CN105467939B - A kind of optimization method of ethane cracking furnace production run - Google Patents
A kind of optimization method of ethane cracking furnace production run Download PDFInfo
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Abstract
The invention provides a kind of optimization method of ethane cracking furnace production run, wherein, this method includes：1：The geometric model of ethane cracking furnace is established, obtains the operational factor outside cracking of ethylene furnace radiant coil；2：The geometric model of cracking of ethylene furnace radiant coil is established, obtains the operational factor of ethane cracking furnace；3：Using 2 result of calculation as condition iteration 1, coupled simulation calculating is carried out；4：When the temperature of the combustion air is increased to 1 DEG C 200 DEG C, the fuel flow rate after calculating is adjusted to 0.9Q 1Q；5：Using 4 result of calculation as condition iteration 2, until pyrolysis furnace operational factor is better than the pyrolysis furnace operational factor before combustion air temperature rise；6：Coupling calculates again.The present invention one is that solve the problems, such as ethane cracking furnace combustion bottom burner combustion air temperature and its radiant section flue gas situation, and another is to provide guidance and optimization for pyrolysis furnace production run.
Description
Technical field
The present invention relates to ethane cracking furnace field, furtherly, is related to a kind of optimization of ethane cracking furnace production run
Method.
Background technology
Ethene is the basic material of petrochemical industry, is referred to as " mother of petrochemical industry ".Ethylene product direct relation plastics, rubber
The development of the industries such as glue, weaving, auxiliary agent, chemical machinery, building, transport and food and drink.About 98% ethene is logical in the world at present
Cross pipes type steaming thermal cracking process and produce what is obtained, therefore, researcher surrounds process units --- the pyrolysis furnace of ethene all the time
Carry out research of technique, and towards improve yield of light olefins, reduce energy consumption, reduce cost and adapt to market economy change direction
Carry out the work.
According to the important requirement of national " 12 " the development of the petrochemical industry, domestic ethylene industry by change development mode,
Implement structural adjustment and focus on scientific development.Embodiment is as follows：From simple large-scale production primary industrial chemicals and
Conventional, low-and-medium-grade products to the necessary industrial chemicals of large-scale production and increase production high-tech content, high added value it is high-end
Petroleum chemicals change；From more scattered and be laid out unreasonable operation to further maximization, intensive, integrated, base
Change, Industry Cluster and optimization layout change；Turn from using petroleum base as raw material to raw material lighting, variation and source variation
Become.
2012,1648.9 ten thousand tons of China's ethene production capacity, 1486.8 ten thousand tons of actual production, Apparent con- sumption about 16,290,000
Ton.In recent years, the energy-saving and emission-reduction and system optimization of the continuous propelling cracking furnace of ethene enterprise, that further improves the energy utilizes effect
Rate, energy resource consumption is reduced, assume responsibility for the social responsibility of energy-saving and emission-reduction.By taking Sinopec as an example, the second of 2010,2011 and 2012
Alkene combustion kinetic energy consumption (mark oil) is respectively 609.28kg/t, 582.95kg/t and 579.59kg/t.The ethene combustion kinetic energy reduced year by year
On the one hand consumption benefits from the optimization of raw material and production run, be on the other hand attributed to the fact that popularization and application, the enterprise of new technique achievement
Technological transformation technical measures and fine-grained management.In recent years, it is pre- mainly to include cracking stove air for the new technique achievement of ethane cracking furnace application
Hot device, twisted slice tube heat transfer enhancement technology, model stove technology and pyrolysis furnace quickly burn technology etc..Pyrolysis furnace air preheater skill
Art mainly preheats the combustion air of combustion bottom burner by the used heat thermal source of ethylene unit, realizes the section of fuel combustion heat supply
Energy, improve the efficiency of energy utilization of ethylene unit.
