CN100561036C - Be used for the two-phase flow shunting is become the device of two or more stream thighs with required vapour-liquid ratio - Google Patents

Abstract

The present invention is a kind of equipment (30) that is used for two-phase inlet flow (41) shunting becoming two or more output streams (42,43).This equipment can be designed as to be kept in each output stream near identical vapour-liquid ratio.The inlet flow of described equipment flows to SEPARATOR OR SEAL CHAMBER (31) by input pipeline (32).In this container, input mouth of pipe below is provided with a striking plate (33), and wall guided should stream strand with the high speed of destroying stream strand and in separator, and liquid will separate in this place impact and with vapour phase.In SEPARATOR OR SEAL CHAMBER, obtain separating of liquid phase and vapour phase.Two vertical suction passages (34,35) are positioned at separator inside.These suction passages and two output pipelines (44,45) fluid are communicated with, and output stream leaves separator by described output pipeline.The lower end of described suction passage is immersed in the liquid phase (39).Described suction passage is provided with hole (36) on sidewall.Vapor stream is crossed the bore portion of liquid level top in the separator.When vapor stream is crossed these holes, produce pressure drop inside and outside the suction passage wall.Therefore liquid be raised and enter suction passage.Upwards flow through suction passage and leave separator and two-phase flow shunt of the vapor mixing of liquid and suction passage inside, biphasic mixture by output pipeline.

Description

Be used for the two-phase flow shunting is become the device of two or more stream thighs with required vapour-liquid ratio

Background of invention

Invention field

The present invention relates to a kind of being used for will comprise the light phase fluid that for example steam and liquid are such and the two-phase inlet flow of heavy phase fluid, splits into the device of two or more two-phase output streams.This device can be guaranteed the vapour-liquid ratio that each output stream obtains expecting.The total discharge of each output stream needn't be identical.The present invention is suitable for but is not limited to the two-phase process flow stock along pipeline or channel flow is flow to the application of in parallel heat exchanger, boiler tube, air-cooler, chemical reactor or pipe-line system.

Correlation technique

In a lot of operating units, all need the separation of two-phase flow, use the dissimilar scheme to more complicated two-phase flow shunt of associate simple symmetrical pipeline shunt (piping split) or threeway in history.

Two-phase process flow stock can be divided into 6 big classes from equipment:

The first kind: the symmetrical pipeline shunt that uses the standard three-way pipe

The traditional approach that separates two-phase flow is to use the standard three-way pipe to make symmetrical pipeline shunt, and relies on this state and come mean allocation to arrive each arm.One is used for two-phase flow is divided into the example of symmetrical pipeline shunt of four output streams shown in the isometrical drawing of Fig. 1.The two-phase inlet flow flows in input pipeline 1.Pipeline 1 makes two-phase flow flow to first threeway 3, and this place's stream thigh is divided into two output streams.In this example, 90 ° of bend pipes 2 are positioned at the upstream of threeway 3.Owing to act on the centrifugal force on the liquid, liquid trends towards flowing near the long radius wall of bend pipe, and steam then trends towards flowing near the minor radius wall.Thereby bend pipe causes being separated and the uneven distribution of steam, liquid across cross-section of pipeline.Minimum in order to be dropped to by the negative effect for shunting performance in the threeway 3 that upstream bend pipe 2 causes, pipeline 1 is as the plane perpendicular to threeway 3 definition that illustrates.In threeway 5a and 5b, be further divided into two output streams from each the stream thigh in two output streams of threeway 3.There is bend pipe 4a threeway 5a upstream, and there is bend pipe 4b threeway 5b upstream.Equally drop to minimumly for the negative effect for shunting performance among threeway 5a and the 5b that will cause by being separated among upstream bend pipe 4a and the 4b, pipeline 7 is perpendicular to two planes by threeway 5a and 5b definition.By using the pipeline shunt of symmetry, the inlet flow in the pipeline 1 is divided into four product stream thighs that flow thus in pipeline 6a, 6b, 6c and 6d.

The pipeline shunt of symmetry may be the most widely used method that is used for the two-phase inlet flow is separated into two or more output streams.Yet history shows that under many circumstances, this principle can not successfully be evenly distributed to output stream with liquid, steam, causes the vapour-liquid ratio difference in the output stream.The subject matter of standard threeway cast symmetry tubes road shunt is that the performance of stream stock stream will depend on the type of flow in the upstream line, and may not total energy keep the disperse flowing state of expectation under all related work situations.The disperse flowing state is a kind of in flow channel or pipeline, and droplet evenly distributes in continuous vapour phase, or in liquid phase continuously the equally distributed flowing state of small bubble (blister flows).The performance of symmetry pipeline shunt also can depend on the existence of the pipe fittings of pipeline shunt upstream as previously mentioned.It is identical that the main limitation of symmetry pipeline shunt is that the flow rate of output stream will be bordering on, to avoid the remarkable difference of output stream vapour-liquid ratio.Another limitation is that two-phase flow can only be divided into the output stream of numbers such as 2,4,8,16 symmetrically.Therefore can not produce 3,5,6,7, the output stream of number such as 9....

The existing proposal by injecting chemicals improves standard threeway cast symmetry tubes road shunt with the surface tension that reduces pipeline shunt upstream liquid performance.After reducing surface tension of liquid, under lower flow rate, will obtain the disperse flowing state.Can obtain the acceptable performance of symmetrical pipeline shunt thus in wider vapour-liquid flow rate range.U. S. Patent 5,190,105 have provided an example, and wherein surface active agent is injected into a plurality of injection wells in the upstream of the two-phase flow pipeline shunt of saturated steam and water, thereby guarantee that each quality (vapor portion) of injecting well is identical, with recovered oil from oil conservator better.

Second class: in three-way pipe, use special insert as blade, baffle plate or static mixer.

People have carried out multiple trial, attempt the shunting performance that improves the standard three-way pipe as the pipeline insert of blade, baffle plate or static mixer by using.

