety of, and return to described first and solve unit；
If not meeting, pre-designed calculation is required and the number of iterations has reached preset limit number, executes the second modeling unit；
Second modeling unit, for establishing the global optimization model of the hydrogen recovery system, and described in establishing respectively
The subsystem Optimized model of psa unit and film separation unit in hydrogen recovery system；
Second initial value setup unit is initialized for the global optimization model to the hydrogen recovery system, with
And the subsystem Optimized model of psa unit and film separation unit is initialized respectively；Wherein, the hydrogen is returned
It includes: that the first the number of iterations upper limit of global optimization model, Yi Jijin is arranged that the global optimization model of receipts system, which carries out initialization,
Enter each pressure-swing absorption apparatus in the psa unit and enters the hydrogeneous of each membrane separation device in the film separation unit
Flow the uninterrupted of stock；Wherein, carrying out initialization to the subsystem Optimized model of psa unit and film separation unit includes:
The secondary iteration maximum number of times of each subsystem Optimized model is set, and is received described in the entrance of the global optimization model specification
Each pressure-swing absorption apparatus and enter the hydrogeneous stream stock of each membrane separation device in the film separation unit in psa unit
Uninterrupted；
Second solves unit, carries out for the subsystem Optimized model respectively to psa unit and film separation unit excellent
Change and solve, and determines the Optimization Solution result of global optimization model according to the Optimization Solution result of subsystems Optimized model；
Wherein, the constraint condition of the global optimization model includes: scheduled into pressure-variable adsorption in hydrogen recovery system
The difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and psa unit actual treatment of unit is less than default relaxation factor, with
And in hydrogen recovery system the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment it is hydrogeneous
The difference for flowing plume amount is less than default relaxation factor；The constraint condition of the global optimization model further include: hydrogen recovery system contains
Pure hydrogen amount in hydrogen stream stock is greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen
Pure hydrogen amount in the hydrogeneous stream stock of recovery system is equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain
And it is emitted into the sum of pure hydrogen content in the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter change
Press the minimum difference of the hydrogeneous stream plume amount of absorbing unit and the hydrogeneous stream plume amount of psa unit actual treatment；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter film point
The minimum difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and film separation unit actual treatment from unit；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-variable adsorption in psa unit
The inlet and outlet of device meet conservation of matter, component conservation, and raw gas pressure, which is greater than or equal to pressure-swing absorption apparatus inlet pressure, to be wanted
It asks, the machining load of pressure-swing absorption apparatus is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or waits
Predetermined component gas cannot penetrate predetermined adsorption layer in default Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: each membrane separation device in film separation unit
Inlet and outlet meet conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, UF membrane
The machining load of device is within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient；
Second judgment unit, for judging whether the Optimization Solution result of global optimization model restrains, if convergence, terminates
The Optimization Solution process of the hydrogen recovery system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminate
The Optimization Solution process of the hydrogen recovery system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, return
It returns the second solution unit and continues Optimization Solution until each subsystem Optimized model reaches secondary iteration maximum number of times.
Further, the design parameter of psa unit and film separation unit includes: each in the hydrogen recovery system
Height, internal diameter, temperature, pressure, processing capacity, adsorbent inventory, classification, Kong Rong and the specific surface of a pressure-swing absorption apparatus
Product；Design temperature, pressure, selectivity and the processing capacity of each membrane separation device；Compressor mould in each pressure-swing absorption apparatus
The processing load of block limits；The processing load limitation of compressor module in each membrane separation device；
The operating parameter of psa unit and film separation unit includes: each pressure-variable adsorption in the hydrogen recovery system
Operation temperature, pressure and the adsorption time of device；The operation temperature and pressure of each membrane separation device；The flow of hydrogeneous stream stock,
Composition and pressure.
Further, first modeling unit is specifically used in the mathematical simulation model for establishing hydrogen recovery system:
The mathematical simulation model of each pressure-swing absorption apparatus in psa unit, each film point in film separation unit are established respectively
Mathematical simulation model and each UF membrane from compressor module in the mathematical simulation model of device, each pressure-swing absorption apparatus
The mathematical simulation model of compressor module in device.
Further, the mathematical simulation of the first modeling unit each pressure-swing absorption apparatus in establishing psa unit
When model, it is specifically used for:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixing to be determined
The equilibrium adsorption capacity of gas component i on the sorbent in gas；qmax,iIndicate that gas component i is being adsorbed in mixed gas to be determined
Maximal absorptive capacity in agent；BiIndicate Langmuir absorption constant of the gas component i on the adsorbent；BjIndicate gas group
Divide Langmuir absorption constant of the j on the adsorbent；PiIndicate the partial pressure of gas component i in mixed gas to be determined；PjTable
Show the partial pressure of gas component j in mixed gas to be determined.
Further, the mathematical simulation of the first modeling unit each pressure-swing absorption apparatus in establishing psa unit
When model, it is specifically used for:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIt indicates wait inhale
In attached mixed gas, the partial pressure of gas component i；BiIndicate that Langmuir absorption of the gas component i on this layer of adsorbent is normal
Number；BijIndicate Langmuir absorption of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j
Constant；KijIndicate that the component j when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j inhales component i
The influence degree of attached effect；Ki,mixIndicate suction-operated of all gas component to gas component i in mixed gas to be adsorbed
Affecting parameters.
As shown from the above technical solution, hydrogen recovery system cooperative optimization method provided by the invention and system, unlike existing
There is technology only to lay particular emphasis on the optimization of pressure-swing absorption apparatus or membrane separation device itself like that, but sufficiently studies each hydrogen and return
Combination collaboration optimization, raw material collaboration optimization between receiving apparatus, from the efficient, economic of entire hydrogen recovery system orientation optimization hydrogen
Recycling；The present invention considers that the collaboration in entire enterprise-wide between hydrogen gas recovering device optimizes from system perspective, gives full play to
Effective resultant force of each hydrogen gas recovering device；Compared with prior art, the present invention can effectively improve the behaviour of hydrogen recovery system
Make horizontal, maximum hydrogen recycling, raising Business Economic Benefit.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is the present invention
Some embodiments for those of ordinary skill in the art without creative efforts, can also basis
These attached drawings obtain other attached drawings.
Fig. 1 is the flow chart for the hydrogen recovery system cooperative optimization method that one embodiment of the invention provides；
Fig. 2 be another embodiment of the present invention provides hydrogen recovery system collaboration optimization system structural schematic diagram.
Specific embodiment
In order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, the technical scheme in the embodiment of the invention is clearly and completely described, it is clear that described embodiment is
A part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art
Every other embodiment obtained without creative efforts, shall fall within the protection scope of the present invention.
One embodiment of the invention provides a kind of hydrogen recovery system cooperative optimization method, flow chart shown in Figure 1,
This method comprises the following steps:
Step 101: establishing the mathematical simulation model of hydrogen recovery system, the hydrogen recovery system includes: pressure-variable adsorption
At least one unit in unit and film separation unit；The psa unit includes at least one pressure-swing absorption apparatus, institute
Stating film separation unit includes at least one membrane separation device, and basis is default in the pressure-swing absorption apparatus and the membrane separation device
It needs to be selectively provided with compressor module.