As it is known by one skilled in the art, in crack furnance radiation section furnace tube material hydrocarbon cracking reaction with high temperature,
The features such as short stop, low hydrocarbon partial pressure.At present, pyrolysis furnace operation prioritization scheme by choose primary product (ethene, propylene and
Butadiene etc.) mass yield be target, suitable thermal cracking process condition is formulated, such as boiler tube out temperature and cracking stock
Deng.CN103289725 discloses a kind of energy-conserving and optimizing control method of ethane cracking furnace, and analytical pyrolysis Raw material processing scheme is to energy
The influence of consumption, product yield, coke cleaning period, using cracking severity model, tube coking speed and plant energy consumption model, with reference to pass
Key technological parameter and control system, optimal radiant coil outlet temperature and water-oil factor are drawn, realize energy-conservation and economic benefit
Maximization target.CN100429461 discloses Ethylene Cracking Furnace At Bottom of Burner System and Method of Air Preheater, utilizes plant area
Lp venting steam, the pyrolysis furnace circulation thermal medium such as chilled water (chw) and plant area's condensate liquid after balance are entered by preheater to cold air
Row preheating, realizes the energy-saving and emission-reduction to ethylene unit.After Shao Chen describes pyrolysis furnace setting air preheater, pyrolysis furnace is reduced
Exhaust gas temperature, the thermal efficiency is improved, introduce fuel consumption, reduce fume emission.
Document《Air preheater applies petrochemical equipment technologies, Shao Chen, 2011.32 (4) in pyrolysis furnace:30-
35》In disclose because ethylene unit used heat thermal source is different, air preheating temperature is also corresponding different, is released after fuel and air burning
The thermo parameters method of thermal discharge will produce difference, and the difference of smoke-filling movement will be to the heat absorption shape of hydrocarbon cracking reaction in boiler tube
Condition, radiant section flue gas pressures field and flow field, radiant section exiting flue gas mean temperature and NOx emission etc. have an impact.
The content of the invention
It is an object of the invention in order to solve ethane cracking furnace combustion bottom burner combustion air temperature and its radiant section
The problem of smoke-filling movement, pressure field and Flow Field Distribution change, another purpose are to provide combustion air temperature rise and fuel
Pyrolysis furnace operational factor change after amount change, a kind of the excellent of ethane cracking furnace production run is provided for pyrolysis furnace production run
Change method.
The invention provides a kind of optimization method of ethane cracking furnace production run, wherein, this method comprises the following steps：
Step 1：The geometric model of ethane cracking furnace is established, the technological design based on ethane cracking furnace combustion bottom burner
Parameter, simulation calculating is carried out to cracking of ethylene furnace radiant coil exterior domain using Fluid Mechanics Computation method, obtain ethene and split
Solve the operational factor outside furnace radiant coil；
Step 2：The geometric model of cracking of ethylene furnace radiant coil is established, based on cracking of ethylene furnace radiant coil
Interior technological parameter, using hydrocarbon cracking reaction model, obtain the operational factor of ethane cracking furnace；
Step 3：By the result of calculation and the ethane cracking furnace spoke of step 2 outside the cracking of ethylene furnace radiant coil of step 1
The result of calculation coupling penetrated in section boiler tube calculates again, using the result of calculation of step 2 as condition, the result of calculation of iterative step 1, directly
Operational factor outside to radiant coil is stable, then exports result of calculation；
Step 4：When the combustion air temperature rise 1 in the process design parameter of the ethane cracking furnace combustion bottom burner
At DEG C -200 DEG C, the fuel flow rate Q in the process design parameter of ethane cracking furnace combustion bottom burner described in step 1 is adjusted to
0.9Q-1Q, then implementation steps 1；
Step 5：Condition using the result of calculation of step 4 as calculation procedure 2, the result of calculation of iterative step 2, works as step
After the completion of 2 calculating, it is ensured that fortune of the pyrolysis furnace operational factor of calculating better than the ethane cracking furnace before combustion air temperature rise
Row parameter；
Step 6：Step 4 and step 5 implementation steps 3 are subjected to coupled simulation calculating.
According to the present invention, ethane cracking furnace radiant section of the invention is divided into boiler tube and outer two parts of boiler tube, in boiler tube
For hydrocarbon raw material cracking reaction region, boiler tube discharges the heat source region of heat for fuel combustion outside.Boiler tube inner region is using cracking
Reaction Kinetics Model is calculated, and obtains material caloric receptivity, the mass yield and cracking of ethylene of low-carbon alkene product in boiler tube
The parameters such as the cycle of operation of stove, boiler tube exterior domain calculate smoke-filling movement, pressure field and cigarette using Fluid Mechanics Computation method
The parameter such as gas component and concentration.Then, the result coupling in boiler tube with boiler tube exterior domain is calculated again, obtains radiant coil pipe
The data such as wall temperature, radiant section flue gas physical parameter and radiant section exit gas temperature.When ethane cracking furnace combustion bottom burner
After combustion air temperature rise, design and operational factor based on ethane cracking furnace, optimize the influx of fuel, combustion process and
The distribution of radiant section smoke-filling movement, realize the optimization of ethane cracking furnace production run.
