CN110270240A - Dilution steam generation mixer - Google Patents
Dilution steam generation mixer Download PDFInfo
- Publication number
- CN110270240A CN110270240A CN201910490513.8A CN201910490513A CN110270240A CN 110270240 A CN110270240 A CN 110270240A CN 201910490513 A CN201910490513 A CN 201910490513A CN 110270240 A CN110270240 A CN 110270240A
- Authority
- CN
- China
- Prior art keywords
- cylinder
- section
- steam generation
- dilution
- dilution steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000012895 dilution Substances 0.000 title claims abstract description 35
- 238000010790 dilution Methods 0.000 title claims abstract description 35
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 238000004227 thermal cracking Methods 0.000 abstract description 5
- 239000012808 vapor phase Substances 0.000 abstract description 5
- 238000005336 cracking Methods 0.000 description 25
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- 239000003610 charcoal Substances 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 241000521257 Hydrops Species 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- -1 ethylene Chemical class 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000693 micelle Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000002277 temperature effect Effects 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/10—Mixing gases with gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
Abstract
The present invention relates to a kind of dilution steam generation mixers, including inner barrel and outer barrel；The inner cylinder forms the direct tube section of integral structure in the axial direction and expands cylinder section, and the direct tube section free end extends out to outside outer cylinder and forms feed(raw material)inlet；It is fixedly linked between the inner cylinder and outer cylinder by direct tube section；Expansion cylinder section free end cross sectional radius gradually expands, and makes to form slight gap between free end end port and outer tube inner wall；The circumferential wall for expanding cylinder section is equipped with the steam passage holes that upper and lower two groups of angles mutually stagger；The inner cylinder expands the corresponding outer cylinder barrel of cylinder section and is equipped with steam inlet.The configuration of the present invention is simple, it is easy to operate, steam dilution can be effectively controlled, and dilution steam generation and vapor-phase thermal cracking raw material can be made to be sufficiently mixed uniformly within limited time and space.
Description
Technical field
The invention belongs to mixer apparatus technical fields, and in particular to dilute during producing cracking gas for hydrocarbon cracking
The mixer that steam and vapor-phase thermal cracking raw material mix.
Background technique
Hydrocarbon cracking is produced the process of cracking gas by ethane cracking furnace.In chemical balance, hydrocarbon cracking it is primary anti-
It should be the increased reaction of volume, reduce reaction pressure and be conducive to hydro carbons to the direction progress for generating the light alkenes such as ethylene, improve
Purpose product yield；Secondary response is the reaction that gas volume reduces, and the progress of secondary response can be inhibited by reducing pressure, is reduced
Coking.Kinetically, although pressure cannot change rate constant, it can be influenced instead by reactant concentration variation
Speed is answered, since the order of reaction of primary first-order equation is smaller than secondary response, primary first-order equation can be increased for secondary counter by reducing pressure
The relative velocity answered.
By above-mentioned two aspect as it can be seen that no matter from thermodynamics or kinetically, reducing pressure all has primary first-order equation
Benefit, and can inhibit the progress of secondary response.
Since hydrocarbon cracking reaction carries out at high temperature, by using the method directly depressurized, first is that safety is deposited
Pyrolysis furnace is not easy to seal under problem, high temperature, and a denier air is leak into high temperature furnace pipe, it may occur that explosion；Second is that being split to subsequent
Venting one's spleen, it is unfavorable to compress, and energy charge can be made to increase, and energy consumption increases, therefore the industrial method for using indirect decompression, that is, uses and add
Enter the hydrocarbon partial pressure in the method reduction boiler tube of diluent, industrially generallys use vapor as diluent.
Steam dilution is exactly the ratio of dilution steam generation Yu cracking stock mass flow.Thinner ratio increases, and can make hydrocarbon point
Pressure reduces, and improves boiler tube logistics speed, reduces film temperature drop, also opposite to shorten the residence time.But thinner ratio is excessive,
Certain adverse effects can be brought, the production capacity of equipment is such as reduced, increase steam and fuel consumption, so must control appropriate
Thinner ratio.Thinner ratio is different with the difference of cracking stock, and principle is the dilution few as far as possible under conditions of energy slagging prevention
Steam just suitably increases thinner ratio only when raw material is easy coking.
The advantages of vapor is as diluent, is mainly reflected in the following aspects:
1. stable cracking temperature.Vapor thermal capacity is larger, and when operation heat supply is unstable, it can play equilibrium temperature
Effect, can also protect boiler tube to prevent from overheating.