In this step, the mathematical simulation model for establishing hydrogen recovery system, specifically includes: establishing pressure-variable adsorption list respectively
The mathematical simulation model of each pressure-swing absorption apparatus in member, the mathematical simulation model of each membrane separation device and each in film separation unit
The mathematical simulation model of compressor module in pressure-swing absorption apparatus and each membrane separation device, wherein connected by hydrogeneous logistics, it can
To construct the mathematical simulation model of hydrogen recovery system.It is understood that compressor module described in this step refer in particular to
The relevant compressor of hydrogen retrieval system, such as the charging and infiltration for desorbing air compressor, membrane separation device of pressure-swing absorption apparatus
Air compressor etc. does not include circulating hydrogen compressor and other technique stream stock compressors.
In a kind of optional embodiment of this step, the mathematical modulo of each pressure-swing absorption apparatus in psa unit is established
Analog model, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment.
It is understood that in this optional embodiment, using absorbing balance equation, mass transfer rate equation and total mass transfer
Equilibrium equation, the mathematical simulation model for establishing the pressure-swing absorption apparatus refer to, using absorbing balance equation, mass transfer rate equation
Establish the mathematical simulation model of each adsorption layer in pressure-swing absorption apparatus respectively with total mass transfer equilibrium equation.Wherein, unstripped gas passes through
The entrance initial value that the calculated result of a certain adsorption layer is calculated as the simulation of next adsorption layer.Specifically, it is assumed that pressure and temperature are permanent
Fixed constant, flow model uses axial dispersion plug flow model, and change in flow caused by adsorbing is calculated by total mass transfer equilibrium equation,
Mass transfer rate equation uses linear driving force model (LDF), and absorbing balance equation is using extension Langmuir model description.
In this optional embodiment, each model equation is as follows:
The mass transfer equilibrium equation of gas component i in element of volume:
Wherein, DLIndicate bed axial diffusion coefficient, m2/s；CiIndicate component i gas phase total concentration, mol/m3；V indicates gas
Flow velocity degree, m/s；ρPIndicate density of gas phase under adsorptive pressure P, kg/m3；ε indicates Molecular Adsorption bed porosity, dimensionless；Table
Show component i adsorption equilibrium concentration, mol/kg.
Total mass transfer equilibrium equation:
Wherein, C indicates bed gas phase concentration, mol/m3；Other parameters meaning is same as above.
Mass transfer rate equation:
Wherein, kiIndicate gas solid transfer coefficient, s；Indicate component i adsorbent bed gas phase concentration, mol/kg；Indicate component
I adsorption equilibrium concentration, mol/kg.
In specific calculate, by adsorption tower bed (pressure-swing absorption apparatus) from tower bottom to tower top, not according to adsorbent classification
With different infinitesimal sections (calculating needs according to practical, same adsorbent layer can also be divided into multiple infinitesimal sections) is divided into, often
The calculated result of one infinitesimal section outlet calculates initial value as next infinitesimal section entrance, successively calculates to absorption tower top, if adsorption tower
It pushes up calculated result and actual value deviation is larger, then return to tower bottom the first infinitesimal section, modification, adjustment relevant parameter.Each infinitesimal section
All using above-mentioned several governing equations modeling, simultaneous solution.Different component is calculated by adsorbent by absorbing balance equation
Adsorbance, the time by the mass transfer rate equation calculation component Jing Guo infinitesimal section, mass transfer material balance equation (total mass transfer material side
The material equation of journey and one-component) mainly pass through a material balance relationship of description component disengaging infinitesimal section, calculating group
Divide the character (concentration, flow etc.) in infinitesimal section exit.
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixing to be determined
The equilibrium adsorption capacity of gas component i on the sorbent in gas；qmax,iIndicate that gas component i is being adsorbed in mixed gas to be determined
Maximal absorptive capacity in agent；BiLangmuir absorption constant of the expression gas component i on the adsorbent, 106Pa-1；BjIt indicates
Langmuir absorption constant of the gas component j on the adsorbent, 106Pa-1；PiIndicate gas group in mixed gas to be determined
The partial pressure of point i, 106Pa；PjIndicate the partial pressure of gas component j in mixed gas to be determined, 106Pa。
In another optional embodiment of this step, the mathematics of each pressure-swing absorption apparatus in psa unit is established
Simulation model, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
In this optional embodiment, mass transfer rate equation and total mass transfer equilibrium equation and last optional embodiment phase
Together, last optional embodiment is specifically referred to, the absorbing balance equation in this optional embodiment and above embodiment are not
Together.In this optional embodiment, absorbing balance equation is described using a kind of improved Langmuir model.
In this optional embodiment, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIt indicates wait inhale
In attached mixed gas, the partial pressure of gas component i, 106Pa；BiIndicate that Langmuir of the gas component i on this layer of adsorbent is inhaled
Attached constant, 106Pa-1；BijIndicate orchid of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j
Ge Miaoer absorption constant；KijIndicate the component when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j
Influence degree of the j to component i suction-operated；Ki,mixIndicate that all gas component is to gas component i in mixed gas to be adsorbed
Suction-operated affecting parameters.
It should be noted that the absorbing balance equation that the present embodiment uses is based on improved Langmuir model.Below
Improved Langmuir model is introduced:
It is main to be described using one pack system Langmuir model or the Langmuir model of extension in current adsorbing separation field
The Phase Equilibria of adsorption process.But one side one pack system Langmuir model is suitable for studying the absorption of one-component gas
Journey research does not consider influencing each other between different component, cannot describe the adsorption process of multicomponent gaseous mixture；On the other hand it extends
Langmuir model be the wide description multicomponent gas-solid adsorption process of application in recent years model, theoretically need experiment true
Determine the adsorption equilibrium costant of various components on the sorbent in mixed atmosphere to be calculated again, but due to the gas more than two components
The acquisition of adsorption equilibrium costant is extremely difficult, therefore, when the model practical application, generally still uses the one pack system Lange of the component
Miao Er absorption constant replaces the adsorption equilibrium costant of the component in gaseous mixture, and it is flat that such simplified processing must increase gaseous mixture
The inaccuracy that the adsorbance that weighs calculates.For this technical problem, the present embodiment provides a kind of improved Langmuir model, this
The improved Langmuir model of kind being capable of Accurate Determining multi component adsorption process adsorbance.
The establishment process of absorbing balance equation provided in this embodiment is given below:
A, by laboratory facilities or data searching, each gas component is acquired in mixed gas to be determined respectively in same absorption
One pack system Langmuir model on agent S obtains the one pack system Langmuir absorption constant B of each gas componenti；Wherein, described
Mixed gas to be determined includes n kind gas component, 1≤i≤n altogether；
B, according to the gas composition of mixed gas to be determined, the gas of every two kinds of components is configured to binary gas and is mixed
Object is prepared obtain altogetherGroup binary gas mixture；Wherein, the gas of every two kinds of components is being configured to binary gas mixture
When, the molar ratio of two kinds of component gas can be any molar ratio in binary gas mixture, it is preferable that two kinds of gas components
Molar ratio is 1:1.
C, Langmuir absorption of each gas component on the adsorbent in every group of binary gas mixture is obtained respectively
Constant Bij, wherein BijIndicate orchid of the component i on the adsorbent S in the binary gas mixture comprising component i and component j
Ge Miaoer absorption constant；The step can be obtained by experiment.