U. S. Patent 4,396,063 has recorded and narrated first example, and wherein static mixer just is positioned at a upstream that comprises the threeway of a Y-branch.For the shunting performance that obtains, promptly the vapour-liquid ratio of each output stream is identical, and disperse stream is for preferred.In the disperse flowing state, biphasic mixture can be taken action as monophasic fluid.Droplet is tending towards following vapor stream with roughly the same speed, or vice versa.Therefore under the disperse flowing state, often can obtain good shunting performance in the three-way pipe.The use of the static mixer of threeway upstream provides the surface perpendicular to the certain area of contour of having of flow direction in the input pipeline.Liquid can impact these surfaces and separate with vapour phase thus.If therefore adopt, static mixer can disturb the disperse flowing state of expectation, and can cause separating of undesirable liquid and steam.Use static mixer can introduce extra pressure drop in operation system, owing to increased the energy consumption of pump and/or compressor, this can cause extra operating cost.Static mixer is also polluted by the pollutant as rust and corrosion products easily.

U. S. Patent 4,824,614 have recorded and narrated second example.This shunt comprises that also one is arranged in the static mixer 22 of the input pipeline of threeway 14 upstreams, and wherein inlet flow 30 is divided into two output streams 74 and 76.One horizontal slice device 24 (horizontal stratifier) is arranged between static mixer 22 and threeway 14.This quantizer is collected fluid from six different heights.Be sent to output stream 76 at minimum i.e. first fluid of highly collecting, be sent to output stream 74, be sent to output stream 76 at the 3rd fluid of highly collecting at second fluid of highly collecting, or the like.As the mixer of first example, the mixer in this example will be tending towards separating liquid from steam, and this is undesirable.This static mixer also can increase operating cost, and vulnerable to pollution.This quantizer is collected fluid and is only striden under the equally distributed situation of cross-section of pipeline at steam and liquid and work, and does not have this situation in actual applications.Mixer/quantizer is combined in U. S. Patent 5,810, tests in the application on the spot of 032 water vapour/water of recording and narrating.The result of this test is than having obtained the shunting of better water vapour and water with mixer/quantizer combination in the threeway of standard buffering.

U. S. Patent 5,810,032 has recorded and narrated the 3rd example.Dissimilar standard pipe threeway inserts is diverted to injection well in parallel with all testing from the oil conservator recovered oil better on the spot in the laboratory with sky G﹠W with water vapour/aqueous mixtures.Studied the pipeline insert of three major types: the static mixer in standard threeway upstream, use throttle valve or nozzle in the perpendicular flow baffle plate of standard threeway upstream and two output branch roads in the standard threeway.Also studied the combination of these three kinds of inserts.Conclusion is the slight improvements that static mixer and vertical baffle only cause shunting performance.In two output branch roads, use throttle valve or nozzle to be claimed the good slightly shunting performance that can cause tested flowing state.Yet do not know what the driving force that liquid is evenly distributed to the output branch road of nozzle and threeway is under the situation of liquid and steam non-uniform Distribution in the input pipeline cross section.In disperse or blister flowing state (drop of vapour phase or the bubble of liquid phase continuously continuously), also do not finish any laboratory flow test, estimation flowing state in laboratory test is laminar flow, wavy laminar flow, slug flow and circulation, predicts as the two-phase flow graph (among the Hydrocarbon Processing in October, 1969 the 105th to 116 page " How to size process piping for two-phaseflow ") that uses Ovid Mr. Baker.This may be find under low flow velocity and low liquid branch rate situation, to have or do not have the divergence of the standard threeway of insert why can better reason.Preferred flow at high speed state, disperse and blister flowing state are from not test (N.T.).If disperseing DisperseTest with the blister flowing state, conclusion very may be different so.

Other people propose to use significantly improved threeway, and do not use special insert in the standard pipe threeway.Japan Patent 62059397A2, U. S. Patent 4,528,919 and U. S. Patent 4,512,368 have been recorded and narrated the example of improved branch pipe tee connection.

The 3rd class: the equipment that depends on the particular flow state of setting up in pipeline shunt upstream.

Owing to lack accurate flowing state figure, be difficult in and predict flowing state in the commercial Application.Most of flowing state figure are mainly based on the mobile status data of the two-phase of small diameter pipeline (＜2 inches) hollow G﹠W.Therefore for example in hydrocarbon/hydrogen system, under the high pressure-temperature in picture hydrotreatment unit, flowing state figure may be inaccurate.

Except flowing state figure unreliable, also there be thermodynamic model unreliable of the amount that is used to predict liquid and steam and character.This unreliability for example may be very remarkable for the hydrocarbon systems of complexity, and wherein hydrocarbon is characterised in that and has adopted pseudocomponent, and has wherein used equation of state to predict evapouration discharge and fluid properties.

Pipe-line system in the treatment plant also often be have as expand, shrink, curve, the complex system of pipe fittings such as safety check.Whenever two-phase flow through these pipe fittingss, total flowing state will be disturbed and be needed long straight pipeline rebuild total flowing state.For example, as previously mentioned, curve and be tending towards separating phase, make heavy liquid phase near curving the motion of long radius wall, lighter steam is near curving the motion of minor radius wall.

Owing to these three reasons, the actual flow state in usually impossible accurately predicting pipeline or the flow channel.In addition, owing in the operating environment as the variable of temperature, pressure, flow rate and fluid chemistry composition and so on, can not all keep a flowing state under all the associative operation environment in operating unit usually.Yet a lot of two-phase flow shunts are designed to only be used for a flowing state.

U. S. Patent 4,516,986 have recorded and narrated first example of this two-phase flow shunt.This shunt comprises inserting is responsible for pipe 12 in one in 10.At interior pipe with in the annular section between being responsible for a baffle plate 13 is arranged.The flowing state of expecting among the person in charge is the annular flow state, wherein flows near the cyclic rings of liquid tube wall, and steam is to flow at tube hub at a high speed.The partially liq attempt of flowing near tube wall converges in the closed end volume 14.From this closed end volume 14, flow of liquid is passed through control valve 23 through outside line 15.Steam converges from the ring-type vapor volume 30 in baffle plate 13 downstreams and sends by pipeline branch road 11, at this branch road, and steam and from the liquid of control valve and stream.Flowmeter 20 in the pipeline branch road 11 in the two-phase flow is used for controlling liquid stream.How accurately flowmeter MEASUREMENT OF STEAM liquor ratio does not give statement.For the MEASUREMENT OF STEAM liquor ratio, need the independent flow measurement of steam and flow of liquid usually.Other flowing states outside circulation, slug flow for example, the shunting performance of equipment may be very poor.Even circulation is the flowing state of dominating in 10 being responsible for, any be positioned at the shunt upstream as the pipe fittings of bend pipe all with Interference Flow.Therefore need specific straight-tube portion in the shunt upstream, its will be in operating unit the occupying volume external space.Also may there be restriction in the amplitude of variation of flow rate.Be lower than design load when total flow rate is reduced to, the pressure drop by baffle plate 13 reduces fast, and the effective pressure drop by control valve 23 can reduce too fast.Open fully at certain point control valve, again controlling liquid stream.By introducing measuring instrument and control valve, this system is no longer simple and firm as other two-phase flow shunts, and increases by the pressure drop of shunt.Higher pressure drop can increase the operating cost of pump pressure in the operating unit and/or compression usually.This patent has been described the method that produces two strands of output streams.Three or more if desired strand output streams so very likely need the shunt of two or more series connection.A lot of if desired output streams, then separate system will become quite complicated, and required pressure drop will become excessive.