Therefore, the coupling meter that the present invention passes through hydrocarbon cracking reaction model in Fluid Mechanics Computation method and radiant coil
Calculate, the combustion air temperature and the most ratio of greater inequality of fuel flow rate sought in the process design parameter of ethane cracking furnace combustion bottom burner
Example, optimal preheated air temperature and radiant section flue-gas temperature field distribution.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is the schematic diagram of ethane cracking furnace provided by the present invention；
Fig. 2 is the schematic diagram of radiant coil provided by the present invention；
Fig. 3 is the schematic diagram of ethane cracking furnace combustion bottom burner provided by the present invention；
Fig. 4 is the schematic diagram of calculation process provided by the present invention.
The description of symbols of accompanying drawing 1：
1 combustion bottom burner；2 radiant coils；3 radiant sections；4 radiant wall burners；5 convection sections；6 heatings tube in section of convection chamber；7 chillings
Boiler
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
According to the invention provides a kind of optimization method of ethane cracking furnace production run, wherein, this method includes following
Step：
Step 1：The geometric model of ethane cracking furnace is established, the technological design based on ethane cracking furnace combustion bottom burner
Parameter, simulation calculating is carried out to cracking of ethylene furnace radiant coil exterior domain using Fluid Mechanics Computation method, obtain ethene and split
Solve the operational factor outside furnace radiant coil；
Step 2：The geometric model of cracking of ethylene furnace radiant coil is established, based on cracking of ethylene furnace radiant coil
Interior technological parameter, using hydrocarbon cracking reaction model, obtain the operational factor of ethane cracking furnace；
Step 3：By the result of calculation and the ethane cracking furnace spoke of step 2 outside the cracking of ethylene furnace radiant coil of step 1
The result of calculation coupling penetrated in section boiler tube calculates again, using the result of calculation of step 2 as condition, the result of calculation of iterative step 1, directly
Operational factor outside to radiant coil is stable, then exports result of calculation；
Step 4：When the combustion air temperature rise 1 in the process design parameter of the ethane cracking furnace combustion bottom burner
At DEG C -200 DEG C, the fuel flow rate Q in the process design parameter of ethane cracking furnace combustion bottom burner described in step 1 is adjusted to
0.9Q-1Q, then implementation steps 1；
Step 5：Condition using the result of calculation of step 4 as calculation procedure 2, the result of calculation of iterative step 2, works as step
After the completion of 2 calculating, it is ensured that fortune of the pyrolysis furnace operational factor of calculating better than the ethane cracking furnace before combustion air temperature rise
Row parameter；
Step 6：Step 4 and step 5 implementation steps 3 are subjected to coupled simulation calculating.
According to the present invention, specifically, present disclosure includes：Cracking of ethylene furnace radiant coil external combustion in step 1
Produced after material burning and fuel combustion flue gas situation (wherein, including temperature field, pressure field and the flue gas composition of production flue gas and
Concentration distribution) calculating；In step 2 based on the technological parameter in cracking of ethylene furnace radiant coil, it is anti-using hydrocarbon cracking
Model is answered, obtains the operational factor of ethane cracking furnace；In cracking of ethylene furnace radiant coil in step 3 and ethane cracking furnace spoke
The coupled simulation penetrated outside section boiler tube calculates, until the operational factor outside radiant coil is stable；Step 4 is to work as the cracking of ethylene
When combustion air temperature in the process design parameter of furnace bottom burner raises 1 DEG C -200 DEG C, then need second described in step 1
Fuel flow rate Q in the process design parameter of alkene pyrolysis furnace combustion bottom burner is adjusted to 0.9Q-1Q, then implementation steps 1；Step 5
Pressed using the condition of the result of calculation of step 4 as calculation procedure 2, the result of calculation of iterative step 2, when the calculating of step 2 is completed
Afterwards, it is ensured that operational factor of the pyrolysis furnace operational factor of calculating better than the ethane cracking furnace before combustion air temperature rise；And
Step 6：Step 4 and step 5 implementation steps 3 are subjected to coupled simulation calculating.