D, the binary interaction parameter K in every group of binary gas mixture between gas component is obtained respectivelyij, wherein Kij
=Bij/Bi, KijIndicate the binary gas mixture comprising component i and component j when being adsorbed on the adsorbent S component j to group
Divide the influence degree of i suction-operated；Wherein, if 0 < Kij< 1, then it represents that gas component j has the adsorption process of gas component i
There is inhibiting effect；If Kij=1, then it represents that gas component j does not influence or influence on the adsorption process of gas component i minimum；
As i=j, Kij=1；If Kij> 1, then it represents that gas component j has facilitation to the adsorption process of gas component i.Its
In, KijCloser to 1, indicate that components influence is smaller, KijDeviation 1 is bigger, shows that components influence is stronger.
E, according to the binary interaction parameter K between gas component in the binary gas mixture of step d acquisitionij, obtain
Suction-operated parameter K of all gas component to gas component i in mixed gas to be determinedi,mix；In this step, especially by
As under type obtains in mixed gas to be determined all gas component to the suction-operated parameter K of gas component ii,mix:
Wherein, yjIndicate that gas component j influences regulatory factor, y to the suction-operated of gas component ijExist for gas component j
Shared gas volume fractions in mixed gas to be determined.
F, according to all gas component in mixed gas to be determined to the suction-operated parameter K of gas component ii,mix, establish
The gas-solid adsorption equilibrium equation of mixed gas to be determined:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined, PiIndicate mixing to be determined
The partial pressure of gas component i in gas, 106Pa, BiIndicate Langmuir absorption constant of the gas component i on the adsorbent,
106Pa-1；.
G, it solves equation and obtains adsorbance of each gas component on adsorbent S.
In a kind of optional embodiment of this step, the mathematical simulation mould of each membrane separation device in film separation unit is established
Type, comprising:
Ignore the flow resistance of two side liquid of film, it is assumed that feed side gas composition changes linearly, and per-meate side is full mixing
The mathematical model of form, component i gas infiltration capacity is as follows:
Wherein, QiIndicate that component i permeates tolerance；JiIndicate infiltration coefficient；A indicates membrane area；PFIndicate raw material film surface
Pressure；xiFIndicate the concentration of gas component i in unstripped gas；xiRIndicate the concentration of gas component i in infiltration residual air；PpIndicate infiltration gas
Pressure；yiPIndicate the concentration of gas component i in infiltration gas.
In a kind of optional embodiment of this step, establish each in the pressure-swing absorption apparatus and the membrane separation device
The mathematical simulation model of compressor module, comprising:
Ccomp=c × Power
Wherein, Power indicates that compressor horsepower calculates；C1Indicate gas constant pressure specific heat；T indicates gas inlet temperature；η table
Show compressor efficiency coefficient；Pin、PoutIndicate compressor inlet and outlet pressure；R indicates gas heat capacity ratio；ρ indicates entry into compressor
The gas density of gas；ρ0Indicate the gas density under standard state；F indicates entry into the gas flow of compressor；C indicates unit
The electricity charge；CcompIndicate power consumption of compressor expense.
Step 102: according to setting for psa unit in the hydrogen recovery system, film separation unit and compressor unit
Parameter and operating parameter are counted, each pressure-swing absorption apparatus in the psa unit is set into and enters the UF membrane list
The uninterrupted of the hydrogeneous stream stock of each membrane separation device, sets the suction of each pressure-swing absorption apparatus in the psa unit in member
The component infiltration rate parameter of each membrane separation device in attached equilibrium kinetics initial parameter value, and the setting film separation unit
Initial value；Wherein, the hydrogeneous stream stock in the hydrogen recovery system include pass in and out psa unit, film separation unit it is hydrogeneous
Stock is flowed, and is emitted into the hydrogeneous stream stock of oil refining gas stream system.
In this step, the design parameter of psa unit and film separation unit includes: in the hydrogen recovery system
Height, internal diameter, temperature, pressure, processing capacity, adsorbent inventory, classification, Kong Rong and the specific surface of each pressure-swing absorption apparatus
Product；Design temperature, pressure, selectivity and the processing capacity of each membrane separation device；Compressor mould in each pressure-swing absorption apparatus
The processing load of block limits；The processing load limitation of compressor module in each membrane separation device；
The operating parameter of psa unit and film separation unit includes: each pressure-variable adsorption in the hydrogen recovery system
Operation temperature, pressure and the adsorption time of device；The operation temperature and pressure of each membrane separation device；The flow of hydrogeneous stream stock,
Composition and pressure.
In this step, adsorption equilibrium kinetic parameter includes: diffusion coefficient, mass tranfer coefficient, pelect number and Lange Miao
That adsorption equilibrium costant.
For example, it is assumed that in hydrogen recovery system psa unit and film separation unit design parameter and operating parameter
As shown in the following table 1~table 3.The hydrogeneous stream stock in part is as shown in table 4.
1 pressure-swing absorption apparatus design parameter of table and operating parameter
| 1#PSA | 2#PSA | |
| Adsorb tower section design parameter | ||
| Diameter, m | 3.2 | 2.8 |
| Height, m | 8.39 | 7.6 |
| Adsorbent filling | ||
| Molecular sieve | 40.5 | 29 |
| Active carbon | 8 | 5.6 |
| Silica gel | 1.8 | 1.2 |
| Activated alumina | 0.7 | 0.6 |
| Adsorption tower operating parameter | ||
| Adsorptive pressure, MPa | 2.1 | 2.1 |
| Material temperature, DEG C | 30~40 | 30~40 |
| Process flow | 10-1-6 | VPSA, 6-2-3 |
| Single column adsorption time, s | 225 | 217 |
2 membrane separation device design parameter of table and operating parameter
3 compressor design parameter of table and operating parameter
The hydrogeneous stream stock information in 4 part of table
Step 103: Mathematical being carried out to the mathematical simulation model of the hydrogen recovery system, obtains the hydrogen recycling
The product hydrogen composition and flow of system output.
Step 104: whether product hydrogen composition and flow in 103 solving result of judgment step, which meet default calculate, requires,
If meeting default calculate to require, 105 are thened follow the steps；If not meeting, pre-designed calculation is required and the number of iterations is not up to preset limit
Number, then in amendment step 102 into each pressure-swing absorption apparatus in the psa unit and enter the UF membrane
The uninterrupted of the hydrogeneous stream stock of each membrane separation device in unit, in the psa unit each pressure-swing absorption apparatus absorption
The component infiltration rate initial parameter value of each membrane separation device in equilibrium kinetics initial parameter value and the film separation unit
One of or a variety of, and return step 103；If not meeting, pre-designed calculation is required and the number of iterations has reached preset limit
Number, thens follow the steps 105.
Step 105: establishing the global optimization model of the hydrogen recovery system, and establish hydrogen recycling system respectively
The subsystem Optimized model of psa unit and film separation unit in system.
Step 106: the global optimization model of the hydrogen recovery system being initialized, and respectively to pressure-variable adsorption
The subsystem Optimized model of unit and film separation unit is initialized；Wherein, to the global optimization of the hydrogen recovery system
It includes: the first the number of iterations upper limit of global optimization model to be arranged, and enter the pressure-variable adsorption list that model, which carries out initialization,
Each pressure-swing absorption apparatus and the uninterrupted into the hydrogeneous stream stock of each membrane separation device in the film separation unit in member；Its
In, carrying out initialization to the subsystem Optimized model of psa unit and film separation unit includes: that each subsystem of setting optimizes
The secondary iteration maximum number of times of model, and receive the global optimization model specification into each in the psa unit
Pressure-swing absorption apparatus and the uninterrupted for entering the hydrogeneous stream stock of each membrane separation device in the film separation unit.
