CN1468651A - Quick gas jet mixer with high homogeneity - Google Patents
Quick gas jet mixer with high homogeneity Download PDFInfo
- Publication number
- CN1468651A CN1468651A CNA021360758A CN02136075A CN1468651A CN 1468651 A CN1468651 A CN 1468651A CN A021360758 A CNA021360758 A CN A021360758A CN 02136075 A CN02136075 A CN 02136075A CN 1468651 A CN1468651 A CN 1468651A
- Authority
- CN
- China
- Prior art keywords
- gas
- taper pipe
- aperture
- distribution grid
- distribution
- 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.)
- Granted
Links
Images
Abstract
The quick gas jet mixer consists of one conic tube with jet hole on the side wall and one straight tube. The conic tube is installed inside the straight tube and the conic tube separates the straight tube into one distributing cavity and one mixing cavity. On the top of the conic tube, there is one distributing board communicated with the first gas inlet; and the distributing cavity is communicated with the second gas inlet. The device of the present invention has simple structure and may be used to complete the mixing of two gas flows in high homogeneity instantaneously.
Description
Technical field
The invention belongs to the quick mixed uniformly device that relates in the field of chemical engineering between two strands of air-flows, be particularly useful for the degree that mixes between the reaction gas flow has the chemical reaction process that has a strong impact on to reactivity worth mixing arrangement.
Technical background
In chemical process, often require to provide a kind of quick mixed uniformly technology of gas as everyone knows.Because speed and uniformity coefficient that gas mixes will directly influence the carrying out of subsequent process.For example, in Ethyl Benzene Dehydrogenation Plant, the mixability of ethylbenzene steam and water vapour directly has influence on the Temperature Distribution of reaction bed, and bad Temperature Distribution will cause the deterioration of reaction.Because ethylbenzene steam has the volume ratio height with mixing of water vapour, the medium temperature difference is big, and allowable pressure drop is little and mix and all once to require high characteristic, not only requires mixer structure simple, and require in less than 1 second incorporation time, to reach the mixture homogeneity on the micelle yardstick.The characteristics that this class is mixed are the rapid mixing that require realization response material in limited space and limited time, these characteristics be present in equally mix between the multistage reactor region and rapid pipeline mixed process in.
A kind of " gas mixer " disclosed in CN 2065096U, its operation principle is negative pressure based on the chamber of main air inlet pipe and the formation of secondary air inlet pipe, can make the secondary air inlet suction automatically of little tolerance, main air inlet drives secondary air inlet with big flow velocity and enters mixing chamber, reach the purpose of mixing, but because the restriction of negative pressure draft is merely able to be applied to the mixing of the secondary air inlet of the stingy amount of suction.A kind of " gas-gas-gas mixing apparatus " disclosed in CN 1049110A, the bump that is beneficial to jet and porous plate produces strong main diffusion and DIFFUSION IN TURBULENCE, thereby realize the rapid mixing of gas-gas storeroom, but adopt the single tube jet, be difficult to reach effective main diffusion, influenced mixture homogeneity.A kind of " flow mixer " disclosed in CN 1176148A, fluid a series of hybrid chambers of must flowing through, the hybrid chamber two ends have tubule (or capillary) to communicate, and can reach uniform mixing, but can't satisfy the fluid rapid mixing of moment.
At patent US 4,865, a kind of " the gas mixing, the distributor that are used for reactor " disclosed among 820 (or CN 1033753A), it is provided with first chamber and second chamber, tubular or slit shape passages by some, the gas of first chamber and second chamber is mixed fully, but this apparatus structure complexity, the installation requirement height.At patent US 5,113, a kind of " method of mixing ethane and chlorine " disclosed in 028, ethane flows in the person in charge, chlorine is injected but be 30～45 ° with the tube hub drift angle by 4 or a plurality of nozzle perpendicular to the person in charge, and two gases further mix in mixing duct subsequently, as seen this device technique is had relatively high expectations, and structure is complicated.In the clear 56-67534 of Japan Patent, disclose by a kind of " contact reactor ", behind first gas process ground floor beds, be divided into a lot of minizones by vertical partition plate, second gas is by the aperture ejection of dispersion pipe, finally reach even mixing by dispersion plate again, this apparatus structure is also complicated, more can't reach the requirement of moment mixing.