U. S. Patent 4,800,921 have recorded and narrated second example, and wherein for level header 16 provides output arm 14a, 14b, 14c etc., upstream output arm is in high height, and the height of each downstream output arm reduces in succession.This scheme should be, if circulation is the flowing state in the collector pipe, the different heights of exporting arm so should guarantee that the thickness of ring-type liquid ring is roughly the same at each output arm place.Then the vapour-liquid ratio in each tributary is claimed near identical.As already mentioned, be difficult to all associative operation environmental forecastings and remain on a certain flowing state.In addition, even circulation can be kept, expect that also vapour-liquid ratio is the function of the total flow rate of each bye-pass in main line.Flow rate in each bye-pass is high more, and the steam that is inhaled into pipeline is many more, and then vapour-liquid ratio is high more.If in certain operational modes, flowing state is different with expection, and for example laminar flow then causes the described serious skewness that arrives the output branch road mutually.

U. S. Patent 4,574,837 have recorded and narrated the 3rd example, wherein suppose known a certain distribution mutually in the level person in charge 10.The person in charge has the opening at different heights, at first flows to annular container 12 to allow fluid, further arrives arm 13 again.The vapour-liquid ratio of stream thigh is determined by the suitable flow area of selecting to lay respectively at the opening of managing 10 tops and bottom in the arm.Pipe top flow area is high more with respect to the bottom flow area, and the vapour-liquid ratio that obtains in the arm is high more.Described equipment only works at laminar flow and undulating horizon flowing state.And liquid level in being responsible for and prediction is the same, and described equipment will only produce the shunting with required vapour-liquid ratio.Therefore this equipment will be only to low speed and to fixing vapour-liquid when characteristic work.The feature that most commerce is used is high flow rate and the vapour-liquid notable change of characteristic when.

U. S. Patent 4,574,827 and 5,437,299 have recorded and narrated other examples of the shunt that depends on the particular flow state of setting up in pipeline shunt upstream.

The 4th class: the equipment of applying centrifugal force.

At U. S. Patent 5,059, recorded and narrated centrifugal two-phase flow shunt in 226.This centrifugal shunt has a tangential fluid input 28 to feed a vortex chamber 23.Have a central hub 38 and blade 39 in this bottom, vortex chamber, steam that Scroll-tupe is mobile and liquid guiding are to delivery outlet 36 and enter output channel 37.Be not easy to understand what the driving force that liquid phase distributes is.Owing to have only an inlet 28 in a side of equipment, so the liquid inlet is not symmetrical.Liquid is mobile along vortex chamber's inwall Scroll-tupe, but because asymmetrical design can't form the thickness that evenly flows with uniform liquid layer/film.Therefore, some blade 39 estimates and can concentrate more liquid than other blades, and what cause output channel 37 is not best liquid distribution.

The 5th class: use extra power to produce the equipment of disperse stream.

European patent 0003202 B1 has recorded and narrated an example of this equipment.The pipeline shunt upstream that gyratory agitation device on motor 32 and the axle 28 is used for being diverted at inlet flow output channel 4a, 4b and 4c makes liquid and vapour mixture disperse.Since can be regardless of the variation of flow rate and liquid property, and produce the disperse flowing state by the shaft work that increases axle 28, so this equipment may be effective.The subject matter of this equipment is the sealing that will obtain between axle 28 and pipeline/bend pipe 21, and this is not an easy task (not being cheap design) under the high-voltage applications as hydrocracking (up to 300 crust).The energy consumption cost of the initial cost of rotating equipment, maintenance cost and motor is also all very high.

The 6th class: separate steam and liquid in the inlet flow earlier, again each is distributed to mutually the equipment of output stream.

Use traditional vapour/liquid/gas separator and conventional apparatus two-phase inlet flow shunting is become three output streams shunt first example as shown in Figure 2.The two-phase inlet flow flows to separator 10 by pipeline 11, separates with vapour phase 12 in this place's liquid phase 13.Vapour phase flows to control valve 15a, 15b and 15c in parallel along steam output pipe line 14.The position of control valve or lifting height are by flow dontroller 16a, 16b and 16c control, to obtain the required steam flow rate by each control valve.Flow measurement is by using the conventional method acquisition in conjunction with Δ P sensor of any as orifice plate or Venturi tube.Flow dontroller is connected with a pressure controller 17.Pressure controller changes flow setting value to keep pressure required in the separator according to flow dontroller 16a, 16b, 16c.Liquid phase 13 flows to control valve 19a, 19b and 19c in parallel along liquid output pipe line 18.The position of control valve or lifting height are passed through the required liquid flow rate of each control valve with acquisition by flow dontroller 20a, 20b and 20c control.Flow measurement is any as the conventional method acquisition of orifice plate in conjunction with Δ P sensor by using.Flow dontroller is connected with a fluid level controller 21.Fluid level controller will change flow setting value to keep liquid level required in the separator 10 according to flow dontroller 19a, 19b and 19c.At last, merge from the steam flow thigh of valve 15a, 15b and 15c and flow of liquid thigh, to produce three strands of two- phase output streams 22,23 and 24 from valve 19a, 19b and 19c.