Step 107: the subsystem Optimized model of psa unit and film separation unit is optimized respectively, and
The Optimization Solution result of global optimization model is determined according to the Optimization Solution result of subsystems Optimized model.
Wherein, the objective function of the global optimization model are as follows: the maximization product hydrogen retrieval benefit of hydrogen recovery system,
Wherein, the product hydrogen retrieval benefit of the hydrogen recovery system is equal to the production of the psa unit and the film separation unit
The sum of product hydrogen retrieval benefit；
The constraint condition of the global optimization model includes: scheduled into psa unit in hydrogen recovery system
The difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and psa unit actual treatment is less than default relaxation factor and hydrogen
The hydrogeneous stream plume of the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment in recovery system
The difference of amount is less than default relaxation factor；The constraint condition of the global optimization model further include: the hydrogeneous stream stock of hydrogen recovery system
In pure hydrogen amount be greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen recycling system
The hydrogeneous pure hydrogen amount flowed in stock of uniting is equal to psa unit and pure hydrogen amount and row in the product hydrogen of film separation unit acquisition
The sum of pure hydrogen content is put into the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter change
Press the minimum difference of the hydrogeneous stream plume amount of absorbing unit and the hydrogeneous stream plume amount of psa unit actual treatment；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter film point
The minimum difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and film separation unit actual treatment from unit；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-variable adsorption in psa unit
The inlet and outlet of device meet conservation of matter, component conservation, and raw gas pressure, which is greater than or equal to pressure-swing absorption apparatus inlet pressure, to be wanted
It asks, the machining load of pressure-swing absorption apparatus is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or waits
Predetermined component gas cannot penetrate predetermined adsorption layer in default Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: each membrane separation device in film separation unit
Inlet and outlet meet conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, UF membrane
The machining load of device is within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient.
Step 108: judging whether the Optimization Solution result of global optimization model restrains, if convergence, terminates the hydrogen
The Optimization Solution process of recovery system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminate the hydrogen
The Optimization Solution process of recovery system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, return step 107
Continue Optimization Solution until each subsystem Optimized model reaches secondary iteration maximum number of times.
It describes in detail below for above-mentioned steps 105-108.
(1) objective function of the global optimization model are as follows: the maximization product hydrogen retrieval benefit of hydrogen recovery system.
Wherein, total recycling benefit of hydrogen recovery system is equal to the sum of the recycling benefit of each hydrogen gas recovering device, each subsystem benefit
fi(Xi) calculated in subsystems respectively, total recycling benefit of hydrogen recovery system are as follows:
The constraint condition of the global optimization model includes A and B:
A: hydrogen recovery system and subsystem i equation consistency constraint are as follows:
……
……
Wherein,Indicate that subsystem i actual recovered handles hydrogeneous stream stock rjFlow, be that subsystem i passes to system
One constant of grade；Indicate that scheduled subsystem i is recycled hydrogeneous stream stock r in hydrogen recovery systemjIn flow, be
System-level variable, ε indicate default relaxation factor.It is understood that subsystem i here indicates psa unit or film point
From unit.N indicates the quantity of the pressure-swing absorption apparatus or membrane separation device that include in psa unit or film separation unit.
B: traffic constraints
Pure hydrogen amount in the hydrogeneous stream stock of hydrogen recovery system is necessarily greater than in the product hydrogen obtained equal to hydrogen retrieval subsystem
Pure hydrogen amount；Pure hydrogen amount in the hydrogeneous stream stock of hydrogen recovery system is equal to the pure hydrogen and drain into gas system that hydrogen retrieval subsystem obtains
It unites the sum of pure hydrogen content in hydrogeneous stream stock.
Wherein,Indicate hydrogeneous stream stock rjFlow；Indicate hydrogeneous stream stock rjHydrogen purity；Indicate subsystem i
Product hydrogen flowrate；Indicate the product hydrogen purity of subsystem i；Expression drains into the hydrogeneous stream plume amount of gas train；Expression drains into the hydrogeneous stream stock hydrogen purity of gas train.
The calculation expression of hydrogen recycling benefit is given below:
fi=fI- product H2 value-fI- supplements calorific value failure costs-fI- compressor power consumption expense
Wherein, fI- product H2 valueIndicate the value of subsystem i recycling hydrogen；fI- supplements calorific value failure costsIndicate that supplement is made because recycling hydrogen
At calorific value of fuel gas loss expense；fI- compressor power consumption expenseIndicate compressor power consumption expense relevant to subsystem i；ciIndicate son
System i product hydrogen price；Indicate subsystem i product hydrogen flowrate；Indicate the low-heat of subsystem i product hydrogen stream stock
Value；LCVNGIndicate the low heat value of unit volume natural gas；cNGIndicate unit volume Gas Prices；Power indicates compressor work
Rate calculates；C1Indicate gas constant pressure specific heat；T indicates gas inlet temperature；η indicates compressor efficiency coefficient；Pin、PoutIndicate pressure
Contracting machine inlet and outlet pressure；R indicates gas heat capacity ratio；ρ indicates gas density；F indicates entry into the gas flow of compressor；C is indicated
The unit electricity charge；CcompIndicate compressor power consumption expense.
(2) objective function of subsystems Optimized model are as follows:
Wherein,Indicate that subsystem i actual recovered handles hydrogeneous stream stock rjFlow, be that subsystem i passes to system
One constant of grade；Indicate that scheduled subsystem i is recycled hydrogeneous stream stock r in hydrogen recovery systemjIn flow, be
System-level variable.
The constraint condition of subsystems Optimized model is respectively as follows:
1. pressure-swing absorption apparatus:
Pressure-swing absorption apparatus inlet and outlet need to meet conservation of matter, component conservation；Raw gas pressure need to enter more than or equal to device
Mouth pressure requirements；Device machining load is constrained by working ability；Product hydrogen hydrogen purity is more than or equal to a certain setting value, preferred to be worth
It is 99.9%；Become one timing of adsorbent equipment raw material, it should be ensured that H2O does not penetrate silica gel bed, i.e. tAbsorption< tH2O, C2 +Heavy hydrocarbon does not penetrate
Active carbon bed, i.e. tAbsorption< tC2+, CH4Mol sieve beds are not penetrated, the i.e. t of adsorbent poisoning is avoidedAbsorption< tCH4；Device processing is negative
Lotus is constrained by working ability.
Wherein, FPIndicate pressure-swing absorption apparatus product hydrogen flowrate；FStripping gasIndicate that pressure-swing absorption apparatus desorbs throughput；Indicate the content of component s in hydrogeneous stream stock rj；yP, component sIndicate pressure-swing absorption apparatus product hydrogen component s content；
yStripping gas, component sIndicate pressure-swing absorption apparatus stripping gas component s content；Indicate pressure-swing absorption apparatus product hydrogen purity；Indicate chargingWhen, the adsorption operations time of pressure-swing absorption apparatus；Indicate chargingWhen, component H in raw material2O enters the time of break-through for finally penetrating silica gel bed from tower bottom；Indicate into
MaterialWhen, component in raw materialHeavy hydrocarbon enters the time of break-through for finally penetrating active carbon bed from tower bottom；Indicate chargingWhen, component CH in raw material4Enter from tower bottom and finally penetrates penetrating for mol sieve beds
Time；Indicate the pressure of hydrogeneous stream stock rj；PIn, PSAIndicate that pressure-swing absorption apparatus entrance requires pressure；Indicate transformation
Adsorbent equipment treating capacity；Indicate pressure-swing absorption apparatus working ability lower limit；Indicate that pressure-swing absorption apparatus processes energy
The power upper limit.
