CN109684769A - Bubble scale regulation-control model modeling method under the conditions of the pure pneumatic operation of MIHA - Google Patents
Bubble scale regulation-control model modeling method under the conditions of the pure pneumatic operation of MIHA Download PDFInfo
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- 239000007789 gas Substances 0.000 description 67
- 239000003921 oil Substances 0.000 description 15
- 230000003519 ventilatory effect Effects 0.000 description 12
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 8
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- 229910052717 sulfur Inorganic materials 0.000 description 5
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 4
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- 125000003118 aryl group Chemical group 0.000 description 2
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- 239000010747 number 6 fuel oil Substances 0.000 description 2
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- 229930192474 thiophene Natural products 0.000 description 2
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- GWZOLWLJEJRQMZ-UHFFFAOYSA-N [S].S Chemical compound [S].S GWZOLWLJEJRQMZ-UHFFFAOYSA-N 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
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Abstract
The present invention relates to bubble scale regulation-control model modeling methods under the conditions of the pure pneumatic operation of MIHA to establish the energy conversion model in bubble breaker by analyzing bubble formation process under pure aerodynamic conditions；Based on the energy conversion model and liquid circulation in bubble breaker, fluid flow is calculated, obtains the strong mixed zone energy absorbing device of gas-liquid, it is final to obtain bubble scale computation model.Method of the invention establishes bubble scale regulation-control model under the conditions of pure pneumatic operation for MIHA, the concentrated expression influence of structure of reactor, system physical property and operating parameter and input energy to bubble scale, the guidance of the reaction system design to reactor design and MIHA, the efficient structure of reactor of design and reaction system can be achieved.
Description
Technical field
The invention belongs to reactors, modeling technique field, and in particular to bubble scale tune under the conditions of the pure pneumatic operation of MIHA
Control model modelling approach.
Background technique
The considerations of for global environmental protection, bunker fuel oil must reduce sulfur content, such as high sea bunker fuel oil sulfur-bearing
Amount must be down to 0.5%, therefore, imperative with low-sulfur distillate fuel oil substitution high-sulfur residual fuel oil.Most of sulphur in crude oil
It is present in residual oil, the sulphur in residual oil is mainly distributed on aromatic hydrocarbons, in resin and asphalt, wherein most sulphur are with pentacyclic
The form of thiophene and thiophene derivant exists.It is usually used and is disconnected the C-S key of residual oil macromolecular by hydrogenolysis, make sulphur
Hydrogen sulfide is converted into remove the sulphur in residual oil.The sulphur being present in non-asphaltene is easier to remove under hydroconversion condition, reachable
To higher conversion level.But since asphalitine is that relative molecular mass is maximum, structure is most complicated in residual oil, polarity is strongest big
Molecule, sulphur therein are difficult to remove, and cause the desulfurization degree in hydrodesulfurization of residual oil limited.
During (calling MIHA in the following text) is reacted in residuum hydrodesulfurization, the conversion of chirvinskite matter is most important.Asphalitine
Core is highly condensed condensed aromatic ring system.Around its condensed aromatic ring system with quantity and differ in size alkyl,
Cyclic alkyl structure is the maximum component of condensation degree in residual oil, simultaneously containing hetero atoms, form and molecular structures such as S, N, O, metals
It is complicated.During residuum hydroconversion, the cracking for becoming small molecule by macromolecular and small molecule dehydrogenation mainly occur for asphalitine
The contrary reaction of two class of condensation of polymerization generation macromolecular.The present invention is using asphalitine hydrodesulfurization reaction as residual hydrogenation
The model reaction of process investigates structure of reactor, system physical property and operating parameter and input energy in bubble breaker
The influence of bubble scale.
Summary of the invention
The purpose of the present invention is to provide bubble scale regulation-control model modeling methods under the conditions of the pure pneumatic operation of MIHA, to grind
Structure of reactor, system physical property and operating parameter and input energy are studied carefully to bubble scale d32Influence, thus realize pair
The guidance of MIHA reactor design and the design of the reaction system of MIHA.
