CN1259124C - Annular space gas lifting type loop reactor - Google Patents
Annular space gas lifting type loop reactor Download PDFInfo
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- CN1259124C CN1259124C CN 200410078140 CN200410078140A CN1259124C CN 1259124 C CN1259124 C CN 1259124C CN 200410078140 CN200410078140 CN 200410078140 CN 200410078140 A CN200410078140 A CN 200410078140A CN 1259124 C CN1259124 C CN 1259124C
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Abstract
The present invention provides an annular space airlift inner ring current reactor which relates to an inner ring current reactor with high gas-liquid separation efficiency and favorable air distribution effect. The annular space airlift inner ring current reactor is mainly characterized in that a gas-liquid separator uses a funnel-tubule gas-liquid separation structure to realize complete gas-liquid separation; an air distributor is a sintered pipe distributor; and the air distributor has small initial air-bubble sizes and can realize the favorable air distribution effect. An inner member is arranged in an annular space lifting pipe in order to improve flow and strengthen mass transfer; and a heat exchange member is arranged in the annular space lifting pipe and is a finger-shaped pipe or a serpentine pipe in order to shift out or lead in heat required by the reaction,. The reactor has the characteristics of high gas-liquid separation efficiency, favorable air distribution effect and uniform radial direction of air content and liquid speed; and the pipe air distributor is used for guaranteeing that the phenomenon of fluid back recycle can not occur in the initial operational phase.
Description
Technical field
The present invention relates to a kind of reactor that is applicable to solution-air and gas-liquid-solid multiphase flow reaction system, relate in particular to a kind of annular space gas lifting type loop reactor, belong to technical field of chemical.
Background technology
Circulation flow reactor is widely used in many fields such as chemical industry, the energy, environment, biochemistry, compares with stirred tank, and Airlift circulating reactor is simple in structure, and gas is not only as reactant, and as a kind of energy carrier, each circulates promotion in bed.Circulation and outside circulation were two kinds in circulation flow reactor was divided into.Compare with external loop reactor, common loop reactor has simple in structure, easily the advantage of processing.In external loop reactor, the down-comer two ends link to each other with tedge by flange, because actual reaction system mostly is the HTHP system, material coefficient of thermal expansion coupling and withstand voltage properties have been proposed very high requirement, have increased difficulty of processing, have improved processing cost; In common loop reactor, inner core places within the urceolus, withstand voltage properties is required to reduce, thereby reduced difficulty of processing, has saved reactor cost.
Present common loop reactor adopts the central gas lift-type more, for some the strong heat release or the endothermic reaction, can not satisfy the heat exchange requirement; Therefore annular space gas lifting type then has bigger heat transfer area, can also in the annular space tedge heat exchange component be installed, and more easily realizes the importing of heat and shifts out, and has improved operating flexibility.
In circulation flow reactor, gas enters tedge, promotes liquid by the different density contrasts that cause of gas holdup between tedge and down-comer and circulates in bed.When gas speed is higher, because the motive force that the gas holdup difference causes is excessive, make that circulation fluid speed and bobble rise velocity are excessive, gas residence time is too short, and reaction conversion ratio is reduced; And when liquid speed was excessive, circulating fluid also can be carried a large amount of bubbles secretly and enter down-comer, and this can cause the generation of side reaction for some special courses of reaction, reduced the selectivity of reaction.Therefore, improving gas-liquid separation efficient is the important channel of improving reaction efficiency with the suitable liquid speed of control.Present most researcher is by adding expanding reach in reactor head, make the liquid prompt drop low to reach the purpose of gas-liquid separation, but when operating gas velocity is higher, because liquid speed is excessive, and it is not simple high as the separative efficiency of gas-liquid separator with expanding reach, have a large amount of bubbles and carried secretly and enter down-comer, can not guarantee needed separating effect.
In the solution-air of bibliographical information and the gas-liquid-solid circulation flow reactor, the orifice-plate type distributors that adopt more, there is following problem in such gas distributor: 1) the distribution of gas effect is bad, the incipient bubble diameter that general orifice-plate type distributor distributes is bigger, and in operating process because the hole plug that partly distributes makes gas distribution inhomogeneous.2) position of general orifice plate distributor is lower than the lower limb of inner core at the bottommost of reactor, when being applied to starch the attitude system, the problem that particle deposition stops up distributor takes place easily.When reactor began to feed gas, also occurring tedge and down-comer easily all had gas to pass through, and causes the phenomenon that can't circulate.Therefore, the design of gas distributor has great importance for the cloth device effect and the stable operation that improve circulation flow reactor.
In circulation flow reactor, when reactor is operated,, form the air pocket of a greater number because stronger bubble coalescence effect makes that the interior bubble size distribution of tedge is inhomogeneous under higher apparent gas speed condition, cause mass-transfer performance to descend, conversion ratio reduces.Therefore, circulation flow reactor in chemical process is used, high production capacity and high reaction conversion ratio mutual restriction.