The device of two-phase flow shunt shown in Figure 2 is quite complicated, and along with as the complexity of the element of sensor, control valve and controller and so on and the increase of number, the risk of failure and upset also increases.The Tai Gao or too low if vapour-liquid ratio becomes in the failure of this control system or in upsetting, some down-stream system may be damaged.For example the vapour-liquid ratio of the stream thigh that flows in pipe increases suddenly, because the overheated risk that can produce carbon build-up in pipe break or the boiler tube of pipe.Another kind of example is if reactor is operated under low excessively vapour-liquid ratio and caused scarce hydrogen, even in very short time, also can produce the risk of quick carbon build-up in the catalytic hydrogenation treatment reactor of parallel connection.Control system complexity and separator flask 10 sizes greatly also can cause the expensive of shunt.

U. S. Patent 4,293,025 has recorded and narrated second example.This two-phase flow shunt comprises that one has the separator flask 10 of the two-phase input mouth of pipe 11.Striking plate 14 is positioned at below the input mouth of pipe, to destroy the high flow rate of inlet flow.Have two or more chimneys 12 (chimney) in the separator.The upper end of chimney is open, enters chimney to allow steam.Chimney has hole 13, so that liquid enters chimney.Cap 16 is positioned at chimney opening top, directly enters to avoid the liquid above chimney.Fluid flow to each chimney is determined by the fluid head of 13 tops, hole and the flow area in hole.For liquid level given in the container, the fluid flow that arrives each chimney is with near constant.Therefore this fluid head becomes liquid distribution and will guarantee the constant fluid flow of each output stream rather than constant vapour-liquid ratio to the two-phase flow shunt of the driving force of the output stream that walks abreast.Another problem that fluid head becomes the shunt of distribution driving force is limited fluid flow amplitude of variation.The area of necessary measuring hole 13 is to obtain the middle liquid level under the design liquid flow rate.If suppose highly by 50% at some mode of operation fluid flow, then liquid level will be higher about 2.25 times than the design liquid level, and liquid may can overflow chimney thus and cause the liquid distribution inequality of output stream.If the fluid flow supposition is lower by 50% than the design fluid flow, then liquid level will only be about 25% of expectation liquid level.In low liquid level, owing to the high sensitivity to fluctuation, the installation of non-level and other manufacturing tolerancess, it is very poor that liquid-distribution property may become.Can be by the fluid flow amplitude of variation that the hole enlarges shunt being set at more height place.Yet if at more height place the hole is set, the liquid-distribution property of design point is with respect to only a shunt decreased performance that highly has the hole.

U. S. Patent 4,662,391, Japan Patent 03113251 A2 and Japan Patent 02197768 A2 recorded and narrated other the example that liquid level is the shunt of the liquid driving force that is evenly distributed to each output stream.

U. S. Patent 5,250,104 have recorded and narrated the 3rd example of the shunt of separating liquid and vapor phase.The biphasic mixture that flows in the pipeline 14 is separated at separator 12.Vapour phase is divided into two stream thighs in threeway 20.In this two vapour phases stream thigh each is by hole 22 and 24.Liquid is concentrated in sump 30 and through two parallel liquid lines 32 and 34.The pressure drop Δ Pv of the steam flow by the hole almost be proportional to the volume steam rate square.Liquid stream is by the pressure drop Δ P of liquid line 32 and 34 _LComprise a static Δ P owing to the height difference of the liquid level of the liquid level in the sump 30 and fluid pipeline end 40 and 42 _SLWith a friction term Δ P _FLΔ P _FLAlmost be proportional to the volume of liquid flow rate square.Because steam and liquid are parallel paths by the path of shunt, described pressure drop needs identical:

ΔPv＝ΔP _SL+ΔP _FL (1)

The flow area of steam hole and fluid pipeline be according to the size manufacturing to reach specific steam flow rate Q _VWith specific liquid flow rate Q _LIf for example actual vapor flow rate is high by 50% in some operator scheme now, then Δ Pv is higher by 125% than what estimate.Because fluid flow is constant, Δ P _FLAlso be constant.In order to satisfy equation (1), Δ P _SLTherefore must increase by 1.25 * Δ Pv.Liquid level in the sump 30 needs significantly to reduce as a result, and at certain a bit, will not have liquid level in the sump 30, and steam and liquid all will enter liquid line 32 and 34.In this case, will cause the bad distribution of liquid to parallel pipeline 32 and 34.On the other hand, if vapor flow rate hypothesis ratio design vapor flow rate is low by 50% in some operator scheme, then Δ Pv hangs down 75% than what estimate.Under the sort of situation, the liquid level in the sump 30 will significantly raise and overflow sump, cause liquid to flow to hole 22 and 24 and skewness.This shunt is proper functioning under design steam flow rate and liquid flow rate only.The liquid of this shunt and vapor flow rate amplitude of variation are not enough for most commercial Application, and the common feature of described commercial Application is liquid and steam flow rate and as density, viscosity, capillary liquid and all notable changes of vapor quality.

Brief summary of the invention

The present invention is the device that is used for two or more output streams of two-phase inlet flow shunting becoming.This device can be designed to keep in each output stream near identical vapour-liquid ratio.

The shunt of one embodiment of the invention is shown in Fig. 3 A, 3B and 3C.Inlet flow flows through an input pipeline and arrives a separator flask.Input mouth of pipe below in the described container is provided with a striking plate and guides to the separator inwall with the high flow rate of destruction stream thigh and with described stream, and liquid will clash at this place and separate with vapour phase.In separator flask, finish separating of liquid phase and vapour phase.

Be provided with two vertical suction passages in separator inside.These suction passages are communicated with two output pipeline fluids, and output stream leaves separator by described output pipeline.Being submerged in the liquid phase of suction passage than low side.Perforate on the suction passage sidewall.Steam is moving by the orifice flow that is arranged in separator liquid level top.Moving when steam by these orifice flows, just produced the inside and outside pressure drop of suction passage wall.Liquid raises and enters described suction passage as a result.The vapor mixing of liquid and described suction passage inside, biphasic mixture upwards flow through passage and leave separator and two-phase flow shunt by output pipeline.

Liquid level in the separator is mainly by the steam flow rate decision that enters container.Liquid level height under the lower steam rate, liquid level is low under the high steam flow rate.The liquid body flow rate influence hardly of described liquid level.

Different with above-mentioned prior art, the present invention has following advantage:

A) shunt of the present invention can be designed as to keep in output stream and is bordering on identical vapour-liquid ratio.Perhaps, shunt can be designed as and keep specific different vapour-liquid ratio in output stream.

B) shunt of the present invention can be designed as any split ratio.Even actual split ratio is different from the design split ratio of shunt in some operational phase, the present invention also can be effective.