2. membrane separation device:
Membrane separation device inlet and outlet need to meet conservation of matter, component conservation；Raw gas pressure need to be more than or equal to UF membrane and fill
Posting port pressure requirements；Device machining load is constrained by working ability；CO impurity cannot be contained in unstripped gas.
Wherein,Indicate hydrogeneous stream stock rjThe content of middle gas component s；yPermeate gas, component sIndicate component s in infiltration gas
Content；ySeep residual air, component sIndicate the content of gas component s in infiltration residual air；Indicate hydrogeneous stream stock rjMiddle gas component CO's
Content.
3. compressor module:
Hydrogeneous stream stock disengaging compressor need to meet flow equilibrium and component balanced, and expression formula is as follows:
FComp, in=FComp, out
FComp, in×yComponent s, in=FComp, out×yComponent s, out
Wherein, FComp, inIndicate suction port of compressor flow；FComp, outIndicate compressor outlet flow；yComponent s, inIndicate compression
Machine inlet component s content；yComponent s, outIndicate compressor outlet component s content.
(3) the first the number of iterations upper limit of global optimization model and the secondary iteration of each subsystem Optimized model are set
Maximum number of times.Wherein, the first the number of iterations upper limit is 5~50；Secondary iteration maximum number of times is 5~40.For example, setting is whole excellent
The first the number of iterations upper limit for changing model is 15 times, default relaxation factor is 0.0001.It is arranged the of each subsystem Optimized model
The two the number of iterations upper limits are 10 times.
Wherein, it is optimized when being solved to each subsystem Optimized model using dedicated solver, method for solving can
To use Kriging approximate model method, genetic algorithm, ant group algorithm etc..Since the method for solving is known content, therefore here not
It is described in detail again.It is equally solved using dedicated solver when being optimized to global optimization model, method for solving can be with
Using Reduced gradient method, gradient projection method etc..Since the method for solving is known content, therefore I will not elaborate.In each subsystem
After Optimized model of uniting solves, judge whether the Optimization Solution result of global optimization model restrains, if convergence, terminates described
The Optimization Solution process of hydrogen recovery system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminate described
The Optimization Solution process of hydrogen recovery system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, step is returned
Rapid 107 continue Optimization Solution until each subsystem Optimized model reaches secondary iteration maximum number of times.
Wherein, the following table 5 is that hydrogen retrieval systematic entirety can be right before and after being optimized using cooperative optimization method of the present invention
Than.It can be seen that from result, system recycles hydrogen 2740Nm3/h more after optimization, has significant economic benefit.
The optimization of table 5 front and back hydrogen retrieval systematic entirety can compare
As shown from the above technical solution, hydrogen recovery system cooperative optimization method provided in an embodiment of the present invention, unlike existing
There is technology only to lay particular emphasis on the optimization of pressure-swing absorption apparatus or membrane separation device itself like that, but sufficiently studies each hydrogen and return
Combination collaboration optimization, raw material collaboration optimization between receiving apparatus, from the efficient, economic of entire hydrogen recovery system orientation optimization hydrogen
Recycling；The present invention considers that the collaboration in entire enterprise-wide between hydrogen gas recovering device optimizes from system perspective, gives full play to
Effective resultant force of each hydrogen gas recovering device；Compared with prior art, the present invention can effectively improve the behaviour of hydrogen recovery system
Make horizontal, maximum hydrogen recycling, raising Business Economic Benefit.
Another embodiment of the present invention additionally provides a kind of hydrogen recovery system collaboration optimization system, referring to fig. 2, the system packet
Include: the first modeling unit 21, the first initial value setup unit 22, first solve unit 23, the modeling of the first judging unit 24, second
Unit 25, the second initial value setup unit 26, second solve unit 27, second judgment unit 28, in which:
First modeling unit 21, for establishing the mathematical simulation model of hydrogen recovery system, the hydrogen recovery system packet
It includes: at least one unit in psa unit and film separation unit；The psa unit includes at least one transformation
Adsorbent equipment, the film separation unit include at least one membrane separation device, the pressure-swing absorption apparatus and UF membrane dress
It sets middle basis and presets and need to be selectively provided with compressor module；
First initial value setup unit 22, for according to psa unit in the hydrogen recovery system and UF membrane list
The design parameter and operating parameter of member are set into each pressure-swing absorption apparatus in the psa unit and enter the film
The uninterrupted of the hydrogeneous stream stock of each membrane separation device in separative unit sets each pressure-variable adsorption dress in the psa unit
The component of each membrane separation device permeates speed in the adsorption equilibrium kinetic parameter initial value set, and the setting film separation unit
Rate initial parameter value；Wherein, the hydrogeneous stream stock in the hydrogen recovery system includes disengaging psa unit, film separation unit
Hydrogeneous stream stock, and be emitted into the hydrogeneous stream stock of oil refining gas stream system；
First solves unit 23, carries out Mathematical for the mathematical simulation model to the hydrogen recovery system, obtains
The product hydrogen composition and flow of the hydrogen recovery system output；
First judging unit 24, the product hydrogen composition and flow in solving result for judging the first solution unit
Whether default calculate of satisfaction requires, and requires if meeting default calculate, executes the second modeling unit；If not meeting pre-designed want
It asks and the number of iterations is not up to preset limit number, then correct inhaling in the first initial value setup unit into the transformation
Coupon member in each pressure-swing absorption apparatus and enter the film separation unit in each membrane separation device hydrogeneous stream stock flow it is big
The adsorption equilibrium kinetic parameter initial value and the UF membrane of each pressure-swing absorption apparatus in small, the described psa unit
One of component infiltration rate initial parameter value of each membrane separation device or a variety of in unit, and return to described first and solve list
Member；If not meeting, pre-designed calculation is required and the number of iterations has reached preset limit number, executes the second modeling unit；
Second modeling unit 25 for establishing the global optimization model of the hydrogen recovery system, and establishes institute respectively
State the subsystem Optimized model of psa unit and film separation unit in hydrogen recovery system；
Second initial value setup unit 26 is initialized for the global optimization model to the hydrogen recovery system,
And the subsystem Optimized model of psa unit and film separation unit is initialized respectively；Wherein, to the hydrogen
The global optimization model of recovery system carries out the first the number of iterations upper limit that initialization includes: setting global optimization model, and
Into each pressure-swing absorption apparatus in the psa unit and enters each membrane separation device in the film separation unit and contain
The uninterrupted of hydrogen stream stock；Wherein, initialization package is carried out to the subsystem Optimized model of psa unit and film separation unit
It includes: the secondary iteration maximum number of times of each subsystem Optimized model being set, and receives the entrance of the global optimization model specification
Each pressure-swing absorption apparatus and the hydrogeneous stream into each membrane separation device in the film separation unit in the psa unit
The uninterrupted of stock；
Second solves unit 27, carries out for the subsystem Optimized model respectively to psa unit and film separation unit
Optimization Solution, and determine according to the Optimization Solution result of subsystems Optimized model the Optimization Solution knot of global optimization model
Fruit；
Wherein, the constraint condition of the global optimization model includes: scheduled into pressure-variable adsorption in hydrogen recovery system
The difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and psa unit actual treatment of unit is less than default relaxation factor, with
And in hydrogen recovery system the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment it is hydrogeneous
The difference for flowing plume amount is less than default relaxation factor；The constraint condition of the global optimization model further include: hydrogen recovery system contains
Pure hydrogen amount in hydrogen stream stock is greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen
Pure hydrogen amount in the hydrogeneous stream stock of recovery system is equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain
And it is emitted into the sum of pure hydrogen content in the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter change
Press the minimum difference of the hydrogeneous stream plume amount of absorbing unit and the hydrogeneous stream plume amount of psa unit actual treatment；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter film point
The minimum difference of the hydrogeneous stream plume amount of hydrogeneous stream plume amount and film separation unit actual treatment from unit；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-variable adsorption in psa unit
The inlet and outlet of device meet conservation of matter, component conservation, and raw gas pressure, which is greater than or equal to pressure-swing absorption apparatus inlet pressure, to be wanted
It asks, the machining load of pressure-swing absorption apparatus is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or waits
Predetermined component gas cannot penetrate predetermined adsorption layer in default Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: each membrane separation device in film separation unit
Inlet and outlet meet conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, UF membrane
The machining load of device is within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient；
Second judgment unit 28, for judging whether the Optimization Solution result of global optimization model restrains, if convergence, is tied
The Optimization Solution process of Shu Suoshu hydrogen recovery system；If not converged but the number of iterations reaches the first the number of iterations upper limit, tie
The Optimization Solution process of Shu Suoshu hydrogen recovery system；If not converged and the number of iterations is not up to the first the number of iterations upper limit,
It returns to the second solution unit and continues Optimization Solution until each subsystem Optimized model reaches secondary iteration maximum number of times.