Three kinds of modes can be used in the formation of MIHA microbubble, it may be assumed that pure to surge, is pure pneumatic and gas-liquid linked.It is pure surge with it is pure
Under the conditions of pneumatic operation, system running and microbubble form required energy and can be mentioned by liquid machine energy or gas-static completely
For；Under gas-liquid linked operating condition, needed for gas-static energy and liquid machine can provide system running simultaneously and microbubble formed
Energy.Bubble scale regulation-control model modeling method is established micro- according to aforementioned research under the conditions of the present invention has inquired into pure pneumatic operation
Bubble Sauter average diameter d32The key of mathematical model is bubble breaker self-energy dissipative shock wave ε in MIHAmixComputation model
Research is based on this, and the method for the present invention includes following steps:
S100. bubble formation process under pure aerodynamic conditions is analyzed, the energy conversion model in bubble breaker is established；
Under the conditions of pure pneumatic operation, fluid flow QL< < gas flow QG, before not being passed through gas, filled in bubble breaker
Full arrest reaction liquid；Assuming that system liquid is closed cycle, i.e., amount of liquid does not change in whole process；Due to gas into
Enter, causes partially liq that will be forced into bubble breaker external circulation line；Bubble breaker length is set as L, diameter D1,
Cross-sectional area S1=π D1 2/4；Nozzle diameter is DN；
It is as follows to make hypothesis:
(1) steady state operation, operating pressure PmIt is constant；
(2) since practical operation pressure is higher, therefore ignore caused by variation and the bubble interface tension of liquid potential energy
The variation of gas pressure in bubble；
(3) since gas density is much smaller than liquid, therefore ignore the kinetic energy of input gas；
Using bubble breaker as control volume, the energy balance under limit is carried out；Under aerodynamic conditions, pressure PG0、
Volume flow is QG0Gas to enter operating pressure constant for PmBubble breaker when, air relief divides static energy, conversion
For liquid kinetic energy and bubble surface energy；The static energy of gas release is equivalent to gas to system work done WG, can according to work done definition
Know:
QGFor gas flow in bubble breaker, it is assumed that gas is perfect gas, then can according to The Ideal-Gas Equation
:
In formula (2), ρG0And MA(respectively enter the gas density and gas molar quality of destroyer；R and T is respectively gas
Body constant and gas temperature；
Formula (2), which are substituted into formula (1) and are integrated, to be obtained:
Enabling the difference of gas pressure and operating pressure at bubble breaker gas access is Δ P, it may be assumed that
Δ P=PG0-Pm (32)
Due to Δ P > 0, WGIts mechanical energy will reduce after < 0, i.e. gas enter bubble breaker；Since bubble is broken
Millstone operating pressure PmIt is constant, and in contrast, liquid gravitational potential energy is negligible, therefore the mechanical energy that gas is reduced will convert
For liquid kinetic energy and bubble interface energy；Therefore following relationship can be obtained by formula (3) (4):
Equation (5) left side of the equal sign is the reduction of gas-static energy, i.e.-WG；Equation (5) right side of the equal sign two are respectively liquid
Kinetic energy and gas-liquid interface energy；Wherein, ρLAnd σLRespectively fluid density and interfacial tension；ULFor the liquid that is flowed out from destroyer
Linear velocity；d32For the bubble Sauter average diameter flowed out from bubble breaker；According to mass balance, QGWith QG0Just like ShiShimonoseki
System:
Due to Δ P < < Pm, therefore QG≈QG0；Primary Calculation shows that gas-liquid interface can be worth can relative to liquid kinetic energy values