In sum, develop that a kind of gas-liquid separation efficient height, good gas distribution are effective, stable operation, under higher operating gas velocity, still can keep the common loop reactor of higher conversion significant for a lot of chemical processes.
Summary of the invention
The purpose of this invention is to provide a kind of annular space gas lifting type loop reactor that is used for solution-air and gas-liquid-solid multiphase flow system, this reactor still can keep higher gas-liquid separation efficient, good gas distribution effect and excellent mass transferring performance and flow behavior under higher superficial gas velocity, thereby makes reactor have higher reaction conversion ratio and production capacity.
Technical scheme of the present invention is as follows: a kind of annular space gas lifting type loop reactor, the reactor urceolus that comprises its top band expanding section, inner core with the concentric installation of urceolus, the gas distributor that is arranged on the gas-liquid separator at inner core top and is arranged on reactor bottom, constitute the annular space tedge between described urceolus and the inner core, it is characterized in that: described gas-liquid separator adopts funnel one tubule formula separator, this separator is infundibulate, the bottom of funnel is connected with the inner core top, has some holes and vertical tubule is installed in the hole on funnel cone sidewall; Described gas distributor is made up of the substrate of perforate and the gas distribution tube that is installed in the hole, and this gas distribution tube is formed by connecting by sintered pipes and stainless steel tube two parts, and the hole on the described substrate is connected with stainless steel tube one end, and shut at the top of other end sintered pipes.
On the basis of such scheme, technical characterictic of the present invention also is: install in described annular space tedge in order to improve and flow and strengthen the inner member of mass transfer and install in order to shift out or to import the heat exchange component of reaction heat in described annular space tedge, this heat exchange component is dactylethrae or coiled pipe.
Another technical characterictic of the present invention also is: be provided with conical baffle between described substrate and interior tube bottom, the symmetry axis of this conical baffle overlaps with the symmetry axis of substrate.
The present invention compared with prior art has the following advantages and the high-lighting effect:
The present invention replaces expansion segmentation gas-liquid separator commonly used in traditional circulation flow reactor with funnel-tubule formula gas-liquid separator, has good gas-liquid separation effect, even when superficial gas velocity is higher, also can avoid a large amount of bubbles to carry secretly.In funnel-tubule formula gas-liquid separator, vertically diameter, height and the number of tubule have determined the resistance of gas-liquid separator, can realize adjusting to liquid speed by regulating these parameters in design, avoid that liquid is fast too highly to cause that a large amount of bubbles carries secretly.In addition, after gas-liquid or gas-liquid-solid mixture enter the vertical tubule of gas-liquid separator, because flow area dwindles, speed increases, mixture is injecting type and leaves flow separator, and liquid or liquid-solid mixture gravitate enter down-comer, thereby realizes good gas-liquid separation.Experimental study shows that bubble velocity and circulation fluid speed increase with the increase of superficial gas velocity, but the degree that increases reduces with the rising of superficial gas velocity, and after superficial gas velocity increased to certain value, bubble velocity and circulation fluid speed almost no longer changed with superficial gas velocity.This is because the increase degree of gas-liquid separator resistance is far longer than the degree that liquid speed increases, and has limited the growth trend of liquid speed.When superficial gas velocity is low, the resistance of gas-liquid separator is less, and its inhibitory action to liquid speed is also less, because gas-liquid separator has this self-adjusting ability among the present invention, make liquid speed be in the reasonable range, guaranteed that reactor can not reduce production efficiency because of the time of staying is too short.
Different with general circulation flow reactor, the present invention adopts the sintering pipe distributor, compare with the general orifice-plate type gas distributor that circulation flow reactor adopted, because the micro-pore diameter very little (＜100 μ m) on the sintered pipes, therefore the original dimension of bubble is little and even, and the speed of its vertical direction was zero when gas left sintered pipes, avoided the orifice-plate type gas distributor since bubble from causing near the lower phenomenon of the gas holdup distributor after the distributor ejection, make gas holdup comparatively even, have good gas distribution effect in axial distribution.In addition, can prolong or shorten sintered pipes length, make sintered pipes be higher than the lower limb of inner core, can avoid the reverse flow phenomenon that may occur in the operation start process and problem that can't normal circulation like this according to designing requirement.
When reactor of the present invention is installed inner member in the annular space tedge, can obviously improve mobile, bubble crushing and reinforcement mass transfer.When particularly operating gas velocity is higher, if do not add inner member, the initial gas uniformly that distributes by the distributor generation coalescence of steeping oneself-meeting, make bubble size inhomogeneous, form the air pocket of some, cause mass-transfer performance to descend, liquid speed, bobble rise velocity be skewness radially, add reactor inner member reasonable in design can make the problems referred to above be improved significantly.In addition, in the annular space tedge, add heat exchanger tube, and only use heat exchange jacket to compare, improved the heat energy power of moving of reactor, can make this reactor be used for the course of reaction of strong heat release or strong heat absorption.