In a kind of optional embodiment, the design of psa unit and film separation unit in the hydrogen recovery system
Parameter includes: height, internal diameter, temperature, pressure, processing capacity, adsorbent inventory, the classification, hole of each pressure-swing absorption apparatus
Appearance and specific surface area；Design temperature, pressure, selectivity and the processing capacity of each membrane separation device；Each pressure-swing absorption apparatus
The processing load of middle compressor module limits；The processing load limitation of compressor module in each membrane separation device；
The operating parameter of psa unit and film separation unit includes: each pressure-variable adsorption in the hydrogen recovery system
Operation temperature, pressure and the adsorption time of device；The operation temperature and pressure of each membrane separation device；The flow of hydrogeneous stream stock,
Composition and pressure.
In a kind of optional embodiment, first modeling unit 21 is in the mathematical simulation mould for establishing hydrogen recovery system
It is specifically used for when type:
The mathematical simulation model of each pressure-swing absorption apparatus in psa unit, each film point in film separation unit are established respectively
Mathematical simulation model and each UF membrane from compressor module in the mathematical simulation model of device, each pressure-swing absorption apparatus
The mathematical simulation model of compressor module in device.
In a kind of optional embodiment, first modeling unit 21 each pressure-variable adsorption in establishing psa unit
When the mathematical simulation model of device, it is specifically used for:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixing to be determined
The equilibrium adsorption capacity of gas component i on the sorbent in gas；qmax,iIndicate that gas component i is being adsorbed in mixed gas to be determined
Maximal absorptive capacity in agent；BiIndicate Langmuir absorption constant of the gas component i on the adsorbent；BjIndicate gas group
Divide Langmuir absorption constant of the j on the adsorbent；PiIndicate the partial pressure of gas component i in mixed gas to be determined；PjTable
Show the partial pressure of gas component j in mixed gas to be determined.
In a kind of optional embodiment, first modeling unit 21 each pressure-variable adsorption in establishing psa unit
When the mathematical simulation model of device, it is specifically used for:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes in psa unit and respectively become
Press the mathematical simulation model of adsorbent equipment；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIt indicates wait inhale
In attached mixed gas, the partial pressure of gas component i；BiIndicate that Langmuir absorption of the gas component i on this layer of adsorbent is normal
Number；BijIndicate Langmuir absorption of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j
Constant；KijIndicate that the component j when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j inhales component i
The influence degree of attached effect；Ki,mixIndicate suction-operated of all gas component to gas component i in mixed gas to be adsorbed
Affecting parameters.
The collaboration of hydrogen recovery system described in embodiment of the present invention optimization system can be used for executing described in above-described embodiment
Hydrogen recovery system cooperative optimization method, principle is similar with technical effect, and and will not be described here in detail.
In the description of the present invention, relational terms such as first and second and the like be used merely to an entity or
Operation is distinguished with another entity or operation, and without necessarily requiring or implying between these entities or operation, there are any
This actual relationship or sequence.Moreover, the terms "include", "comprise" or its any other variant be intended to it is non-exclusive
Property include so that include a series of elements process, method, article or equipment not only include those elements, but also
Further include other elements that are not explicitly listed, or further include for this process, method, article or equipment it is intrinsic
Element.In the absence of more restrictions, the element limited by sentence "including a ...", it is not excluded that including described
There is also other identical elements in the process, method, article or equipment of element.
The above examples are only used to illustrate the technical scheme of the present invention, rather than its limitations；Although with reference to the foregoing embodiments
Invention is explained in detail, those skilled in the art should understand that: it still can be to aforementioned each implementation
Technical solution documented by example is modified or equivalent replacement of some of the technical features；And these are modified or replace
It changes, the spirit and scope for technical solution of various embodiments of the present invention that it does not separate the essence of the corresponding technical solution.