To ignore, therefore, equation (5) can simplify are as follows:
S200. based on the energy conversion model and liquid circulation in bubble breaker, fluid flow is calculated；
Since the liquid of disengaging destroyer is closed cycle, i.e. disengaging fluid flow is equal, therefore has:
QL=ULS1(1-φG) (36)
Wherein, gas holdup φ in bubble breakerGIt is calculated as follows:
By (8) (9) Shi Ke get:
ULFor the superficial velocity of gas-liquid mixture in bubble breaker, formula (10) substitution equation (7) can be obtained:
It can be calculated by equation (11) because of nozzle diameter fluid flow Q caused by gas inputL, it can be obtained by equation (7):
Under the conditions of pure pneumatic operation, QL<<QG, then equation (11) are simplified are as follows:
Thus it obtains:
By perfect condition equation it is found that there are following relationships:
Formula (15) substitution equation (14) can be obtained:
From equation (16): bubble breaker cross-sectional area S1To liquid circulation flow QLIt influences bigger；
Due to:
V in formulaNFor flow velocity at nozzle；
Work as VNOne timing, can be obtained by formula (16) and (17):
Work as DNOne timing, can be obtained by formula (16) and (17):
It can be obtained by formula (10) and (16):
Thus it completes under pure aerodynamic conditions to QLEstimation；
S300. the strong mixed zone energy absorbing device ε of gas-liquid is calculatedmix；
It can be obtained according to the first law of thermodynamics:
In above formula, LmixSection length, m are mixed strongly for gas-liquid in bubble breaking；λ1For the ratio between gas-liquid volume flow, λ1=
QG/QL；K1For bubble breaker nozzle diameter and destroyer diameter ratio, K1=DN/D1；
LmixDecay in bubble breaking area with liquid peak flow rate (PFR) until the length to disappear is related, liquid peak flow rate (PFR) exists
In its attenuation process, center line velocity UjmAttenuation law do not influenced by bubble disturbance around it, and meet following decaying
Rule:
In equation (22), x is the horizontal distance at bubble breaker core to maximum speed.Work as UjmDecay to gas-liquid mixed
Object superficial velocity ULWhen, high speed disappears, and will form uniform gas-liquid mixed logistics later；Therefore, LmixFor Ujm=ULWhen x value,
That is:
To can be obtained after equation (23) abbreviation:
It can be obtained after equation (24) are substituted into (21) and abbreviation:
Association type (16) (20) and equation (25) can calculate εmix。
S400. the bubble scale of microbubble in MIHA is calculated；
Microbubble d in MIHA32It can be calculated based on the first research of inventor；
dmax=0.75 (σL/ρL)0.6εmix-0.4 (54)
dmin=11.4 (μL/ρL)0.75εmix -0.25 (55)
Wherein, dminFor bubble minimum diameter；dmaxFor bubble maximum gauge；μLFor hydrodynamic viscosity.
Another object of the present invention is to provide bubble scale tune under the conditions of the pure pneumatic operation of MIHA of above method building
Control model.
Another object of the present invention is to provide the reactor of above method design.
Structure of reactor of the invention can be found in the patent CN106187660A of inventor's earlier application, in the present invention no longer
It repeats.Model reaction device structure, system physical property and operating parameter and input energy in the present invention using building is to bubble
The influence of scale, so as to carry out relevant structure of reactor parameter designing according to the demand to bubble scale.
Method of the invention establishes bubble scale regulation-control model under the conditions of pure pneumatic operation, concentrated expression for MIHA
The influence of structure of reactor, system physical property and operating parameter and input energy to bubble scale is, it can be achieved that set reactor
The guidance of the reaction system of meter and MIHA design, the efficient structure of reactor of design and reaction system.