Content of the present invention
The object of the present invention is to provide a kind of quick gas jet mixer with high homogeneity, to overcome the prior art complex structure and can't satisfy the defective that the medium temperature difference is big, volume ratio is high, allowable pressure drop is little and can't reach the moment mixing, it not only has simple in structure, and can finish the even mixing of two strands of gases in moment.
Technical conceive of the present invention is such:
The key that realizes the moment mixing of gas high evenness is that realization body spreads and DIFFUSION IN TURBULENCE effectively, make second gas of introducing be distributed on the whole cross section of blender or pipeline equably with high-intensity momentum, and make it be dispersed into many micelles as far as possible, to increase the contact area between different material, finally finish mixed process by molecular diffusion.
According to above-mentioned design, the inventor has proposed the technical scheme of realization the object of the invention as described below:
The quick injection stream mixing arrangement of gas high evenness of the present invention comprises that a sidewall has Taper Pipe and a straight tube of jet orifice, and Taper Pipe is sleeved in the straight tube, and Taper Pipe is divided into a distribution cavity and a hybrid chamber with straight tube.
The vertex of a cone place of Taper Pipe is provided with the distribution grid of a porous, and this distribution grid is connected with first gas access, and first gas can enter in the hybrid chamber equably by the aperture on the distribution grid.
Straight tube is provided with the inlet of second gas, and second gas enters in the distribution cavity by this inlet.
When needs carried out rapid mixing with two kinds of gases, first gas was entered by inlet, and entered hybrid chamber in the Taper Pipe equably by the aperture on the distribution grid of porous; Second gas enters distribution cavity by inlet, enters hybrid chamber in the Taper Pipe by the jet orifice on the Taper Pipe side, forms a jet face, clashes into strongly and entrainments with first gas, carries out rapid mixing, and further mixes in hybrid chamber.
First gas enters hybrid chamber in the Taper Pipe by the aperture on the distribution grid of porous, improved the uniformity that first gas distributes on the cross section of hybrid chamber, second gas enters in the Taper Pipe by the jet orifice on the Taper Pipe sidewall, second gas of introducing is distributed at a high speed on the entire cross section in the Taper Pipe equably, the structure of the jet orifice on the Taper Pipe sidewall has possessed the wide and dark function of jet penetrating depth of jet coverage density simultaneously, fully realize main diffusion and DIFFUSION IN TURBULENCE, thereby can reach the requirement of high evenness moment mixing.
Device provided by the present invention, because of having simple in structure, the high characteristics of moment mixture homogeneity, so be particularly suitable for that the medium temperature difference is big, volume (mole) mixes than gas high evenness moment of high, atm number, as mixing between the premixed before the reactor, multistage catalytic fixed bed reactor region and pipeline gas mixing.Its mixed effect can each cross section concentration root-mean-square-deviation S characterize, S is littler, mixes more evenly, reaches the requirement that mixes when it is generally acknowledged S=0.05 substantially.
Wherein: S-----concentration root-mean-square-deviation c
i----------sample point concentration
N------sample point number c--------mean concentration
Figure of description
Below will be explained in detail the present invention by accompanying drawing.
Fig. 1 is the high evenness gas injection stream mixing apparatus schematic diagram before the reactor.
Fig. 2 is that first gas access is arranged on the gas injection stream mixing apparatus schematic diagram on the straight tube side.
Fig. 3 is the gas injection stream mixing apparatus schematic diagram of distribution-free plate.
Fig. 4 is a jet orifice distribution schematic diagram on the Taper Pipe sidewall.
Fig. 5 is dissimilar distribution grid schematic diagram.
As seen from Figure 1, high evenness gas injection stream mixing apparatus of the present invention, comprise the Taper Pipe (2) and the straight tube (1) that have jet orifice (5) on the sidewall, Taper Pipe (2) is sleeved in the straight tube (1), and sealing is fixed in the inwall of straight tube (1) and the inlet tube outer wall of first gas respectively, straight tube (1) lower end joins by a cambic conical shell and first gas inlet tube, and Taper Pipe (2) is divided into a distribution cavity (8) and a hybrid chamber (3) with straight tube.
The vertex of a cone place of Taper Pipe (2) is provided with a distribution grid (6) that has many uniform holes, this distribution grid (6) is connected with the inlet (7) of first gas that is arranged on the straight tube end, and first gas enters hybrid chamber (3) in the uniform hole on distribution grid (6) again by inlet (7);
The inlet of second gas (4) is arranged on the side of straight tube (1), and is connected with distribution cavity (8).