C) shunt of the present invention all will play a role equally well under all flowing states in input pipeline.

D) shunt of the present invention is not very sensitive to the arrangement of upstream or downstream line system.For example, its performance can not be subjected to the shunt upstream as the influence that curves or the pipe fittings of valve exists.

E) shunt of the application of the invention can produce the output stream of arbitrary number.Use the symmetrical pipeline shunt of buffering threeway (impact tee) can only produce 2,4,8 ... Deng an output stream, and the present invention also can produce 3,5,6,7,9 ... Deng an output stream.

F) shunt of the present invention has been represented the design of a simple rigid.It does not have detection facility and moving member.It only needs low the maintenance, and does not need the concern of plant operator.

G) shunt of the present invention is an open system, is not vulnerable to pollute.In operating unit, use this shunt therefore will can not influence the overvoltage protection principle.For the hydroprocessing unit, the equipment that is positioned at the shunt upstream can still be subjected to being positioned at the overvoltage protection of the pressure-relief valve in shunt downstream thus.

H) no matter the pressure drop of down-stream system have how high, the pressure drop of shunt very low (being～0.05 crust under design conditions).

I) shunt of the present invention has been represented the big design of cost effect of a compactness.

Brief Description Of Drawings

Fig. 1 has showed prior art, is the isometrical drawing of the pipe-line system that comprises of symmetrical pipeline shunt.In this example of symmetrical pipeline shunt, inlet flow is divided into 4 output streams by using three standard pipe threeways.

Fig. 2 has also showed prior art, is the process flow diagram that is used for inlet flow is split into the vapour/liquid/gas separator with metering device of three output streams.

Fig. 3 A, 3B and 3C have showed one embodiment of the invention.Fig. 3 A is this embodiment's of dissecing along the A-A line a side cross-sectional views.Fig. 3 B is the viewgraph of cross-section that dissects along the B-B line.Fig. 3 C is the plan view that dissects along the C-C line.

Fig. 4 shows that first of shunt of the present invention makes the process flow diagram of use-case.This shunt is used for two-phase flow is diverted to the processing system of three parallel connections that comprise heat exchanger, metering device and boiler tube.

Fig. 5 shows that second of shunt of the present invention makes the process flow diagram of use-case.This shunt is used for two-phase flow is diverted to the dropping liquid bed chemical reactor of two parallel connections.

Fig. 6 A, 6B and 6C have showed another embodiment of the present invention, and have shown the design of optional suction passage.Fig. 6 A is this embodiment's of dissecing along the A-A line a viewgraph of cross-section.Fig. 6 B is the side cross-sectional views of dissecing along the B-B line.Fig. 6 C is the side cross-sectional views of dissecing along the C-C line.

Fig. 7 A and 7B have showed the embodiment more of the present invention that shunt is made into the constituent element of chemical reactor.Fig. 7 A is the side cross-sectional views of chemical reactor bottom.Fig. 7 B is the viewgraph of cross-section of the suction passage that dissects along A-A line among Fig. 7 A.

Fig. 8 has showed one embodiment of the present of invention that shunt is made into the constituent element of housing and pipeline thermal exchanger.Fig. 8 is the side cross-sectional views of heat exchanger and shunt.

Optional embodiment of the present invention includes but not limited to the design shown in the figure.

Background of invention

The industrial treatment equipment upstream of a lot of types all needs two-phase flow is separated into two or more output streams and has identical vapour-liquid ratio in each output stream.For example:

● in the operation stove, boiler tube in parallel is most commonly used to process-liquid, to avoid excessive boiler tube diameter and economic stove design is provided.Therefore the incoming flow thigh need be diverted in the boiler tube in parallel of this stove upstream.

● in modern treatment plant, often use series of heat exchanger in parallel, as serial housing and tubular heat exchanger.This is for fear of excessive tube bank diameter and/or the heat integration in the optimization process factory.

● because the restriction of bundle size, and since under the excessive situation of input set length of tube fluid to the bad distribution of air cooling organ pipe in parallel, the air-cooler bundle is the most standing be changed in parallel.

● chemical reactor such as dropping liquid bed bioreactor can be set to parallel-connection structure.In high-voltage applications, the diameter that can be provided with like this to reduce reactor also reduces the total reactor cost thus.Need increase in the reconstruction of more catalyst volume in existing factory in treatment plant, in parallel with existing chemical reactor but not in series increase new chemical reactor, often be very attractive from the economic point of view.Reason is that if in series increase new reactor with existing chemical reactor, then the total reactor pressure drop significantly increases.This needing can to cause the replacement/renewal of the costliness of pump and/or compressor.On the other hand, increase, then can actually reduce pressure drop, thereby, also can make the yielding capacity of factory higher even use identical pump and compressor if new reactor is in parallel.

History shows that the effort of shunting two-phase flow can not produce the output stream of identical vapour-liquid ratio under many circumstances.The example that has the result of different vapour-liquid ratios in the output stream has:

For stove:

Because vapor phase has lower thermal capacitance for liquid, thereby the boiler tube that obtains high vapour-liquid ratio stream strand is warmmer than the boiler tube that obtains low vapour-liquid ratio stream strand.Even therefore be lower than the rated heat input, rated heat load of stove, also can reach maximum and allow the pipe metal temperature.Stove can not transmit it thus and is designed the heat that transmits at first.The possibility of result is the lower productivity from processing unit.In the hydrocarbon operation, the pipe metal temperature of heat causes the charcoal formation rate on the tube wall to increase.The possibility of result is to make too early the shutting down in unit because of boiler tube needs decoking.At last, if steam and liquid are distributed to each boiler tube in parallel by the automatic control system as flow control valve and so on, if control system is failed, one or more boiler tubes may just no longer obtain any liquid suddenly and supply with so.The result can cause the overheated of boiler tube and break.