Detailed description of the invention
Fig. 1 is bubble formation process physical model schematic diagram under pure aerodynamic conditions；
Fig. 2 is operation temperature to bubble scale d32Influence；
Fig. 3 is gas supply pressure differential deltap P to bubble scale d32Influence；
Fig. 4 is gas supply pressure differential deltap P to energy absorbing device εmixInfluence；
Fig. 5 is gas supply pressure differential deltap P to gas holdup φGInfluence；
Fig. 6 is ventilatory capacity QGTo bubble scale d32Influence；
Fig. 7 is ventilatory capacity QGTo energy absorbing device εmixInfluence；
Fig. 8 is ventilatory capacity QGTo gas holdup φGInfluence.
Specific embodiment
Explanation and specific embodiment are further elaborated technical solution of the present invention with reference to the accompanying drawing.
Embodiment 1
S100. bubble formation process under pure aerodynamic conditions is analyzed, the energy conversion model in bubble breaker is established；
Arrest reaction liquid is filled with before not being passed through gas, in bubble breaker.After starting to be passed through gas, due to gas
Pressure PGWith system operating pressure PmBetween there are pressure differential deltap P, gas-static can will be passed to liquid, promote liquid occur turbulence,
And gas pressure itself is rapidly reduced to the operating pressure in MIHA.Due to the flowing of gas-liquid two-phase, gas-liquid is from bubble breaker
Outflow.For pneumatic operation condition, fluid flow QLMuch smaller than gas flow QG, energy needed for system is run is almost
It can be provided by gas pressure.
Establish physical model schematic diagram as shown in Figure 1:
Assuming that system liquid is closed cycle, i.e., amount of liquid does not change in whole process.Due to the entrance of gas, lead
Cause partially liq that will be forced into bubble breaker external circulation line.Bubble breaker length is set as L (m), diameter D1
(m), cross-sectional area S1(m2)(S1=π D1 2/4).Nozzle diameter is DN(m)。
It is as follows to make hypothesis:
(1) steady state operation, operating pressure PmIt is constant；
(2) since practical operation pressure is higher, therefore ignore caused by variation and the bubble interface tension of liquid potential energy
The variation of gas pressure in bubble；
(3) since gas density is much smaller than liquid, therefore ignore the kinetic energy of input gas.
Using bubble breaker as control volume, the energy balance under limit is carried out.Under aerodynamic conditions, pressure PG0
(Pa), volume flow QG0(m3/ s) gas to enter operating pressure constant for Pm(Pa) when bubble breaker, gas release
Part static energy is converted into liquid kinetic energy and bubble surface energy.The static energy of gas release is equivalent to gas to system work done WG
(W), according to known to work done definition:
QG(m3/ s) it is gas flow in bubble breaker, for simplicity, it is assumed that and in the range of present invention research, gas
Body is perfect gas, then can obtain according to The Ideal-Gas Equation:
In formula (2), ρG0(Kg/m3) and MAIt (Kg/mol) is respectively the gas density and molal weight for entering destroyer；R
(8.314J/mol.K) and T (K) are respectively gas constant and gas temperature.