The semi-cone angle α of Taper Pipe (2) is 5～25 °;
The aperture of the jet orifice (5) that is provided with on the sidewall of Taper Pipe (2) is homogeneous or non-homogeneous, and the aperture is 10～120mm, the size of view apparatus and deciding; The perforate of non-homogeneous, the ratio of big aperture is 1～5, big aperture is staggered evenly distributed.Can be distributed on the same circumference as Fig. 4 A, also can be distributed on the different circumference as Fig. 4 B:
Distribution grid (6) can be hemispherical or conical distribution grid, it also can be sieve plate shape distribution grid, as shown in Figure 5, wherein A is a hemispherical dome structure, and B is a sieve plate shape structure, C is a conical structure, can choose any one kind of them during use, the aperture d in the uniform hole on the distribution grid (6) is 6～80mm, is evenly arranged on the distribution grid, pitch of holes is 1.5～4d, and the size of d depends on the size of the amount of first gas; Mixing the low slightly occasion of requirement, also distribution grid can be set.
As seen from Figure 2: except first gas access (7) are arranged on the side of straight tube (1), and be connected with distribution grid (6), and second gas is directly by outside the straight tube lower end double as import (4) by the transition of a bend pipe (9), remaining part all same Fig. 1 is set.This structure is suitable for the mixing of gas between multistage catalytic fixed bed reactor region and the mixing of two strands of gases of pipeline.
When needs carried out rapid mixing with two kinds of gases, first gas was entered by the inlet (7) of first gas, entered equably in the hybrid chamber (3) by the distribution hole on the distribution grid (6); Second gas enters distribution cavity (8) by the inlet (4) of second gas, enter in the hybrid chamber (3) by the jet orifice (5) on Taper Pipe (2) side again, form a jet face, clash into strongly and entrainment with first gas, under high turbulent flow, carry out rapid mixing, realize further in hybrid chamber (3) that simultaneously the diffusion of molecular level mixes.
First gas enters in the interior hybrid chamber (3) of Taper Pipe (2) by the uniform hole on the distribution grid (6), improved the uniformity that first gas distributes on the cross section of hybrid chamber, second gas enters in the hybrid chamber (3) by the jet orifice (5) of Taper Pipe (2), second gas of introducing is distributed on the whole cross section of Taper Pipe (2) apace, equably, the structure of jet orifice (5) has been taken into account the relation of the jet coverage density and the jet degree of depth on Taper Pipe (2) side, thereby can reach the requirement of rapid mixing.
As seen from Figure 3, except distribution grid (6) was not set, all the other structures all were similar to Fig. 1, and its operation principle is also with the explanation of Fig. 1.Require low slightly occasion for mixing, impermanence is not that a structure is more simply installed, and has certain practicality.
Further set forth content of the present invention below by embodiment.
Adopt device shown in Figure 1 to carry out the gas bulk testing.
First gas is for having added the air of tracer (ethanol), second gas is air, the diameter of straight tube (1) is 1100mm, spherical distribution grid (6) diameter is 500mm, aperture, distribution hole on the spherical distribution grid (6) is 38mm, uniform being arranged on the distribution grid, the semi-cone angle α of Taper Pipe (2) is 15 °, jet orifice on the Taper Pipe 2 (5) aperture is 38mm, the ratio of momentum of the first fluid and second fluid is 11.8, in hybrid chamber 3 exit sampling analyses, and employing formula (1) and formula (2) calculate, and root-mean-square-deviation S is 0.019.This digital proof device shown in Figure 1 has very good mixed effect.
Adopt device shown in Figure 1 to carry out the gas bulk testing.
First gas is for having added the air of tracer (ethanol), second gas is air, the diameter of straight tube (1) is 1100mm, spherical distribution grid (6) diameter is 720mm, aperture, distribution hole on the spherical distribution grid (6) is 32mm, the semi-cone angle α of Taper Pipe (2) is 10 °, the aperture of the jet orifice (5) on the Taper Pipe (2) is two kinds of 40mm and 25mm, big aperture is staggered evenly distributed as Fig. 4 A, the ratio of momentum of the first fluid and second fluid is 3.67, in hybrid chamber (3) exit sampling analysis, and employing formula (1) and formula (2) calculate, and root-mean-square-deviation S is 0.017.This digital proof device shown in Figure 1 has very good mixed effect.
Adopt device shown in Figure 2 to carry out the gas bulk testing.