2. protecting boiler tube.In the presence of having vapor, since high-temperature steam is oxidizing, it can inhibit in cracking stock
Corrosion of the contained sulphur to boiler tube, so, even if sulfur content is up to 2%(mass fraction), it is also not enough to constitute the corruption to boiler tube
Erosion threatens.
3. removing coking.The iron and nickel of boiler tube can be catalyzed the life charcoal reaction of hydrocarbon gas, and vapor has oxidation to iron and nickel
Effect can inhibit their catalytic action to raw charcoal reaction, and vapor has certain removing to act on generated charcoal.
So the important research topic in dilution steam generation position one and direction how is added in limited pyrolysis furnace space.
Summary of the invention
The purpose of the present invention is to provide a kind of dilution steam generation mixers, and structure is simple, easy to operate, and can be limited
Time and space in make dilution steam generation and vapor-phase thermal cracking raw material is sufficiently mixed uniformly.
To achieve the goals above, the technical solution of the present invention is as follows:
A kind of dilution steam generation mixer, including inner barrel and outer barrel；The inner cylinder forms the direct tube section of integral structure in the axial direction
With expansion cylinder section, the direct tube section free end extends out to outside outer cylinder and forms feed(raw material)inlet；Lead between the inner cylinder and outer cylinder
Direct tube section is crossed to be fixedly linked；
Expansion cylinder section free end cross sectional radius gradually expands, and makes to be formed between free end end port and outer tube inner wall thin
Small―gap suture；The circumferential wall for expanding cylinder section is equipped with the steam passage holes that upper and lower two groups of angles mutually stagger；
The inner cylinder expands the corresponding outer cylinder barrel of cylinder section and is equipped with steam inlet.
As a further improvement of the present invention: the outer cylinder main body is straight tube structure, and end is undergauge structure.Such straight tube
It is mixed in outer cylinder lower space that the cooperation of structure and end undergauge structure can further strengthen cracking gas and dilution steam generation air-flow
Disturbance is closed, its being sufficiently mixed in outer cylinder lower space is promoted.
As a further improvement of the present invention: the expansion cylinder section is in frustum cone structure.The axis for expanding cylinder section frustum cone structure is cut
Face base angle is 75-85 degree.The design for expanding barrel structure in this way can be such that gas flow rate reduces, and be more advantageous to the sucking drainage of gas；Together
When may insure that flow surface resistance is minimum, fluid-pressure drop loss reduction.
As a further improvement of the present invention: the central axis of the steam passage holes is tilted to outer cylinder outlet end, thus into
One step accelerates mixing rate.
As a further improvement of the present invention: inner cylinder is spurted by steam passage holes due to dilution steam generation and expands cylinder section region,
To which jet stream is penetrated into cracking stock air-flow, when large scale macroscopic view uniform concentration distribution to be reached, this needs to dilute and steam
The momentum of vapour is greater than cracking stock air-flow momentum.High-speed jet causes shear layer, and the unstability of shear layer will drive and around flow
The movement of body, to, to improve the area of molecule diffusion, reach stream by cracking stock fluid breakup at many small micelles
The uniform mixing of body.Therefore, dilution steam generation will form jet stream, and steam passage holes aperture is more demanding.For a certain amount of aperture face
Product, aperture is small, and flow velocity is high, although the turbulent extent of dilution steam generation is big, the projected area after dilution steam generation injection is small, can not be complete
The full flowing for driving boundary layer；Aperture is big, and flow velocity is small, can not form high velocity jet body, drives cracking gas air-flow, therefore this hair
The bright steam passage holes pore size control is in 10-20mm.
The operation principle of the present invention is that: after cracking stock is produced by convection section in cracking furnace, into the inner cylinder of dilution steam generation mixer,
Cracking gas is flowed from above to below along inner cylinder direct tube section；Dilution steam generation enters the top that outer cylinder and inner cylinder are formed by steam inlet
It is buffered in cavity, then is entered in the lower cavity that outer cylinder and inner cylinder are formed by steam passage holes；Dilution steam generation and cracking gas
Reach thick mixing in the expansion cylinder section of inner cylinder, then further mixes cracking gas with dilution steam generation in outer cylinder lower space.
The configuration of the present invention is simple, it is easy to operate, steam dilution can be effectively controlled, and can be within limited time and space
It is sufficiently mixed dilution steam generation and vapor-phase thermal cracking raw material uniformly.
Detailed description of the invention
Fig. 1 is main structure figure of the invention；
Fig. 2 is the structural schematic diagram of inner cylinder in the present invention；
Fig. 3 is A-A section view amplification assumption diagram in Fig. 2.
Specific embodiment
In order to deepen the understanding of the present invention, the present invention is done below in conjunction with drawings and examples and is further retouched in detail
It states.