Formula (2), which are substituted into formula (1) and are integrated, to be obtained:
Enabling the difference of gas pressure and operating pressure at bubble breaker gas access is Δ P (Pa), it may be assumed that
Δ P=PG0-Pm (60)
Due to Δ P > 0, WGIts mechanical energy will reduce after < 0, i.e. gas enter bubble breaker.Since bubble is broken
Millstone operating pressure PmIt is constant, and in contrast, liquid gravitational potential energy is negligible, therefore the mechanical energy that gas is reduced will convert
For liquid kinetic energy and bubble interface energy.Therefore following relationship can be obtained by formula (3) (4):
Equation (5) left side is the reduction (- W of gas-static energyG), also as energy source needed for system running；Equation
(5) two, the right is respectively liquid kinetic energy and gas-liquid interface energy.Wherein, ρL(Kg/m3) and σL(N/m) be respectively fluid density and
Interfacial tension；UL(m/s) linear velocity of the liquid flowed out from destroyer；d32(m) bubble to be flowed out from bubble breaker
Sauter average diameter；According to mass balance, QGWith QG0There is following relationship:
For research of the invention, Δ P < < Pm, therefore, QG≈QG0.For sake of convenience, it is hereinafter referred to as enter and
The gas flow of outflow is with QGIt indicates.Primary Calculation shows that gas-liquid interface can be worth can ignore relative to liquid kinetic energy values.This
Text ignores this first, is then checked by calculating.Therefore, equation (5) can simplify are as follows:
S200. based on the energy conversion model and liquid circulation in bubble breaker, fluid flow is calculated；
According to closed cycle above it is assumed that disengaging fluid flow is equal, therefore have
QL=ULS1(1-φG) (64)
Wherein, gas holdup φ in bubble breakerGIt can be calculated as follows:
By (8) (9) Shi Ke get:
Obviously, ULFor the superficial velocity of gas-liquid mixture in bubble breaker.Formula (10) substitution equation (7) can be obtained:
It can be calculated by equation (11) because of nozzle diameter fluid flow Q caused by gas inputL, but form is more complex,
It must make Rational Simplification according to this project actual conditions.It can be obtained by equation (7):
Calculation shows that under conditions of present invention research, QL<<QG.Therefore equation (11) can simplify are as follows:
Thus it obtains:
In fact, by perfect condition equation it is found that there are following relationships:
Formula (15) substitution equation (14) can be obtained:
From equation (16): bubble breaker cross-sectional area S1To liquid circulation flow QLIt influences bigger；
Due to:
V in formulaNFor flow velocity at nozzle；
Work as VNOne timing, can be obtained by formula (16) and (17):
Work as DNOne timing, can be obtained by formula (16) and (17):
It can be obtained by formula (10) and (16):
It is based on to Q under full aerodynamic conditions aboveLRough calculation.And then according to known VNDetermine diameter DN(work as DNCentainly
When, V can also be acquiredN)。
S300. the strong mixed zone energy absorbing device ε of gas-liquid is calculatedmix；
d32With the strong mixed zone energy absorbing device ε of gas-liquid in bubble breakermixIt is closely related.It is fixed according to thermodynamics first
Lv Ke get:
In above formula, LmixSection length, m are mixed strongly for gas-liquid in bubble breaking；λ1For the ratio between gas-liquid volume flow (λ1=
QG/QL)。K1For bubble breaker nozzle diameter and destroyer diameter ratio (K1=DN/D1)。
Evans etc. has been derived by L according to kinetic energy conservation principlemixMathematical model, but can not be suitable for the present invention
The involved situation of research, it is therefore desirable to re-start derivation.Present invention research thinks, LmixWith liquid peak flow rate (PFR) in bubble
Decaying in fracture area is until the length to disappear is related.Liquid peak flow rate (PFR) is in its attenuation process, center line velocity Ujm's
Attenuation law is not influenced by bubble disturbance around it, and meets following attenuation law:
In equation (22), x is the horizontal distance at bubble breaker core to maximum speed.Work as UjmDecay to gas-liquid mixed
Object superficial velocity ULWhen, high speed disappears, and will form uniform gas-liquid mixed logistics later.Therefore, LmixFor Ujm=ULWhen x value.
That is:
To can be obtained after equation (23) abbreviation:
It can be obtained after equation (24) are substituted into (21) and abbreviation:
Association type (16) (20) and equation (25) can calculate εmix。
S400. the bubble scale of microbubble in MIHA is calculated；
Microbubble d in MIHA32It is calculated according to following formula；
dmax=0.75 (σL/ρL)0.6εmix -0.4 (82)
dmin=11.4 (μL/ρL)0.75εmix -0.25 (83)
Wherein, dminFor bubble minimum diameter；dmaxFor bubble maximum gauge；μLFor hydrodynamic viscosity.
Embodiment 2
The present embodiment illustrates the bubble scale regulation-control model of the building of the method based on embodiment 1.