First gas is for having added the air of tracer (ethanol), second gas is air, the diameter of straight tube (1) is 500mm, conical distribution grid (6) diameter is 200mm, aperture, distribution hole on the conical distribution grid (6) is 6mm, the semi-cone angle α of Taper Pipe (2) is 22.5 °, the aperture of the jet orifice (5) on the Taper Pipe (2) is two kinds of 10mm and 20mm, big aperture is staggered evenly distributed as Fig. 4 B, the ratio of momentum of the first fluid and second fluid is 4.50, in hybrid chamber (3) exit sampling analysis, and employing formula (1) and formula (2) calculate, and root-mean-square-deviation S is 0.022.This digital proof device shown in Figure 2 has very good mixed effect.
Adopt device shown in Figure 1 to carry out the gas bulk testing.
First gas is for having added the air of tracer (ethanol), second gas is air, the diameter of straight tube (1) is 500mm, sieve plate shape distribution grid (6) diameter is 200mm, aperture, distribution hole on the sieve plate distribution grid (6) is 6mm, the semi-cone angle α of Taper Pipe (2) is 7.5 °, the aperture of the jet orifice (5) on the Taper Pipe (2) is two kinds of 10mm and 30mm, big aperture is staggered evenly distributed as Fig. 4 A, the ratio of momentum of the first fluid and second fluid is 4.20, in hybrid chamber (3) exit sampling analysis, and employing formula (1) and formula (2) calculate, and root-mean-square-deviation S is 0.021.This digital proof device shown in Figure 1 has very good mixed effect.
Adopt device shown in Figure 3 to carry out the gas bulk testing.
First gas is for having added the air of tracer (ethanol), second gas is air, the diameter of straight tube (1) is 500mm, does not establish distribution grid, and the semi-cone angle α of Taper Pipe (2) is 5 °, the aperture of the jet orifice (5) on the Taper Pipe (2) is two kinds of 10mm and 50mm, big aperture is staggered evenly distributed as Fig. 4 A, and the ratio of momentum of the first fluid and second fluid is 7.20, in hybrid chamber (3) exit sampling analysis, and employing formula (1) and formula (2) calculate, and root-mean-square-deviation S is 0.055.This digital proof device shown in Figure 3 has mixed effect preferably.
Employing has the gas mixer of jet orifice commercial plant shown in Fig. 4 A, all same Fig. 1 of all the other structures.
First gas is the process gas of ethylbenzene and steam, temperature is 530 ℃, second gas is overheated steam, temperature is 750 ℃, the diameter of phi 1200mm of straight tube (1), spherical distribution grid (6) diameter is Φ 500mm, distributed aperture on the spherical distribution grid (6) is 32mm, and the semi-cone angle α of Taper Pipe (2) is 9 °, and the aperture of the jet orifice (5) on the Taper Pipe (2) is two kinds of 30mm and 20mm, big aperture is staggered evenly distributed, the ratio of momentum of the first fluid and second fluid reaches 5.56, and straight tube Different Diameter in exit is respectively 629.8 ℃ and 626.4 ℃ to the mixed temperature of position finding after mixing, about 3 ℃ of temperature deviation has very good mixed effect.This commercial plant blender meets design requirement fully.
Therefore, device of the present invention, not only simple in structure, can realize the rapid mixing of two strands of gases in moment, and have desirable mixed effect, can fully satisfy the specification requirement of industrial department, promote the technological progress of relevant industrial.
Claims (8)
1. quick gas jet mixer with high homogeneity, it is characterized in that: comprise that a sidewall has a Taper Pipe of jet orifice (5) (2) and a straight tube (1), Taper Pipe (2) is sleeved in the straight tube (1), and Taper Pipe (2) is divided into a distribution cavity (8) and a hybrid chamber (3) with straight tube (1); The vertex of a cone place of Taper Pipe (2) is provided with distribution grid (6), and distribution grid (6) is connected with the inlet (7) of first gas, and first gas is gone up equally distributed aperture by inlet (7) by distribution grid (6) and entered in the hybrid chamber (8); The semi-cone angle α of Taper Pipe (2) is 5～25 °; Distribution cavity (8) is connected with the inlet (4) of second gas, and second gas enters distribution cavity (8) by inlet (4), and spurts in the hybrid chamber (3) by the jet orifice (5) that is located on Taper Pipe (2) sidewall.
2. device as claimed in claim 1 is characterized in that: first gas access (7) can be arranged on the side of straight tube (1), and are connected with distribution grid (6) by the transition of a bend pipe (9).