Description of drawings
Fig. 1 is the front view of annular space gas lifting type loop reactor provided by the invention.
Fig. 2 is the profile of single gas distribution tube.
Fig. 3 is the B-B cutaway view of Fig. 1, expresses the gas distributor structure.
Fig. 4 is the A-A cutaway view of Fig. 1, expresses the gas-liquid separator structure.
The specific embodiment
Describe concrete structure of the present invention and embodiment in detail below in conjunction with accompanying drawing:
Annular space gas lifting type loop reactor provided by the present invention is mainly by reactor urceolus 1, reactor inner core 2 with the concentric installation of reactor urceolus, be arranged on inner member 3, heat exchange component 10 in the annular space tedge, gas-liquid separator funnel 9, be installed in vertical tubule 8 on the tapered sidewalls of gas-liquid separator funnel (gas-liquid separator funnel 9 and all vertical tubules mounted thereto 8 common constitute gas-liquid separators), be arranged on the distributor substrate 15 of reactor bottom and be arranged on gas distribution tube 12 on this substrate, conical baffle 14 is formed, as shown in Figure 1.The bottom of reactor urceolus 1 and distributor substrate 15 are connected with form of flanges, and there are certain distance in 15 of reactor inner core 2 and distributor substrates, and this distance can be regulated according to design.Reactor inner core sectional area is 0.1～0.5 with the ratio of reactor urceolus sectional area; Conical baffle 14 is between substrate and interior tube bottom, the symmetry axis of this conical baffle overlaps with the symmetry axis of substrate, its bottom links to each other with distributor substrate 15, avoid liquid in the down-comer excessive and damage reactor to the impulsive force of substrate 15, play the effect of water conservancy diversion simultaneously, improve flowing of reactor bottom.。
The structure of gas distribution tube 12 as shown in Figure 2, by being welded to form, shut with stainless steel blind plate or sintered plate on the sintered pipes top by stainless steel tube 17 and sintered pipes 18.Stainless steel tube links to each other with the distributor substrate, and the internal diameter of one section stainless steel tube of close substrate is 1/8～1/2 of a sintered pipes internal diameter, and the sintered pipes external diameter is 5～50mm; Can make gas uniform distribution in each gas distribution tube, the gas in the distributor pipe enters the annular space tedge from the sintered pipes micropore.
Gas distributor provided by the present invention is made of jointly distributor substrate 15 and some sintering tubular type gas distribution tubes 12, the arranging as shown in Figure 3 of distributor pipe.On one or several concentric circumferences on the distributor substrate 15, evenly have several holes, the number in hole can be determined according to designing requirement, each hole is connected with the stainless steel tube 17 of gas distribution tube 12, the sintered pipes of gas distribution tube should be higher than the lower limb of inner core 2 at least, to guarantee directly to enter the annular space tedge after gas leaves distributor, avoid when solid concentration is too high, the gas anti-channeling enters down-comer, causes the reactor can not normal circulation even reverse flow takes place.
For the heat of removing the reaction generation or the heat that imports reaction needed, in the annular space tedge of reactor, heat exchange component 10 is installed, this member is fixing by component holder 11.Heat exchange component is dactylethrae or coiled pipe.The quantity of heat exchange component and length are by the fuel factor and the operating condition decision of reaction.
When operating gas velocity is higher, because coalescence takes place in uphill process bubble, make bubble size distribution inhomogeneous, cause gas holdup to have tangible radial distribution, and liquid speed also can be the radial distribution that the limit wall is little, the center is big.In order to improve this radially inhomogeneous mobile distribution, the present invention is equipped with inner member 3 in the annular space tedge, and the number of inner member and installation site thereof reach DESIGN OF REACTOR by flowing in the bed and require to determine.Inner member 3 existing broken air pockets, thereby the effect of reinforcement mass transfer can play the effect that distributes again to flowing again.
At the urceolus top is an expanding reach, and the external diameter of this expanding reach can design according to producing needs, is generally 1.5～3 times of reactor urceolus diameter.Gas-liquid separator is funnel-tubule formula structure, whole separator is infundibulate, the column part of funnel and the gap between the expanding reach are 0～60mm, the bottom of funnel is connected with the inner core top, on one or several concentric circumferences on the cone sidewall of funnel, evenly have some holes, the hole links to each other with vertical tubule, the vertically diameter of tubule, quantity and highly can as requested gas-liquid separation efficient and circulation fluid speed determine that general vertical tubule total sectional area is 0.01～0.5 of an expanding reach sectional area.