For heat exchanger and air-cooler:

For the heat exchanger and the air-cooler of parallel connection, the overall thermal performance significantly reduces under the situation that vapour-liquid ratio does not wait.Particularly between hot and cold stream, have in the special applications of the close temperature difference.For example, if heat transfer system comprises the heat exchanger A and the B of two parallel connections, heat exchanger A obtains the stream thigh of high vapour-liquid ratio, and heat exchanger B obtains the stream thigh of low vapour-liquid ratio.Because of the stream thigh thermal capacitance among the heat exchanger A is lower, the driving Δ T among the heat exchanger A is lower.Transmission heat load among the heat exchanger A is therefore lower.In heat exchanger B, higher because of stream thigh thermal capacitance wherein, it is higher that it drives Δ T.Transmission heat load among the heat exchanger B is therefore higher.Yet, the still high low heat transfer that compensates inadequately among the heat exchanger A that gets of the heat transmission that increases among the heat exchanger B.General effect is that the total amount of heat of transmitting in these exchangers significantly reduces.The possibility of result that is lower than the heat transmission of expectation in the exchanger is that the productivity of processing unit is lower, and this has serious economic consequences.

In some situation, liquid also may cause fouling, obstruction and/or corrosion to the inequality distribution of exchanger in parallel.An example is the heat exchanger with parallel connection of vaporizing liquid.Usually, treatment plant is designed to avoid exchanger inside to vaporize fully.In other words, avoid by " doing ".Reason is always to have unvaporized pollutant in process stream thigh.If certain position of " doing " in exchanger produces, these pollutants can be deposited on to conduct heat passs the surface, and this is because they dissolved originally or the liquid that is dispersed in has wherein disappeared now.Although it is in plant design, do not predict, existing if a liquid that significantly is less than desired value in the exchanger in parallel then does may be created in this exchanger.Its possibility of result is pollution and/or a blockage problem serious in the exchanger, follows the heating rate and the unit is stopped with the cleaning exchanger of passing at the low.

Another example is the product air-cooler bundle in the hydrotreatment unit.When reactor effluent is cooled, NH ₄Cl and NH ₄The ammonia salt of HS and so on will precipitate and may cause serious corrosion and blockage problem.Therefore add rinse water to dissolve these salt.Yet history shows, the process stream stock that will comprise rinse water flows to that air-cooler bundle in parallel has caused the bad distribution of rinse water and in the intrafascicular corrosion and the blockage problem that obtain seldom or do not obtain rinse water.

For chemical reactor:

For the chemical reactor of the parallel connection of dropping liquid bed bioreactor and so in the hydrotreatment unit, it is most important to obtain identical vapour-liquid ratio in the inlet of each reactor.In the hydroprocessing reactor, as hydrocracking or hydrotreating reactor, wherein, hydrocarbon components under the solid catalyst effect with H-H reaction, the low vapour-liquid ratio that offers reactor will cause hydrogen dividing potential drop lower in the reactor, and this also will cause lower reactive rate, high carbon build-up speed and catalysqt deactivation.Even offer the very short expensive loads that also can cause badly damaged catalyst reactor particle of the operating time of the too low vapour-liquid ratio of reactor.

Describe in detail

Shunt of the present invention can be designed to handle the separation ratio of any needs.Separate than the total mass flow rate of the total mass flow rate that is defined as output stream divided by inlet flow.For example, the present invention both can be designed to 50%/50% shunting, also can be 5%/95% shunting.Because the two-phase flow shunt is an open system with low overall presure drop without any control valve, therefore be that the hydraulic pressure capacity of downstream streaming system but not two-phase flow shunt itself have been set and separated ratio.Correct when designing, even split ratio has departed from the design split ratio of two-phase flow shunt, shunt can guarantee that also the vapour-liquid ratio in each output stream is approaching identical.At this its reason is described:

Suppose that shunt has been designed to separate than 30%/70% the two-phase inlet flow be split into two output streams for suction passage A respectively with B.This design will cause varying in size of two suction passage mesopores different with the cross-section area of two suction passages usually.In some operator scheme, separate can be 40%/60% now than also, but not the design load 30%/70% of two-phase flow shunt.In this case, cross the hole of suction passage A side than the more vapor stream of original expectation.It is big that therefore the pressure drop of suction passage A from the outside to the inboard become.The more liquid of result raises and enters this suction passage.Owing to the low split ratio of suction passage B, cross the hole of suction passage B side than the less vapor stream of original expectation.Therefore the pressure drop of suction passage B from the outside to the inboard diminish.The less liquid of result raises and enters this suction road.By this way, this design is tending towards compensating for different split ratios.

If the split ratio of given suction passage is higher than predicted value under certain operational modes, so higher gas flow will cause higher fluid flow.Similarly, if the split ratio of given suction passage is lower than predicted value, so lower gas flow will cause lower fluid flow.The result is the influence of the split ratio that only changed on low degree very of the vapour-liquid ratio in the output pipeline.

Fig. 4 has provided shunt can keep first example of identical vapour-liquid ratio in output stream, it has shown the process flow diagram of the processing system with heat exchanger, metering device and boiler tube in parallel.Cold two-phase incoming flow 50 need be by heating with use stove 61 with hot-fluid 58 and 65 heat exchanges.The cold flow 50 at first shunt 51 of the application of the invention splits into three stream thighs 52,53 and 54.Output stream 52 flows through the series A of the tube side 67 of the shell wall, pipeline thermal exchanger 55a, 55b, 55c, 55d and the stove 61 that comprise housing.Output stream 53 flows through the serial B of the tube side 68 of the shell wall, pipeline thermal exchanger 56a, 56b, 56c, 56d and the stove 61 that comprise housing.Output stream 54 flows through the serial C of the tube wall, pipeline thermal exchanger 57a, 57b, 57c and the control valve 69 that comprise housing.Merge into product stream 64 from the output stream 62,63 and 60 of series A, B and C respectively.The design vapour-liquid flow rate of shunt 51 and character are table 1 illustrate.

Table 1: the design flow rate and the character of the steam of shunt 51 and liquid among Fig. 4

	The design situation
		Steam flow, cubic meter/hour	1400
Vapor density, kilograms per cubic meter	9.5
		Steam viscosity, centipoise	0.018
Fluid flow, cubic meter/hour	260
		Fluid density, kilograms per cubic meter	765
Fluid viscosity, centipoise	0.36

Surface tension of liquid, dynes per centimeter

14.7

Shunt 51 is designed to be respectively 40%/40%/20% for series A, B and C split ratio.Be intended to make each output stream 52,53,54 to have identical vapour-liquid ratio.When actual split ratio with the design split ratio 40%/40%/20% identical, the vapour-liquid ratio of three output streams 52,53,54 will be near identical.Yet the pressure drop that proves given flow rate is higher than 20% of predicted value for series A.Not being both of flow resistance because the different layout of beam line of the series A of two parallel connections and B and slightly different exchanger and stove design.The pressure drop that also proves given flow rate is lower than 30% of former predicted value for serial C.The mobilization force of series C is low to be because the traffic demand of control valve 69 controls is higher.Because the flow resistance difference of running system in parallel, split ratio is different with expectation.