3. device as claimed in claim 1 is characterized in that: distribution grid (6) can be removed, and directly hybrid chamber (3) is connected with the inlet (7) of first gas.
4. device as claimed in claim 1 is characterized in that: the semi-cone angle α of Taper Pipe (2) is 6～15 °.
5. device as claimed in claim 1 is characterized in that: the aperture that Taper Pipe (2) is gone up jet orifice (5) is 10～120mm.
6. device as claimed in claim 1 is characterized in that: the aperture that Taper Pipe (2) is gone up jet orifice (5) is homogeneous aperture or non-homogeneous aperture, and the aperture ratio of big aperture is 1～5.
7. as claim 1 and require 6 described devices, it is characterized in that: jet orifice (5) is distributed in same circumference or is distributed on a plurality of circumference, constitutes evenly being staggered of big aperture.
8. device as claimed in claim 1 is characterized in that: a kind of in hemispherical, taper shape or the sieve plate shape distribution grid of distribution grid (6), the aperture in the distribution hole on the distribution grid (6) is 6～80mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN02136075.8A CN1228133C (en) | 2002-07-17 | 2002-07-17 | Quick gas jet mixer with high homogeneity |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN02136075.8A CN1228133C (en) | 2002-07-17 | 2002-07-17 | Quick gas jet mixer with high homogeneity |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1468651A true CN1468651A (en) | 2004-01-21 |
| CN1228133C CN1228133C (en) | 2005-11-23 |
Family
ID=34146302
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN02136075.8A Expired - Fee Related CN1228133C (en) | 2002-07-17 | 2002-07-17 | Quick gas jet mixer with high homogeneity |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1228133C (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008077287A1 (en) * | 2006-12-27 | 2008-07-03 | Ningbo Wanhua Polyurethanes Co. Ltd. | An orifice jet-type injection reactor |
| CN101940878A (en) * | 2010-05-21 | 2011-01-12 | 中国神华能源股份有限公司 | Method for denitrating gas fume |
| US8042988B2 (en) | 2006-12-27 | 2011-10-25 | Ningbo Wanhua Polyurethanes Co. Ltd. | Hole-jetting type mixer-reactor |
| CN102658042A (en) * | 2012-04-23 | 2012-09-12 | 华东理工大学 | Low dropout flow guiding nozzle type mixing device for preparing styrene by ethylbenzene dehydrogenation |
| CN102824870A (en) * | 2012-08-10 | 2012-12-19 | 辽宁中顺科技装备有限公司 | Hydraulic stirring device |
| CN103629947A (en) * | 2013-10-24 | 2014-03-12 | 哈尔滨宏万智科技开发有限公司 | Mixed heating spray pipe |
| CN103962058A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Premixer, radial fixed-bed reactor and butaneoxidative dehydrogenation reaction system |
| CN108412641A (en) * | 2018-06-15 | 2018-08-17 | 潍柴西港新能源动力有限公司 | Fuel gas mixer |
| CN109894010A (en) * | 2019-03-05 | 2019-06-18 | 南京汇金锦元光电材料有限公司 | Flexible wide cut continuous magnetron sputtering plated film gas mixer |
| CN111905632A (en) * | 2020-08-18 | 2020-11-10 | 湖南京昌生物科技有限公司 | Low-resistance mixer, mixing method and application |
-
2002
- 2002-07-17 CN CN02136075.8A patent/CN1228133C/en not_active Expired - Fee Related
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008077287A1 (en) * | 2006-12-27 | 2008-07-03 | Ningbo Wanhua Polyurethanes Co. Ltd. | An orifice jet-type injection reactor |
| US8042988B2 (en) | 2006-12-27 | 2011-10-25 | Ningbo Wanhua Polyurethanes Co. Ltd. | Hole-jetting type mixer-reactor |
| CN101940878A (en) * | 2010-05-21 | 2011-01-12 | 中国神华能源股份有限公司 | Method for denitrating gas fume |
| CN101940878B (en) * | 2010-05-21 | 2012-12-05 | 中国神华能源股份有限公司 | Method for denitrating gas fume |
| CN102658042A (en) * | 2012-04-23 | 2012-09-12 | 华东理工大学 | Low dropout flow guiding nozzle type mixing device for preparing styrene by ethylbenzene dehydrogenation |
| CN102658042B (en) * | 2012-04-23 | 2014-05-07 | 华东理工大学 | Low dropout flow guiding nozzle type mixing device for preparing styrene by ethylbenzene dehydrogenation |