Claims (10)
1. a kind of hydrogen recovery system cooperative optimization method characterized by comprising
Step S1: establishing the mathematical simulation model of hydrogen recovery system, the hydrogen recovery system include: psa unit and
At least one unit in film separation unit；The psa unit includes at least one pressure-swing absorption apparatus, the film point
Include at least one membrane separation device from unit, needs to select according to default in the pressure-swing absorption apparatus and the membrane separation device
It is provided with compressor module to selecting property；
Step S2: joined according to the design parameter of psa unit and film separation unit in the hydrogen recovery system and operation
Number is set into each pressure-swing absorption apparatus in the psa unit and enters each UF membrane dress in the film separation unit
The uninterrupted for the hydrogeneous stream stock set sets the adsorption equilibrium dynamics ginseng of each pressure-swing absorption apparatus in the psa unit
The component infiltration rate initial parameter value of each membrane separation device in number initial value, and the setting film separation unit；Wherein, institute
Stating the hydrogeneous stream stock in hydrogen recovery system includes the hydrogeneous stream stock for passing in and out psa unit, film separation unit, and discharge
To the hydrogeneous stream stock of oil refining gas stream system；
Step S3: Mathematical is carried out to the mathematical simulation model of the hydrogen recovery system, obtains the hydrogen recovery system
The product hydrogen of output forms and flow；
Step S4: whether product hydrogen composition and flow in judgment step S3 solving result, which meet default calculate, requires, if meeting
Default calculate requires, and thens follow the steps S5；If not meeting, pre-designed calculation is required and the number of iterations is not up to preset limit number,
In amendment step S2 into each pressure-swing absorption apparatus in the psa unit and enter each in the film separation unit
The adsorption equilibrium power of each pressure-swing absorption apparatus in the uninterrupted of the hydrogeneous stream stock of membrane separation device, the psa unit
Learn one of the component infiltration rate initial parameter value of each membrane separation device in initial parameter value and the film separation unit
Or it is a variety of, and return step S3；If not meeting, pre-designed calculation is required and the number of iterations has reached preset limit number, executes step
Rapid S5；
Step S5: the global optimization model of the hydrogen recovery system is established, and is established in the hydrogen recovery system respectively
The subsystem Optimized model of psa unit and film separation unit；
Step S6: the global optimization model of the hydrogen recovery system is initialized, and respectively to psa unit
It is initialized with the subsystem Optimized model of film separation unit；Wherein, to the global optimization model of the hydrogen recovery system
Carrying out initialization includes: the first the number of iterations upper limit of global optimization model to be arranged, and enter in the psa unit
Each pressure-swing absorption apparatus and the uninterrupted for entering the hydrogeneous stream stock of each membrane separation device in the film separation unit；Wherein,
Carrying out initialization to the subsystem Optimized model of psa unit and film separation unit includes: each subsystem Optimized model of setting
Secondary iteration maximum number of times, and receive the global optimization model specification into each transformation in the psa unit
Adsorbent equipment and the uninterrupted for entering the hydrogeneous stream stock of each membrane separation device in the film separation unit；
Step S7: respectively optimizing the subsystem Optimized model of psa unit and film separation unit, and according to
The Optimization Solution result of subsystems Optimized model determines the Optimization Solution result of global optimization model；
Wherein, the objective function of the global optimization model are as follows: the maximization product hydrogen retrieval benefit of hydrogen recovery system,
In, the product hydrogen retrieval benefit of the hydrogen recovery system is equal to the product of the psa unit and the film separation unit
The sum of hydrogen retrieval benefit；
The constraint condition of the global optimization model includes: scheduled into the hydrogeneous of psa unit in hydrogen recovery system
The difference for flowing the hydrogeneous stream plume amount of plume amount and psa unit actual treatment is less than default relaxation factor and hydrogen recycles
In system the hydrogeneous stream plume amount of the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment it
Difference is less than default relaxation factor；The constraint condition of the global optimization model further include: in the hydrogeneous stream stock of hydrogen recovery system
Pure hydrogen amount is greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen recovery system contains
Pure hydrogen amount in hydrogen stream stock is equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain and is emitted into
The sum of pure hydrogen content in the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: the scheduled transformation that enters is inhaled in hydrogen recovery system
The minimum difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and psa unit actual treatment of coupon member；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter UF membrane list
The minimum difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and film separation unit actual treatment of member；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-swing absorption apparatus in psa unit
Inlet and outlet meet conservation of matter, component conservation, raw gas pressure is greater than or equal to pressure-swing absorption apparatus inlet pressure requirements, becomes
The machining load of pressure adsorbent equipment is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or equal to default
Predetermined component gas cannot penetrate predetermined adsorption layer in Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: the disengaging of each membrane separation device in film separation unit
Mouth meets conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, membrane separation device
Machining load be within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient；
Step S8: judging whether the Optimization Solution result of global optimization model restrains, if convergence, terminates hydrogen recycling system
The Optimization Solution process of system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminate hydrogen recycling system
The Optimization Solution process of system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, return step S7 continue into
Row Optimization Solution is until each subsystem Optimized model reaches secondary iteration maximum number of times.
2. hydrogen recovery system cooperative optimization method according to claim 1, which is characterized in that the hydrogen recovery system
The design parameter of middle psa unit and film separation unit includes: height, internal diameter, temperature, the pressure of each pressure-swing absorption apparatus
Power, processing capacity, adsorbent inventory, classification, Kong Rong and specific surface area；The design temperature of each membrane separation device, pressure, choosing
Selecting property and processing capacity；The processing load limitation of compressor module in each pressure-swing absorption apparatus；It is pressed in each membrane separation device
The processing load of contracting machine module limits；
The operating parameter of psa unit and film separation unit includes: each pressure-swing absorption apparatus in the hydrogen recovery system
Operation temperature, pressure and adsorption time；The operation temperature and pressure of each membrane separation device；Flow, the composition of hydrogeneous stream stock
And pressure.
3. hydrogen recovery system cooperative optimization method according to claim 1, which is characterized in that establish hydrogen recovery system
Mathematical simulation model, comprising:
The mathematical simulation model of each pressure-swing absorption apparatus in psa unit, each UF membrane dress in film separation unit are established respectively
The mathematical simulation model and each membrane separation device of compressor module in the mathematical simulation model set, each pressure-swing absorption apparatus
The mathematical simulation model of middle compressor module.
4. hydrogen recovery system cooperative optimization method according to claim 3, which is characterized in that establish psa unit
In each pressure-swing absorption apparatus mathematical simulation model, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes each transformation in psa unit and inhale
The mathematical simulation model of adsorption device；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixed gas to be determined
The equilibrium adsorption capacity of middle gas component i on the sorbent；qmax,iIndicate that gas component i is on the sorbent in mixed gas to be determined
Maximal absorptive capacity；BiIndicate Langmuir absorption constant of the gas component i on the adsorbent；BjIndicate that gas component j exists
Langmuir absorption constant on the adsorbent；PiIndicate the partial pressure of gas component i in mixed gas to be determined；PjIndicate to
Measure the partial pressure of gas component j in mixed gas.
5. hydrogen recovery system cooperative optimization method according to claim 3, which is characterized in that establish psa unit
In each pressure-swing absorption apparatus mathematical simulation model, comprising:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes each transformation in psa unit and inhale
The mathematical simulation model of adsorption device；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIndicate to be adsorbed
In mixed gas, the partial pressure of gas component i；BiIndicate Langmuir absorption constant of the gas component i on this layer of adsorbent；Bij
Indicate Langmuir absorption constant of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j；
KijIt indicates that the component j when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j adsorbs component i to make
Influence degree；Ki,mixIndicate that all gas component influences the suction-operated of gas component i in mixed gas to be adsorbed
Parameter.