According to the present invention, Fluid Mechanics Computation method outside the cracking of ethylene furnace radiant coil include combustion model,
Turbulence model, component delivery model and radiation patterns.
According to the present invention, the process design parameter of the ethane cracking furnace combustion bottom burner, i.e. ethane cracking furnace radiant section
The process design parameter that pipe outer fuel burns and flue gas situation calculates includes fuel flow rate, fuel pressure and fuel temperature, combustion-supporting
Excess air coefficient in the air door size of air, combustion air temperature and combustion air.
According to the present invention, the burning of cracking of ethylene furnace radiant coil outer fuel and the calculating of flue gas situation are split based on ethene
It is Q to solve furnace bottom burner fuel flow, and combustion air temperature is normal temperature, establishes the geometry of ethane cracking furnace, utilizes meter
Fluid operator mechanics method is calculated the operational factor outside cracking of ethylene furnace radiant coil, wherein, the ethane cracking furnace
Operational factor outside radiant coil includes producing after fuel combustion the flow field of flue gas, temperature field, pressure field, flue gas composition and dense
Degree distribution and the flame temperature field and flame height of fuel combustion.
According to the present invention, it is anti-that the hydrocarbon cracking reaction model in the cracking of ethylene furnace radiant coil includes hydro carbons chemistry
Answer model, heat transfer model, flow model and pressure model.
According to the present invention, the technological parameter in the cracking of ethylene furnace radiant coil includes raw material type, raw material feeds intake
Amount, initial operating stage and the boiler tube out temperature and pressure in latter stage, tube coking speed.
According to the present invention, the pyrolysis furnace operational factor that step 2 calculates include material caloric receptivity in radiant coil,
The mass yield of low-carbon alkene product and the cycle of operation of ethane cracking furnace.
According to the present invention, radiant section pipe is interior under step 6 ethane cracking furnace combustion bottom burner air preheat situation and manages outer coupling
Stable parameter outside total cracking of ethylene furnace radiant coil calculated includes radiant section flue gas flow field, temperature field, pressure
The field of force, boiler tube tube wall temperature, fuel combustion flames height and temperature；And radiant section flue gas flow field is 0.01m/s-50m/s, temperature
Field is -50 DEG C -1750 DEG C, pressure field is -2000Pa-20000Pa, boiler tube tube wall temperature is 900 DEG C -1150 DEG C, fuel combustion
Flame height is 0.1m-6m and flame front flue-gas temperature is 1000 DEG C -1450 DEG C, is shown outside cracking of ethylene furnace radiant coil
Operational factor is stable.
The calculating that hydrocarbon cracking reacts in cracking of ethylene furnace radiant coil is based on ethane cracking furnace design inventory etc.
Parameter, the geometry of radiant coil is established, using hydrocarbon cracking reaction model, calculate material in radiant coil and absorb heat
The cycle of operation of amount, the mass yield of low-carbon alkene product and ethane cracking furnace.
Coupling in cracking of ethylene furnace radiant coil and outside pipe, which calculates, is reacted based on hydrocarbon cracking in radiant section pipe
Result of calculation, the burning of radiant section pipe outer fuel and flue gas situation are calculated, until the parameter stability of radiant section operation.
It is to be based on that coupling under ethane cracking furnace combustion bottom burner air preheat situation in radiant section pipe and outside pipe calculates again
Design inventory and fuel quantity Q.After preheating temperature of the air from normal temperature adjustment used heat, fuel quantity is accordingly adjusted, then carry out coupling
It is total to calculate, before ensureing the radiant section technological parameter after adjustment better than combustion air temperature rise, instruct the reality of ethane cracking furnace
Operation.