It is as follows that modeling method based on embodiment 1 obtains bubble scale regulation-control model:
dmax=0.75 (σL/ρL)0.6εmix -0.4 (89)
dmin=11.4 (μL/ρL)0.75εmix -0.25 (90)
Embodiment 3
Modeling method of the present embodiment based on embodiment 1 is operated for specific structure of reactor and reaction system research
Influence of the temperature to bubble scale, and gas supply pressure differential deltap P and ventilatory capacity QGTo bubble scale, energy absorbing device εmixIt is gentle to contain
Rate φGInfluence.
(1) operation temperature is to bubble scale d32Influence；
Design conditions are as follows:
Destroyer diameter D1=0.02m；Bubble breaker nozzle diameter and destroyer diameter ratio K1=0.5；
Ventilatory capacity 80L/h；Residual oil density pL=800Kg/m3；
Residual oil interfacial tension σLFitting formula is as follows:
σL=[31.74-0.04775 (T+273.15)] × 10-3(N/m)；
Residual oil dynamic viscosity μLFitting formula is as follows；
Operating pressure Pm=14MPa；Supply pressure differential deltap P=6MPa；Gas temperature T=400~500 DEG C.
Operation temperature is to d32Influence as shown in Figure 2；As can be seen that increasing system temperature is conducive to bubble d32Reduction.
This is mainly due to temperature raising, residual oil viscosity and surface tension reduce, and lead to d in systemminAnd dmaxCaused by reduction.
(2) gas supply pressure differential deltap P is to bubble scale d32Influence；
Design conditions are as follows:
Destroyer diameter D1=0.02m；Bubble breaker nozzle diameter and destroyer diameter ratio K1=0.5；
Residual oil density pL=800Kg/m3；Operating pressure Pm=14MPa；Supply pressure differential deltap P=1~10MPa；Gas temperature T
=450 DEG C.
As a result as shown in Figure 3 (ventilatory capacity 80L/h)；
(3) gas supply pressure differential deltap P is to energy absorbing device εmixInfluence；
Design conditions are the same as (2)；Pressure differential deltap P is supplied to energy absorbing device εmixInfluence it is as shown in Figure 4；
(4) gas supply pressure differential deltap P is to gas holdup φGInfluence；
Design conditions are the same as (2)；As a result as shown in Figure 5；
As can be seen that increasing for draught head, bubble breaker energy absorbing device increases, and bubble diameter reduces, gas holdup drop
It is low.The enhancing of liquid turbulence degree causes energy absorbing device increase and bubble to reduce in bubble breaker, finally to mass transfer and macroscopic view
Reaction rate has an impact.
(5) ventilatory capacity QGTo bubble scale d32Influence；
Design conditions are as follows:
Destroyer diameter D1=0.02m；Bubble breaker nozzle diameter and destroyer diameter ratio K1=0.5；
Ventilatory capacity QG=1~100L/h；Residual oil density pL=800Kg/m3；Operating pressure Pm=14MPa；Supply pressure differential deltap P
=0.1~10MPa；T=500 DEG C of gas temperature.
As a result as shown in Figure 6；
(6) ventilatory capacity QGTo energy absorbing device εmixInfluence；
Design conditions are with (5), as a result as shown in Figure 7；
(7) ventilatory capacity QGTo gas holdup φGInfluence；
Design conditions are with (5), as a result as shown in Figure 8；
As can be seen that working as QGWhen smaller, d32With QGIncrease and quickly reduce；Work as QGWhen larger, to d32Influence compared with
It is small.Energy absorbing device in the bubble breaker approximate linear increase tendency with the increase of ventilatory capacity, gas holdup in reactor
Increase with the increase of ventilatory capacity.