It is mixed to be related to a kind of dilution steam generation mixed for dilution steam generation with vapor-phase thermal cracking raw material for the present embodiment as shown in Figure 1:
Clutch comprising inner barrel and outer barrel.
1 main body of outer cylinder is straight tube structure as shown in Figure 1:, and a diameter of 270mm, upper end port is for the company with inner cylinder 2
It connects, lower end port is in undergauge structure, and the minimum diameter formed after undergauge is greater than or equal to the radius of outer cylinder straight drum part, undergauge knot
Structure makes downdraught generate disturbance again, and then strengthens cracking gas further with dilution steam generation and mix.Corresponding inner cylinder expands cylinder
22 positions of section, 1 barrel of outer cylinder are equipped with steam inlet 11.
As shown in Figure 2: inner cylinder 2 forms the direct tube section 21 of integral structure from top to bottom in the axial direction and expands cylinder section 22,
11 diameter of direct tube section is 150mm, and 11 free end of direct tube section extends out to outside outer cylinder and forms feed(raw material)inlet 211；Inner cylinder straight tube
21 middle sections of section are fixedly linked by flange or welding with 1 upper end port of outer cylinder.
As shown in Figure 2: the 22 free end radius of expansion cylinder section of inner cylinder gradually expands, and forms frustum cone structure, is more advantageous to it
The sucking of gas drains, but expands cylinder section expanded- angle too greatly, and fluid resistance will increase, and pressure drop will increase.It is formed by circle
It is 80 degree in shaft section base angle the present embodiment of platform structure, so that the expansion cylinder angle for expanding cylinder section is controlled, so as to ensure fluid
Drag losses are minimum, it is ensured that mixed effect.
Before being mixed as shown in Figure 1: due to cracking stock with cracking gas, 350 DEG C of temperature or so, temperature difference can cause inner cylinder axis
To thermal expansion, so inner cylinder, which expands between 22 free end port of cylinder section and 1 inner wall of outer cylinder, forms slight gap；In addition, dilution is steamed
Vapour can pass through minimum gap and purge to the gas of surrounding lower part, avoids causing hydrops, generates dead zone.
As shown in Figure 2 and Figure 3: it is logical that the circumferential wall that inner cylinder expands cylinder section 22 is equipped with the steam that upper and lower two groups of angles mutually stagger
Hole 221 so that dilution steam generation be made to disperse, and relatively evenly enters inner cylinder and expands cylinder section region；In order to make dilution steam generation form height
Stream is emanated stream, and 221 pore size control of steam passage holes is for 10-20mm, and 221 aperture of steam passage holes is 15mm in the present embodiment.In order to
Promote high-speed flow that cracking stock is driven to flow downward, accelerate mixing velocity, the central axis of steam passage holes 221 is exported to outer cylinder
End inclination.
The above is only used to illustrate the technical scheme of the present invention and not limits, and those of ordinary skill in the art are to this
The other modifications or equivalent replacement that the technical solution of invention is made, without departing from the spirit and scope of the technical program,
It is intended to be within the scope of the claims of the invention.
Claims (6)
1. a kind of dilution steam generation mixer, it is characterised in that: including inner barrel and outer barrel；
The inner cylinder forms the direct tube section of integral structure in the axial direction and expands cylinder section, and the direct tube section free end extends out to
Outer cylinder is outer and forms feed(raw material)inlet；It is fixedly linked between the inner cylinder and outer cylinder by direct tube section；
Expansion cylinder section free end cross sectional radius gradually expands, and makes to be formed between free end end port and outer tube inner wall thin
Small―gap suture；The circumferential wall for expanding cylinder section is equipped with the steam passage holes that upper and lower two groups of angles mutually stagger；
The inner cylinder expands the corresponding outer cylinder barrel of cylinder section and is equipped with steam inlet.
2. dilution steam generation mixer according to claim 1, it is characterised in that: the outer cylinder main body is straight tube structure, end
End is undergauge structure.
3. dilution steam generation mixer according to claim 1, it is characterised in that: the expansion cylinder section is in frustum cone structure.
4. dilution steam generation mixer according to claim 3, it is characterised in that: the shaft section for expanding cylinder section frustum cone structure
Base angle is 75-85 degree.
5. dilution steam generation mixer according to claim 1, it is characterised in that: the central axis of the steam passage holes is outside
The inclination of cylinder outlet end.