According to the present invention, in step 4, the combustion-supporting sky in the process design parameter of the ethane cracking furnace combustion bottom burner
When the temperature of gas raises 50 DEG C -120 DEG C, the fuel flow rate after calculating is adjusted to 0.95Q-0.99Q；
Preferably, when the temperature of the combustion air raises 80 DEG C -100 DEG C, by the cracking of ethylene furnace bottom after calculating
Fuel flow rate in the process design parameter of burner is adjusted to 0.96Q-0.98Q.
The applicable ethane cracking furnace of the optimization method of production run provided by the invention mainly includes：Radiant section, convection section
And quenching boiler, refer to Fig. 1.
Radiant section：Multigroup radiating furnace tube in burner hearth center is arranged in, boiler tube can take various forms, and the journey of 1-1 configurations two is not
Isometrical no branch, refers to Fig. 2, either 2-1 types and the journey branch reducing radiating furnace tube of 4-1 types two or other configuration boiler tubes；Radiation
Section two bottom sides arrangement combustion bottom burner, refer to Fig. 3, top both sides arrangement radiant wall burner, additional heat and change heat point
Cloth.
Convection section：Horizontally disposed multigroup heating tube in section of convection chamber, it is easy to the high efficient heat exchanging of cracking stock, is passed more using various strengthen
Thermal technology improves its heat transfer efficiency.
In order to solve the variation issue of ethane cracking furnace combustion bottom burner combustion air temperature rise after-burning doses.By right
Radiant section pipe outer fuel burns and flue gas situation calculates, and acquisition includes the data such as flow of flue gas, pressure field and temperature field.Utilize
Hydrocarbon feed cracking reaction model calculates pyrolysis furnace operational factor in pipe, and as condition, couples the fuel outside radiant coil
Burning and flowing etc. calculate again.After combustion air temperature raises, suitable fuel quantity is selected to be helped after being raised with combustion bottom burner
Combustion air themperature is adapted so that before pyrolysis furnace operational factor is better than combustion air temperature rise, allows the production of ethane cracking furnace
Operation is optimized.Process of the present invention refers to Fig. 4.
After the temperature rise of ethane cracking furnace combustion bottom burner combustion air, the combustion air after temperature rise will be brought into
More heats enter radiant section.Combustion air temperature rise after, volumetric expansion, into radiant section after combustion air mixed with fuel
The combustion position of conjunction will will produce difference with the uninflated combustion position of combustion air temperature, and this difference will influence radiant section flue gas
Temperature field, flow field and pressure field distribution, and then the change of the parameter such as temperature, pressure and speed of material in pipe is produced, operation is not
Cycle of operation of the mass yield of product, boiler tube service life and pyrolysis furnace etc. when will influence low-carbon alkene the purpose of.
In the actual moving process of ethane cracking furnace, generally combustion bottom burner combustion air temperature is controlled by adjusting fuel flow rate
Change, fuel quantity how is correctly adjusted to ensure that the stable supplying of heat, fuel combustion be stable and temperature field suitable distribution etc. is
The major issue solved is needed after the rise of ethane cracking furnace combustion bottom burner combustion air temperature.
Embodiment
Embodiment 1
As shown in figure 1, annual output 100000 tons of pyrolysis furnaces of ethene, the pyrolysis furnace radiant section are made up of 48 groups of 2-1 type boiler tubes,
Divide 6 big groups, be arranged in burner hearth center.36 combustion bottom burners, fuel and combustion air are non-premixed combustion, the temperature of combustion air
Spend for 50 DEG C.48 radiant wall burners, fuel and combustion air are premixed combustion.
Hydrocarbon raw material is by taking certain hydrogenation tail oil as an example, inventory 41200kg/h, and dilution steam generation is with hydrocarbon feed weight ratio
0.75, radiant coil out temperature is respectively 555 DEG C and 812 DEG C, inlet and outlet pressure (gauge pressure) be respectively 0.19Mpa and
0.11Mpa.Dilution steam generation and hydrocarbon feed weight ratio, radiant coil out temperature and inlet and outlet pressure are constant, fuel with
(gas volume fractions 19 based on methane and hydrogen:1), calculate respectively combustion bottom burner combustion air temperature be increased to 50 DEG C and
The change of radiant section technological parameter under the different schemes of fuel change, refers to table 1, the operation outside cracking of ethylene furnace radiant coil
Parameter includes the flue gas pressures average -100Pa of radiant section exit face, and mean flow rate 6m/s, mean temperature is 1050 DEG C.