| CN102824870A (en) * | 2012-08-10 | 2012-12-19 | 辽宁中顺科技装备有限公司 | Hydraulic stirring device |
| CN102824870B (en) * | 2012-08-10 | 2015-09-09 | 辽宁中顺科技装备有限公司 | A kind of hydraulic agitation device |
| CN103962058A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Premixer, radial fixed-bed reactor and butaneoxidative dehydrogenation reaction system |
| KR20140098019A (en) * | 2013-01-30 | 2014-08-07 | 차이나 페트로리움 앤드 케미컬 코포레이션 | Premixer, radially fixed bed reactor, and reaction system for oxidative dehydrogenation of butene |
| US9718745B2 (en) | 2013-01-30 | 2017-08-01 | China Petroleum & Chemical Corporation | Premixer, radially fixed bed reactor, reaction system for oxidative dehydrogenation |
| RU2654041C2 (en) * | 2013-01-30 | 2018-05-15 | Чайна Петролеум Энд Кемикал Корпорейшн | Premixing device, reactor with fixed bed and radial flow and reaction system for oxidative dehydrogenization of butylene |
| KR102198625B1 (en) * | 2013-01-30 | 2021-01-05 | 차이나 페트로리움 앤드 케미컬 코포레이션 | Premixer, radially fixed bed reactor, and reaction system for oxidative dehydrogenation of butene |
| CN103629947A (en) * | 2013-10-24 | 2014-03-12 | 哈尔滨宏万智科技开发有限公司 | Mixed heating spray pipe |
| CN108412641A (en) * | 2018-06-15 | 2018-08-17 | 潍柴西港新能源动力有限公司 | Fuel gas mixer |
| CN109894010A (en) * | 2019-03-05 | 2019-06-18 | 南京汇金锦元光电材料有限公司 | Flexible wide cut continuous magnetron sputtering plated film gas mixer |
| CN111905632A (en) * | 2020-08-18 | 2020-11-10 | 湖南京昌生物科技有限公司 | Low-resistance mixer, mixing method and application |
| CN111905632B (en) * | 2020-08-18 | 2022-07-19 | 湖南京昌生物科技有限公司 | Low-resistance mixer, mixing method and application |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1228133C (en) | 2005-11-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101733056B (en) | Impinging stream micro-channel reactor and application | |
| CN1228133C (en) | Quick gas jet mixer with high homogeneity | |
| US4162971A (en) | Injectors with deflectors for their use in gassing liquids | |
| US8211375B2 (en) | Flow distribution device for downflow catalytic reactors | |
| CA2681583C (en) | Low-pressure-drop mixing device and use thereof in the mixing of two gases/vapours | |
| CN102658042B (en) | Low dropout flow guiding nozzle type mixing device for preparing styrene by ethylbenzene dehydrogenation | |
| CN107261873A (en) | Pipeline fluid mixer structure | |
| CN205550237U (en) | Organosilicon fluidized bed reactor gas distribution arrangement | |
| US4480925A (en) | Method of mixing fluids | |
| CN1073247C (en) | Liquid flow control device, reactor using same and liquid flow control method | |
| CN201735388U (en) | Gas distributor for gas-liquid dispersion | |
| CN205550244U (en) | Micro-channel reactor for producing nano sulfate | |
| CN1030284C (en) | Gas-gas mixing apparatus | |
| CN216890150U (en) | Variable-circulation multi-directional-flow efficient mixing reaction device | |
| CN202527113U (en) | Low-pressure-drop diversion nozzle type mixing device for preparing styrene through ethylbenzene dehydrogenation | |
| CN208727198U (en) | It is a kind of for mixing the gas mixer of nitrogen and ozone | |
| CN206935149U (en) | Pipeline fluid mixer structure | |
| RU203043U1 (en) | Complete dissolution aerator | |
| CN211813660U (en) | Jet aerator and sewage treatment system | |
| CN221182677U (en) | Novel gas mixing distributor for chloridizing reaction of chloroacetone | |
| CN106237938A (en) | Logistics mixing distributor and solid particle bed reactor | |
| CN218795160U (en) | Gas mixing tank for uniformly mixing multiple gases | |
| CN107281983A (en) | Micro-channel reactor for producing nano sulfate | |
| CN220834988U (en) | Ultralow specific gas-gas mixer for tail gas treatment | |
| CN113968614B (en) | Multistage cooperative self-circulation anaerobic ammonia oxidation reaction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20051123 Termination date: 20170717 |