Claims (3)
1. bubble scale regulation-control model modeling method under the conditions of a kind of pure pneumatic operation of MIHA, which is characterized in that including walking as follows
It is rapid:
S100. bubble formation process under pure aerodynamic conditions is analyzed, the energy conversion model in bubble breaker is established；
Under the conditions of pure pneumatic operation, fluid flow QL< < gas flow QG, before not being passed through gas, full of quiet in bubble breaker
Only reaction solution；Assuming that system liquid is closed cycle, i.e., amount of liquid does not change in whole process；Due to the entrance of gas,
Cause partially liq that will be forced into bubble breaker external circulation line；Bubble breaker length is set as L, diameter D1, horizontal
Sectional area S1=π D1 2/4；Nozzle diameter is DN；
It is as follows to make hypothesis:
(1) steady state operation, operating pressure PmIt is constant；
(2) since practical operation pressure is higher, thus ignore liquid potential energy variation and bubble interface tension caused by bubble
The variation of interior gas pressure；
(3) since gas density is much smaller than liquid, therefore ignore the kinetic energy of input gas；
Using bubble breaker as control volume, the energy balance under limit is carried out；Under aerodynamic conditions, pressure PG0, volume
Flow is QG0Gas to enter operating pressure constant for PmBubble breaker when, air relief divides static energy, is converted into liquid
Body kinetic energy and bubble surface energy；The static energy of gas release is equivalent to gas to system work done WG, according to known to work done definition:
QGFor gas flow in bubble breaker, it is assumed that gas is perfect gas, then can obtain according to The Ideal-Gas Equation:
In formula (2), ρG0And MA(respectively enter the gas density and gas molar quality of destroyer；R and T is respectively that gas is normal
Several and gas temperature；
Formula (2), which are substituted into formula (1) and are integrated, to be obtained:
Enabling the difference of gas pressure and operating pressure at bubble breaker gas access is Δ P, it may be assumed that
Δ P=PG0-Pm(4)
Due to Δ P > 0, WGIts mechanical energy will reduce after < 0, i.e. gas enter bubble breaker；Due to bubble breaker
Operating pressure PmIt is constant, and in contrast, liquid gravitational potential energy is negligible, therefore the mechanical energy that gas is reduced translates into liquid
Body kinetic energy and bubble interface energy；Therefore it can be obtained by formula (3) (4):
Equation (5) left side of the equal sign is the reduction of gas-static energy, i.e.-WG；Equation (5) right side of the equal sign two are respectively liquid kinetic energy
With gas-liquid interface energy；Wherein, ρLAnd σLRespectively fluid density and interfacial tension；ULLinear speed for the liquid flowed out from destroyer
Degree；d32For the bubble Sauter average diameter flowed out from bubble breaker；According to mass balance, QGWith QG0There is following relationship:
Due to Δ P < < Pm, therefore QG≈QG0；Primary Calculation shows that gas-liquid interface can be worth can neglect relative to liquid kinetic energy values
Slightly, therefore, equation (5) are simplified are as follows:
S200. based on the energy conversion model and liquid circulation in bubble breaker, fluid flow is calculated；
Since the liquid of disengaging destroyer is closed cycle, i.e. disengaging fluid flow is equal, therefore has:
QL=ULS1(1-φG) (8)
Wherein, gas holdup φ in bubble breakerGIt is calculated as follows:
By (8) (9) Shi Ke get:
ULFor the superficial velocity of gas-liquid mixture in bubble breaker, formula (10) substitution equation (7) can be obtained:
It can be calculated by equation (11) because of nozzle diameter fluid flow Q caused by gas inputL, it can be obtained by equation (7):
Under the conditions of pure pneumatic operation, QL<<QG, then equation (11) are simplified are as follows:
Thus it obtains:
By perfect condition equation it is found that there are following relationships:
Formula (15) substitution equation (14) can be obtained:
From equation (16): bubble breaker cross-sectional area S1To liquid circulation flow QLIt influences bigger；
Due to:
V in formulaNFor flow velocity at nozzle；
Work as VNOne timing, can be obtained by formula (16) and (17):
Work as DNOne timing, can be obtained by formula (16) and (17):
It can be obtained by formula (10) and (16):
Thus it completes under pure aerodynamic conditions to QLEstimation；
S300. the strong mixed zone energy absorbing device ε of gas-liquid is calculatedmix；
It can be obtained according to the first law of thermodynamics:
In above formula, LmixSection length, m are mixed strongly for gas-liquid in bubble breaking；λ1For the ratio between gas-liquid volume flow, λ1=QG/QL；
K1For bubble breaker nozzle diameter and destroyer diameter ratio, K1=DN/D1；
LmixDecay in bubble breaking area with liquid peak flow rate (PFR) until the length to disappear is related, liquid peak flow rate (PFR) declines at it
During subtracting, center line velocity UjmAttenuation law do not influenced by bubble disturbance around it, and meet following attenuation law:
In equation (22), x is the horizontal distance at bubble breaker core to maximum speed；Work as UjmDecay to gas-liquid mixture table
See speed ULWhen, high speed disappears, and will form uniform gas-liquid mixed logistics later；Therefore, LmixFor Ujm=ULWhen x value, it may be assumed that
To can be obtained after equation (23) abbreviation:
It can be obtained after equation (24) are substituted into (21) and abbreviation:
Association type (16) (20) and equation (25) can calculate εmix；
S400. the bubble scale of microbubble in MIHA is calculated；
Microbubble d in MIHA32It is calculated according to following formula；
dmax=0.75 (σL/ρL)0.6εmix -0.4 (26)
dmin=11.4 (μL/ρL)0.75εmix -0.25 (27)
Wherein, dminFor bubble minimum diameter；dmaxFor bubble maximum gauge；μLFor hydrodynamic viscosity.
2. bubble scale regulation-control model under the conditions of the pure pneumatic operation of MIHA of claim 1 the method building.
3. the reactor of claim 1 the method design.
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| CN110245434A (en) * | 2019-06-18 | 2019-09-17 | 南京延长反应技术研究院有限公司 | Hydrogen transmits regulation-control model modeling method under the conditions of the pure pneumatic operation of MIHA |
| CN113035285A (en) * | 2021-04-01 | 2021-06-25 | 南京延长反应技术研究院有限公司 | Method for calculating influence of microbubble size on oil product hydrodesulfurization effect |
| CN113075091A (en) * | 2021-02-24 | 2021-07-06 | 南京延长反应技术研究院有限公司 | Method for determining size of bubbles in TA system prepared by PX oxidation |
| WO2023077844A1 (en) | 2021-11-08 | 2023-05-11 | 南京延长反应技术研究院有限公司 | Method for evaluating microbubble enhancement in system for preparing hydrogen peroxide by means of anthraquinone process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110245434A (en) * | 2019-06-18 | 2019-09-17 | 南京延长反应技术研究院有限公司 | Hydrogen transmits regulation-control model modeling method under the conditions of the pure pneumatic operation of MIHA |
| CN110245434B (en) * | 2019-06-18 | 2023-06-27 | 南京延长反应技术研究院有限公司 | Modeling method of hydrogen transmission regulation model under MIHA pure pneumatic operation condition |
| CN113075091A (en) * | 2021-02-24 | 2021-07-06 | 南京延长反应技术研究院有限公司 | Method for determining size of bubbles in TA system prepared by PX oxidation |
| CN113075091B (en) * | 2021-02-24 | 2023-01-10 | 南京延长反应技术研究院有限公司 | Method for determining size of bubbles in TA system prepared by PX oxidation |
| CN113035285A (en) * | 2021-04-01 | 2021-06-25 | 南京延长反应技术研究院有限公司 | Method for calculating influence of microbubble size on oil product hydrodesulfurization effect |
| WO2023077844A1 (en) | 2021-11-08 | 2023-05-11 | 南京延长反应技术研究院有限公司 | Method for evaluating microbubble enhancement in system for preparing hydrogen peroxide by means of anthraquinone process |
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