Table 1
| Combustion air temperature, DEG C | 25 | 50 | 50 | 50 |
| Combustion bottom burner fuel quantity, kg/s | 1.5088 | 1.4862 | 1.4937 | 1.5013 |
| Fuel ratio, % | 100 | 98.5 | 99.0 | 99.5 |
| Whether air dampers adjust | It is no | It is | It is | It is |
| Radiant section thermic load, MW | 37.49211 | 37.49369 | 37.54156 | 37.49514 |
| Yield of ethene, wt% | 31.19 | 31.19 | 31.24 | 31.19 |
| Propene yield, wt% | 18.95 | 18.95 | 18.95 | 18.95 |
| The pyrolysis furnace cycle of operation, day | 56.7 | 56.8 | 59.6 | 56.9 |
Embodiment 2
As shown in figure 1, annual output 100000 tons of pyrolysis furnaces of ethene, the pyrolysis furnace radiant section are made up of 48 groups of 2-1 type boiler tubes,
Divide 6 big groups, be arranged in burner hearth center.36 combustion bottom burners, fuel and combustion air are non-premixed combustion, the temperature of combustion air
Spend for 120 DEG C.48 radiant wall burners, fuel and combustion air are premixed combustion.
Hydrocarbon raw material is by taking certain hydrogenation tail oil as an example, inventory 41200kg/h, and dilution steam generation is with hydrocarbon feed weight ratio
0.75, radiant coil out temperature is respectively 555 DEG C and 812 DEG C, inlet and outlet pressure (gauge pressure) be respectively 0.19Mpa and
0.11Mpa.Dilution steam generation and hydrocarbon feed weight ratio, radiant coil out temperature and inlet and outlet pressure are constant, fuel with
(gas volume fractions 19 based on methane and hydrogen:1), calculate respectively and be increased to 120 DEG C in combustion bottom burner combustion air temperature
With the change of radiant section technological parameter under the different schemes of fuel change, table 2 is referred to, the fortune outside cracking of ethylene furnace radiant coil
Row parameter includes the flue gas pressures average -100Pa of radiant section exit face, and mean flow rate 6m/s, mean temperature is 1050 DEG C.
Table 2
| Combustion air temperature, DEG C | 25 | 120 | 120 | 120 |
| Combustion bottom burner fuel quantity, kg/s | 1.5088 | 1.4484 | 1.4560 | 1.4635 |
| Fuel ratio, % | 100 | 96.0 | 96.5 | 97.0 |
| Whether air dampers adjust | It is no | It is | It is | It is |
| Radiant section thermic load, MW | 37.49211 | 37.48956 | 37.49395 | 37.49247 |
| Yield of ethene, wt% | 31.19 | 31.19 | 31.19 | 31.19 |
| Propene yield, wt% | 18.95 | 18.95 | 18.95 | 18.95 |
| The pyrolysis furnace cycle of operation, day | 56.7 | 56.6 | 58.8 | 56.7 |
It can be seen from the result Tables 1 and 2 of Examples 1 and 2, according to the production run of ethane cracking furnace provided by the invention
Optimization method, using new simulation method, it is anti-to couple hydrocarbon cracking in radiant coil outer fuel combustion position and pipe
Situation is answered, the actual motion operation of different air preheating temperatures is disclosure satisfy that, therefore, according to ethane cracking furnace provided by the invention
Production run optimization method, the practical operation of ethane cracking furnace can be instructed, so realize ethylene unit production fortune
Row optimization.