Now, the difference of vapour-liquid ratio is estimated as 9 cover vapour-liquid ratios in each series in parallel that is caused by the flow resistance of series A that is different from expection and C.These a few cover vapour-liquid ratios and the result that estimate provide at table 2.Steam and fluid flow correspond respectively to 50%, 100% and 200% of steam and liquid design discharge.Results estimated as the Δ P of the Δ P of shunt, three series, the vapour-liquid volume ratio and the %DVLR of stream thigh 52,53 and 54, also provides at table 2.%DVLR is defined as:

VL wherein _iAnd VL _FeedBe respectively the volume vapour-liquid ratio of output stream i and input incoming flow, Nsplit is the number from the shunt output stream.

As shown in table 2, be different from original design even work as the flow resistance of downstream system, given diverter designs also demonstrates superior performance in very big vapour-liquid ratio scope.

Vapour-liquid ratio changes to 21.5 from 1.3, and the pressure drop of series changes to 20.9 crust from 1.3 crust.By series A exceed 20% flow resistance and serial B to hang down the average %DVLR that 30% flow resistance causes low to 2.97%.

Table 2: performance with shunt 51 of the down-stream system flow resistance that is different from expection

Mechanical tolerance influence when the shunt performance is subjected to shunt manufacturing and installation.Especially the flow area of the relative height of suction passage and suction passage mesopore can influence its performance.

Second example of the application of shunt of the present invention is presented in the process flow diagram of Fig. 5.The existing dropping liquid bed bioreactor 75 that has loaded 190 cubic metres of catalyst granules is too little, so that can not produce the product that needs with the speed of needs.Therefore need increase by 90 cubic metres of catalyst volumes again.Not that series connection increases new catalyst volume on existing reactor, but on existing reactor 75, be installed in parallel new reactor 74.Shunt 71 of the present invention is used to two-phase incoming flow 70 is split into two output streams 72 and 73 that offer reactor 75 and 74 respectively.Reactor 74 and 75 split ratio are respectively 32%/68%.In reactor downstream, come the output stream 76 of autoreactor 74 and output stream 77 merging that come autoreactor 75 to become product stream 78.Suction passage in the shunt 71 former being decided to be is in equal height, but in this example, improved 10mm corresponding to the suction passage A of stream strands 72 than the suction passage B corresponding to stream strands 73.And the flow area of suction passage A mesopore has increased 2% than originally, and the flow area of suction passage B mesopore is than originally having reduced 2%.The difference of the height difference of suction passage and the flow area in hole all will increase stream burst 72 vapour-liquid ratios with respect to stream thigh 73.

Shunt 71 is designed to steam and the liquid flow rate and the character of table 3.

Table 3: the design flow rate and the character of the steam of shunt and liquid among Fig. 5

	The design situation
		Steam flow, cubic meter/hour	1170
Vapor density, kilograms per cubic meter	27.0
		Steam viscosity, centipoise	0.022
Fluid flow, cubic meter/hour	421
		Fluid density, kilograms per cubic meter	566

Fluid viscosity, centipoise	0.0115
		Surface tension of liquid, dynes per centimeter	4.5

Now the operational condition of vast scope is assessed the vapour-liquid ratio %DVLR of equation (2) definition that causes by above-mentioned manufacturing and location tolerance.The assessment operational condition provide at table 4, and correspond respectively to steam and liquid the design flow rate 50%, 100% and 200%.Results estimated, Δ P, the Δ P of reactor, the vapour-liquid volume ratio and the %DVLR of stream thigh 72 and 73 as shunt also provide at table 4.

Table 4: the shunt performance of the manufacturing of worst condition and location tolerance.

As shown in table 4, even if having the manufacturing and the location tolerance of poor situation, also obtaining superior shunting performance under steam and the liquid flow rate on a large scale.

For two examples of Fig. 4 and Fig. 5, shunt is designed to produce the output stream with identical vapour-liquid ratio.Described shunt also can be designed to produce the output stream of different vapour-liquid ratios.For example, shunt can be designed as the two-phase inlet flow is split into three output streams with split ratio 20%/20%/60% and vapour-liquid volume ratio 10/12/20.In the commercial Application of most of two-phase flow shunts, but be to be desirably in identical vapour-liquid ratio is arranged in the output stream.

In the separator of the present invention, separating of steam and liquid is unnecessary good as traditional phase separator.Most of liquid separates with steam and gets final product.Also because of the mean allocation of steam, the less drop that passes through jointly with steam will be assigned to suction passage.Therefore the separator of two-phase flow shunt can be designed to linear steam rate and therefore the littler cross-section area higher than traditional phase separator.And it is obviously lower that the liquid holdup time that needs is compared to the conventional separators with metering device shown in the image pattern 2 for the separator of two-phase flow shunt.Its liquid holdup time of conventional separators with metering device is 5-20 minute, has reserved the response time of tank level control system and has allowed the operator to take manual action under the situation that automatic control system lost efficacy.For the two-phase flow shunt, liquid level is more or less by fixing and mainly definite by the steam useful load immediately.Therefore the liquid holdup time in the separator of two-phase flow shunt can hang down by 5 seconds.Total result is, the traditional phase separator that uses in the separator of two-phase flow shunt and the treatment plant is compared very compact.As an example, size and the cost that is designed to the pressurized container of the size of pressurized container of the shunt 51 among Fig. 4 of vapour-liquid ratio in the table 1 and character and the traditional phase separator among cost and Fig. 2 compared.The tradition phase separator also is designed to steam and fluid flow and the character in the table 1.The result provides at table 5.

Table 5: the pressurized container size of described shunt and conventional separators and cost are relatively

	Shunt among Fig. 4	The tradition phase separator
			Inside diameter of vessel, millimeter	800	2750
The tangent length of container, millimeter	1830	9700
			Design pressure, crust	80	80
Design temperature, degree centigrade	230	230
			Constituent material	Carbon steel	Carbon steel
The estimating apparatus cost, dollar (2003)	21,600	374,000

The cost that table 5 provides is the cost that container adds the internals in suction road and so on.The installation cost not included that comprises foundation, assembling, isolation, pipeline and metering device etc.The 3-4 that total installation cost typically is the equipment cost that table 5 provides doubly.As seen from Table 5, with respect to using traditional phase separator, shunt of the present invention provides a kind of compactness and cheap selection.