6. a kind of hydrogen recovery system cooperates with optimization system characterized by comprising
First modeling unit, for establishing the mathematical simulation model of hydrogen recovery system, the hydrogen recovery system includes: transformation
At least one unit in absorbing unit and film separation unit；The psa unit includes at least one pressure-variable adsorption dress
It sets, the film separation unit includes at least one membrane separation device, root in the pressure-swing absorption apparatus and the membrane separation device
It needs to be selectively provided with compressor module according to default；
First initial value setup unit, for setting according to psa unit in the hydrogen recovery system and film separation unit
Parameter and operating parameter are counted, each pressure-swing absorption apparatus in the psa unit is set into and enters the UF membrane list
The uninterrupted of the hydrogeneous stream stock of each membrane separation device, sets the suction of each pressure-swing absorption apparatus in the psa unit in member
The component infiltration rate parameter of each membrane separation device in attached equilibrium kinetics initial parameter value, and the setting film separation unit
Initial value；Wherein, the hydrogeneous stream stock in the hydrogen recovery system include pass in and out psa unit, film separation unit it is hydrogeneous
Stock is flowed, and is emitted into the hydrogeneous stream stock of oil refining gas stream system；
First solves unit, carries out Mathematical for the mathematical simulation model to the hydrogen recovery system, obtains the hydrogen
The product hydrogen composition and flow of gas recovery system output；
First judging unit, the product hydrogen in solving result for judging the first solution unit forms and whether flow is full
Default calculate of foot requires, and requires if meeting default calculate, executes the second modeling unit；If not meeting pre-designed calculation to require and change
Generation number is not up to preset limit number, then correct in the first initial value setup unit into the psa unit
In each pressure-swing absorption apparatus and enter the uninterrupted, described of the hydrogeneous stream stock of each membrane separation device in the film separation unit
It is each in the adsorption equilibrium kinetic parameter initial value and the film separation unit of each pressure-swing absorption apparatus in psa unit
One of component infiltration rate initial parameter value of membrane separation device is a variety of, and returns to described first and solve unit；If not
Meet default calculating requirement and the number of iterations has reached preset limit number, then executes the second modeling unit；
Second modeling unit for establishing the global optimization model of the hydrogen recovery system, and establishes the hydrogen respectively
The subsystem Optimized model of psa unit and film separation unit in recovery system；
Second initial value setup unit initializes, Yi Jifen for the global optimization model to the hydrogen recovery system
The other subsystem Optimized model to psa unit and film separation unit initializes；Wherein, the hydrogen is recycled and is
It includes: the first the number of iterations upper limit of global optimization model to be arranged, and enter institute that the global optimization model of system, which carries out initialization,
State each pressure-swing absorption apparatus and the hydrogeneous stream stock into each membrane separation device in the film separation unit in psa unit
Uninterrupted；Wherein, carrying out initialization to the subsystem Optimized model of psa unit and film separation unit includes: setting
The secondary iteration maximum number of times of each subsystem Optimized model, and receive the global optimization model specification into the transformation
Each pressure-swing absorption apparatus and the flow into the hydrogeneous stream stock of each membrane separation device in the film separation unit in absorbing unit
Size；
Second solves unit, optimizes and asks for the subsystem Optimized model respectively to psa unit and film separation unit
It solves, and determines the Optimization Solution result of global optimization model according to the Optimization Solution result of subsystems Optimized model；
Wherein, the constraint condition of the global optimization model includes: scheduled into psa unit in hydrogen recovery system
Hydrogeneous stream plume amount and the difference of hydrogeneous stream plume amount of psa unit actual treatment be less than default relaxation factor, Yi Jiqing
The hydrogeneous stream stock of the scheduled hydrogeneous stream plume amount into film separation unit and film separation unit actual treatment in gas recovery system
The difference of flow is less than default relaxation factor；The constraint condition of the global optimization model further include: the hydrogeneous stream of hydrogen recovery system
Pure hydrogen amount in stock is greater than or equal to the pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain；Hydrogen recycling
Pure hydrogen amount in the hydrogeneous stream stock of system be equal to pure hydrogen amount in the product hydrogen that psa unit and film separation unit obtain and
It is emitted into the sum of pure hydrogen content in the hydrogeneous stream stock of gas train；
The objective function of the psa unit subsystem Optimized model are as follows: the scheduled transformation that enters is inhaled in hydrogen recovery system
The minimum difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and psa unit actual treatment of coupon member；
The objective function of the film separation unit subsystem Optimized model are as follows: scheduled in hydrogen recovery system to enter UF membrane list
The minimum difference of the hydrogeneous stream plume amount of the hydrogeneous stream plume amount and film separation unit actual treatment of member；
The constraint condition of the psa unit subsystem Optimized model are as follows: each pressure-swing absorption apparatus in psa unit
Inlet and outlet meet conservation of matter, component conservation, raw gas pressure is greater than or equal to pressure-swing absorption apparatus inlet pressure requirements, becomes
The machining load of pressure adsorbent equipment is within the scope of pressure-swing absorption apparatus working ability, and product hydrogen hydrogen purity is greater than or equal to default
Predetermined component gas cannot penetrate predetermined adsorption layer in Reinheitszahl and unstripped gas；
The constraint condition of the film separation unit subsystem Optimized model are as follows: the disengaging of each membrane separation device in film separation unit
Mouth meets conservation of matter, component conservation, and raw gas pressure is greater than or equal to membrane separation device inlet pressure requirements, membrane separation device
Machining load be within the scope of membrane separation device working ability and in unstripped gas without containing designated gas ingredient；
Second judgment unit, if convergence, terminates described for judging whether the Optimization Solution result of global optimization model restrains
The Optimization Solution process of hydrogen recovery system；If not converged but the number of iterations reaches the first the number of iterations upper limit, terminate described
The Optimization Solution process of hydrogen recovery system；If not converged and the number of iterations is not up to the first the number of iterations upper limit, is returned
Two solution units continue Optimization Solution until each subsystem Optimized model reaches secondary iteration maximum number of times.
7. hydrogen recovery system according to claim 6 cooperates with optimization system, which is characterized in that the hydrogen recovery system
The design parameter of middle psa unit and film separation unit includes: height, internal diameter, temperature, the pressure of each pressure-swing absorption apparatus
Power, processing capacity, adsorbent inventory, classification, Kong Rong and specific surface area；The design temperature of each membrane separation device, pressure, choosing
Selecting property and processing capacity；The processing load limitation of compressor module in each pressure-swing absorption apparatus；It is pressed in each membrane separation device
The processing load of contracting machine module limits；
The operating parameter of psa unit and film separation unit includes: each pressure-swing absorption apparatus in the hydrogen recovery system
Operation temperature, pressure and adsorption time；The operation temperature and pressure of each membrane separation device；Flow, the composition of hydrogeneous stream stock
And pressure.
8. hydrogen recovery system according to claim 6 cooperates with optimization system, which is characterized in that first modeling unit
It is specifically used in the mathematical simulation model for establishing hydrogen recovery system:
The mathematical simulation model of each pressure-swing absorption apparatus in psa unit, each UF membrane dress in film separation unit are established respectively
The mathematical simulation model and each membrane separation device of compressor module in the mathematical simulation model set, each pressure-swing absorption apparatus
The mathematical simulation model of middle compressor module.
9. hydrogen recovery system according to claim 8 cooperates with optimization system, which is characterized in that first modeling unit
In establishing psa unit when the mathematical simulation model of each pressure-swing absorption apparatus, it is specifically used for:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes each transformation in psa unit and inhale
The mathematical simulation model of adsorption device；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIndicate the coverage rate of gas component i on adsorbent in mixed gas to be determined；qiIndicate mixed gas to be determined
The equilibrium adsorption capacity of middle gas component i on the sorbent；qmax,iIndicate that gas component i is on the sorbent in mixed gas to be determined
Maximal absorptive capacity；BiIndicate Langmuir absorption constant of the gas component i on the adsorbent；BjIndicate that gas component j exists
Langmuir absorption constant on the adsorbent；PiIndicate the partial pressure of gas component i in mixed gas to be determined；PjIndicate to
Measure the partial pressure of gas component j in mixed gas.
10. hydrogen recovery system according to claim 8 cooperates with optimization system, which is characterized in that first modeling is single
Member when the mathematical simulation model of each pressure-swing absorption apparatus, is specifically used in establishing psa unit:
Using absorbing balance equation, mass transfer rate equation and total mass transfer equilibrium equation, establishes each transformation in psa unit and inhale
The mathematical simulation model of adsorption device；
Wherein, the absorbing balance equation are as follows:
Wherein, θiIt indicates in mixed gas to be adsorbed, the coverage rate of gas component i on certain layer of adsorbent；PiIndicate to be adsorbed
In mixed gas, the partial pressure of gas component i；BiIndicate Langmuir absorption constant of the gas component i on this layer of adsorbent；Bij
Indicate Langmuir absorption constant of the component i on this layer of adsorbent in the binary gas mixture comprising component i and component j；
KijIt indicates that the component j when adsorbing on this layer of adsorbent of the binary gas mixture comprising component i and component j adsorbs component i to make
Influence degree；Ki,mixIndicate that all gas component influences the suction-operated of gas component i in mixed gas to be adsorbed
Parameter.
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