In reactor of the present invention, material mobile as follows in reactor: gas is from the gas access 16, enter reactor annular space tedge through gas distribution tube 12, gas rises at the annular space tedge with bubble form entrained liquids or liquid-solid mixture, after the vertical tubule 8 of gas-liquid separator carries out gas-liquid separation, liquid or liquid-solid mixture Returning reactor inner core 2, gas leaves reactor from gas vent 7.Liquid 13 enters reactor from the liquid inlet, leaves reactor from liquid outlet 4.Cooling water enters heat exchange component 10 from cooling off water inlet 5, through behind the heat exchanging process, leaves reactor from steam (vapor) outlet 6.
Circulating bed reactor in the novel gas-lifting type involved in the present invention can be used for the gentle liquid-solid heterogeneous reaction process of gas-liquid, as wastewater treatment, methyl alcohol is synthetic, dimethyl ether is synthetic etc.
Claims (3)
1. annular space gas lifting type loop reactor, the reactor urceolus that comprises its top band expanding section, inner core with the concentric installation of urceolus, the gas distributor that is arranged on the gas-liquid separator at inner core top and is arranged on reactor bottom, constitute the annular space tedge between described urceolus and the inner core, it is characterized in that: described gas-liquid separator adopts funnel-tubule formula separator, this separator is infundibulate, the bottom of funnel is connected with inner core (2) top, has some holes and vertical tubule (8) is installed in the hole on funnel cone sidewall; Described gas distributor is made up of the substrate (15) of perforate and the gas distribution tube that is installed in the hole, this gas distribution tube is formed by connecting by sintered pipes and stainless steel tube two parts, hole on the described substrate is connected with stainless steel tube one end, and shut at the top of other end sintered pipes; Be provided with conical baffle (14) between described substrate and interior tube bottom, the symmetry axis of this conical baffle overlaps with the symmetry axis of substrate; The inner member (3) and the heat exchange component (10) in order to shift out or to import reaction heat that flow and strengthen mass transfer in order to improve are installed in the annular space tedge.
2. according to the described annular space gas lifting type loop reactor of claim 1, it is characterized in that: described sintered pipes external diameter is 5～50mm.
3. according to the described annular space gas lifting type loop reactor of claim 1, it is characterized in that: described inner core sectional area is 0.1～0.5 with the ratio of urceolus sectional area.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410078140 CN1259124C (en) | 2004-09-17 | 2004-09-17 | Annular space gas lifting type loop reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410078140 CN1259124C (en) | 2004-09-17 | 2004-09-17 | Annular space gas lifting type loop reactor |
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| CN1605385A CN1605385A (en) | 2005-04-13 |
| CN1259124C true CN1259124C (en) | 2006-06-14 |
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332748C (en) * | 2005-09-16 | 2007-08-22 | 清华大学 | Self circulated cascade gas lift type internal-loop reactor system |
| CN1321919C (en) * | 2005-10-14 | 2007-06-20 | 北京工业大学 | Technological process and apparatus of serial gas stripping inner circulation reactor |
| CN101209402B (en) * | 2006-12-27 | 2011-11-30 | 西安航天华威化工生物工程有限公司 | Shell pass multi-cavity type multi-layer bed fixed bed reactor |
| CN101209401B (en) * | 2006-12-27 | 2011-10-26 | 西安航天华威化工生物工程有限公司 | Shell pass multi-cavity type fixed bed reactor |
| CN102049175B (en) * | 2009-10-27 | 2013-08-28 | 中国石油化工股份有限公司 | Gas-liquid circulation flow reactor and method for treating odorous waste gas containing hydrocarbons |
| CN102309914B (en) * | 2010-07-07 | 2014-04-16 | 中国石油化工股份有限公司 | Treatment method for stinky waste gas discharged by storage tank |
| CN102580628A (en) * | 2012-03-02 | 2012-07-18 | 青海中航资源有限公司 | Device and method for simultaneously producing chloromethane and ammonia by taking ammonium chloride as raw material |
| UA122964C2 (en) * | 2014-11-12 | 2021-01-27 | Ені С.П.А. | Reaction device with air-lift type internal circulation |
| CN106318853B (en) * | 2015-06-23 | 2018-12-14 | 中国科学院上海高等研究院 | Automatically cleaning spiral biologicalreactorwithinnercyclicfowofairlifttype |
| EP3290105B1 (en) * | 2016-08-30 | 2021-01-20 | Alfa Laval Corporate AB | Method for evaluating lifting force in a heat exchanger |
| CN108579418A (en) * | 2018-05-07 | 2018-09-28 | 安徽金森源环保工程有限公司 | A kind of ammonium hydroxide gasification burner and its working method |
| CN110252213B (en) * | 2019-05-27 | 2022-03-22 | 河北科技大学 | Fluidized bed reaction device for producing chloromethane and ammonia |
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