6. dilution steam generation mixer according to claim 1, it is characterised in that: the steam passage holes aperture is 10-20mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910490513.8A CN110270240A (en) | 2019-06-06 | 2019-06-06 | Dilution steam generation mixer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910490513.8A CN110270240A (en) | 2019-06-06 | 2019-06-06 | Dilution steam generation mixer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110270240A true CN110270240A (en) | 2019-09-24 |
Family
ID=67961942
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910490513.8A Pending CN110270240A (en) | 2019-06-06 | 2019-06-06 | Dilution steam generation mixer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110270240A (en) |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD244499A5 (en) * | 1985-04-01 | 1987-04-08 | Waagner-Biro Ag,At | MIXING DEVICE FOR DIFFERENTLY TEMPERED GAS STROEMES |
| CN1112457A (en) * | 1994-03-15 | 1995-11-29 | 英国氧气集团有限公司 | Gas dissolving |
| US6034288A (en) * | 1993-04-22 | 2000-03-07 | Imperial Chemical Industries Plc | Process for vaporization of halocarbons |
| JP2001321649A (en) * | 2000-05-18 | 2001-11-20 | Toshiba Corp | Fluid mixing device |
| WO2002070116A1 (en) * | 2001-03-02 | 2002-09-12 | Parsons Advanced Technologies Inc. | Assembly and method for mixing gases |
| JP2012200662A (en) * | 2011-03-25 | 2012-10-22 | Toshiba Corp | Fluid mixing apparatus and steam turbine plant |
| RU142474U1 (en) * | 2014-03-25 | 2014-06-27 | Владимир Сергеевич Мельников | PLANT FOR PROCESSING WORKING SURFACES WITH A DISINFECTANT SOLUTION USING WATER VAPOR |
| US20150092513A1 (en) * | 2012-07-05 | 2015-04-02 | Fmc Kongsberg Subsea As | Multiphase flow mixing apparatus and method of mixing |
| JP2015073971A (en) * | 2013-10-11 | 2015-04-20 | 川崎重工業株式会社 | Gas mixer |
| CN206535441U (en) * | 2016-12-30 | 2017-10-03 | 新阳科技集团有限公司 | Ethylbenzene stream and water vapour static mixing device |
| CN107530721A (en) * | 2015-04-16 | 2018-01-02 | 纳米蒸汽有限公司 | Equipment for nano-particle generation |
| TW201809549A (en) * | 2016-07-18 | 2018-03-16 | 愛德華有限公司 | Inlet assembly and method |
| CN210434326U (en) * | 2019-06-06 | 2020-05-01 | 常州瑞凯化工装备有限公司 | Dilution steam mixer |
-
2019
- 2019-06-06 CN CN201910490513.8A patent/CN110270240A/en active Pending
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD244499A5 (en) * | 1985-04-01 | 1987-04-08 | Waagner-Biro Ag,At | MIXING DEVICE FOR DIFFERENTLY TEMPERED GAS STROEMES |
| US6034288A (en) * | 1993-04-22 | 2000-03-07 | Imperial Chemical Industries Plc | Process for vaporization of halocarbons |
| CN1112457A (en) * | 1994-03-15 | 1995-11-29 | 英国氧气集团有限公司 | Gas dissolving |
| JP2001321649A (en) * | 2000-05-18 | 2001-11-20 | Toshiba Corp | Fluid mixing device |
| WO2002070116A1 (en) * | 2001-03-02 | 2002-09-12 | Parsons Advanced Technologies Inc. | Assembly and method for mixing gases |
| JP2012200662A (en) * | 2011-03-25 | 2012-10-22 | Toshiba Corp | Fluid mixing apparatus and steam turbine plant |
| US20150092513A1 (en) * | 2012-07-05 | 2015-04-02 | Fmc Kongsberg Subsea As | Multiphase flow mixing apparatus and method of mixing |
| JP2015073971A (en) * | 2013-10-11 | 2015-04-20 | 川崎重工業株式会社 | Gas mixer |
| RU142474U1 (en) * | 2014-03-25 | 2014-06-27 | Владимир Сергеевич Мельников | PLANT FOR PROCESSING WORKING SURFACES WITH A DISINFECTANT SOLUTION USING WATER VAPOR |
| CN107530721A (en) * | 2015-04-16 | 2018-01-02 | 纳米蒸汽有限公司 | Equipment for nano-particle generation |
| TW201809549A (en) * | 2016-07-18 | 2018-03-16 | 愛德華有限公司 | Inlet assembly and method |
| CN206535441U (en) * | 2016-12-30 | 2017-10-03 | 新阳科技集团有限公司 | Ethylbenzene stream and water vapour static mixing device |
| CN210434326U (en) * | 2019-06-06 | 2020-05-01 | 常州瑞凯化工装备有限公司 | Dilution steam mixer |
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