The preferred embodiment of the present invention described in detail above, still, the present invention are not limited in above-mentioned embodiment
Detail, in the range of the technology design of the present invention, a variety of simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of optimization method of ethane cracking furnace production run, it is characterised in that this method comprises the following steps：
Step 1：The geometric model of ethane cracking furnace is established, the technological design ginseng based on ethane cracking furnace combustion bottom burner
Number, simulation calculating is carried out to cracking of ethylene furnace radiant coil exterior domain using Fluid Mechanics Computation method, obtains cracking of ethylene
Operational factor outside furnace radiant coil；
Step 2：The geometric model of cracking of ethylene furnace radiant coil is established, based in cracking of ethylene furnace radiant coil
Technological parameter, using hydrocarbon cracking reaction model, obtain the operational factor in cracking of ethylene furnace radiant coil；
Step 3：By the result of calculation and the ethane cracking furnace radiant section of step 2 outside the cracking of ethylene furnace radiant coil of step 1
Result of calculation coupling in boiler tube calculates again, using the result of calculation of step 2 as condition, the result of calculation of iterative step 1, until spoke
The operational factor penetrated outside section boiler tube is stable, then exports result of calculation；
Step 4：When the combustion air temperature in the process design parameter of the ethane cracking furnace combustion bottom burner raises 1 DEG C -200
DEG C when, the fuel flow rate Q in the process design parameter of ethane cracking furnace combustion bottom burner described in step 1 is adjusted to 0.9Q-1Q,
Implementation steps 1 again；
Step 5：Condition using the result of calculation of step 4 as calculation procedure 2, the result of calculation of iterative step 2, when step 2
After the completion of calculating, it is ensured that operation ginseng of the pyrolysis furnace operational factor of calculating better than the ethane cracking furnace before combustion air temperature rise
Number；
Step 6：Step 4 and step 5 implementation steps 3 are subjected to coupled simulation calculating.
2. optimization method according to claim 1, wherein, in step 1, outside the cracking of ethylene furnace radiant coil
Fluid Mechanics Computation method includes combustion model, turbulence model, component delivery model and radiation patterns.
3. optimization method according to claim 1, wherein, in step 1, the work of the ethane cracking furnace combustion bottom burner
Skill design parameter includes fuel flow rate, fuel pressure, fuel temperature, the air door size of combustion air, combustion air temperature and helped
Fire excess air coefficient in air.
4. optimization method according to claim 1, wherein, in step 1, outside the cracking of ethylene furnace radiant coil
Operational factor includes flow field, temperature field, pressure field, flue gas composition and the concentration distribution and fuel of production flue gas after fuel combustion
Burned flame temperature field and flame height.
5. optimization method according to claim 1, wherein, in step 2, in the cracking of ethylene furnace radiant coil
Hydrocarbon cracking reaction model includes hydro carbons Chemical Reaction Model, heat transfer model, flow model and pressure model.
6. optimization method according to claim 1, wherein, in step 2, in the cracking of ethylene furnace radiant coil
Technological parameter includes raw material type, raw material inventory, initial operating stage and boiler tube out temperature and pressure, the tube coking in latter stage
Speed.
7. optimization method according to claim 1, wherein, in step 2, in the cracking of ethylene furnace radiant coil
Operational factor includes the operation week of material caloric receptivity, the mass yield of low-carbon alkene product and ethane cracking furnace in radiant coil
Phase.
8. optimization method according to claim 1, wherein, in step 4, when the ethane cracking furnace combustion bottom burner
When combustion air temperature in process design parameter raises 50 DEG C -120 DEG C, by ethane cracking furnace combustion bottom burner described in step 1
Process design parameter in fuel flow rate Q be adjusted to 0.95Q-0.99Q, then implementation steps 1.
9. optimization method according to claim 7, when in the process design parameter of the ethane cracking furnace combustion bottom burner
Combustion air temperature raise 80 DEG C -100 DEG C when, by the process design parameter of ethane cracking furnace combustion bottom burner described in step 1
In fuel flow rate be adjusted to 0.96Q-0.98Q, then implementation steps 1.
10. optimization method according to claim 1, wherein, it is stable outside the cracking of ethylene furnace radiant coil
Parameter includes radiant section flue gas flow field, temperature field, pressure field, boiler tube tube wall temperature, fuel combustion flames height and temperature；And spoke
Penetrate that a section flue gas flow field is 0.01m/s-50m/s, temperature field is -50 DEG C -1750 DEG C, pressure field is -2000Pa-20000Pa, boiler tube
Tube wall temperature is 900 DEG C -1150 DEG C, fuel combustion flames are highly 0.1m-6m and flame front flue-gas temperature is 1000 DEG C -1450
℃。
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| CN201410448859.9A CN105467939B (en) | 2014-09-04 | 2014-09-04 | A kind of optimization method of ethane cracking furnace production run |
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