Fig. 3 A, 3B, 3C, 6A, 6B, 6C, 7A, 7B and 8 provide the optional structure of shunt of the present invention.Provide these figure just for illustration the present invention and alternative.They also are not intended to be limited in the scope of this disclosed principle or as construction drawing.These figure can not be considered to the restriction to the inventive concept scope.The relative dimensions that accompanying drawing shows should not thought and equals or be proportional to commercial embodiment.

Referring now to embodiments of the invention, accompanying drawing.Shunt 30 shown in Fig. 3 A, 3B and the 3C is the shunts that are used for inlet flow two output streams 42 of 41 fens profit retentions and 43.Shunt 30 comprises the container 31 with a supplying tube 32 and two output tubes 44 and 45.Supplying tube 32 is connected to the wall of container 31, to form fluid-tight.The lower end of pipe 32 is open, enters container 31 to allow inlet flow 42.One striking plate 33 with sidewall 40 is arranged below supplying tube 32.Striking plate 33 and sidewall 40 constitute a mobile passage, earlier inlet flow 41 are divided into two streams, again with the cylindrical wall of these two conductances to container 31.Two vertical in essence suction passages 34 and 35 are positioned at container 31.Each suction passage comprises that one has the pipe of open top and bottom.Fall into oblivion in liquid 39 lower end of suction passage.The upper end of suction passage 34 or outlet are connected to output pipeline 44, and the upper end of suction passage 35 or outlet are connected to output pipeline 45, leave two runners of container 31 with formation.Between the wall of container 31 and output pipeline 44 and 45, form fluid-tight.Have hole 37 on the pipe side wall of suction passage 34, have hole 36 on the pipe side wall of suction passage 35.

In operating process, two-phase inlet flow 41 enters container 31 by pipeline 32 now.Two-phase impinging jet striking plate 33, this can destroy the high flow rate of this stream thigh and will flow strand cylindrical wall of guiding container 31.In container 31, liquid phase 39 is separated with vapour phase 38.Described liquid phase converges the zone in the heavy phase of container bottom and converges, and vapour phase then converges in the zone of gently converging mutually on container top.Steam 38 flows through hole 36 and 37 parts on the suction passage wall on the liquid level now.By the mobile pressure drop that can produce from the suction passage outside to suction passage inside in hole, thereby the liquid rising enters suction passage.Liquid 39 flows through the open end, bottom of suction passage 34 and 35 and passes through subsurface hole 36 and 37 parts in the container 31.Described liquid mixes in suction passage with described steam, biphasic mixture in suction passage on flow to its outlet and by output pipeline 44 and 45 flow containers 31.

Feed entrance preferably is symmetrically located between the suction passage, as shown in Figure 3A.This container cross section that will be used in vapour/liquid separation needs is actively little, and this also will distribute by the droplet of steam path more equably.Shunt is preferably designed as charging inlet flow thigh bump or striking plate and wall shown in Fig. 3 B and 3C.When input incoming flow thigh crash panel and wall, liquid is tending towards separating from vapour phase, and prevents the high speed input jet from arriving the liquid level in the container and may cause liquid reentrainment and fluctuation.

Select the tank fill level of the gross area need to obtain in hole on the suction passage.Bigger hole area causes lower steam drop and causes higher liquid level thus, and the vertical height that consequently lower pressure drop and liquid need promote is complementary.On the contrary, less area causes lower liquid level.The hole area of each suction passage can be used for setting the vapour-liquid ratio of suction passage output stream.If the hole area of suction passage A increases with respect to the hole area of another suction passage B, the vapour-liquid ratio of the relative suction passage B of the vapour-liquid ratio of the output stream of suction passage A increases so.The cross-section area of each suction passage and shape also influence the vapour-liquid ratio of tank fill level and each output stream thigh.

The hole in the suction road shown in Fig. 3 A is the circle hole.But these holes also can be vertical trench or have other shapes, as V-arrangement, triangle, rectangle, polygonal, ellipse etc.The area in hole needn't evenly distribute on the whole height of suction passage.For example, suction passage can have less hole area near the bottom, and has bigger hole area near the top.

Suction passage shown in Fig. 3 A and the 3B has circular cross section, but suction passage also can have a lot of other shape of cross sections, as triangle, rectangle, ellipse, polygonal etc.The cross section of suction passage also can be along the length change of suction passage.

The bottom of the suction passage shown in Fig. 3 A is open to flow of fluid.But under many circumstances, if the bottom lock of described suction passage, the hole of all liq so the subsurface suction passage side of need flowing through, the shunting performance that then can be improved.

The suction passage of the shunt shown in Fig. 3 A and the 3B is vertical.But suction passage does not need fully vertically.Need only suction passage and have vertical part, perhaps in other words, the process steam that upwards flows enters the hole as long as liquid is inhaled into the passage constraint, and it is just enough to import one of output pipeline 44 and 45 to arrive the suction passage outlet then.

The container 31 of the shunt among Fig. 3 A, 3B and the 3C is the horizontal cylinder container with oval head.But this separator of the present invention or container can have Any shape and direction.Other examples of container shapes and direction are vertical cylindrical chamber, spherical container, have the case type container of rectangular cross section etc.

Among Fig. 4, input and output stream is by the turnover of container 31 upper walls.But input and output stream can be by other wall turnover as base wall and sidewall.

With reference to the shunt shown in Fig. 6 A, 6B and the 6C variation of the present invention is described.Shunt 80 comprises vertical cylindrical chamber 81.This shunt has inlet flow 88 and enters by the pipeline 87 that runs through container 81 sidewalls.Vertical manger board 86 is positioned at this inlet downstream.This shunt has three output streams 91,92 and 85.Output stream 91 flows out by the output pipeline 99 that runs through container 31 upper walls.Output pipeline 99 is connected to suction passage 82 in fat leakage mode.Suction passage 82 has circular cross section and for convergent, so that the cross-section area of passage dwindles downwards.Suction passage 82 is provided with four vertical grooves 94.Suction passage 82 is open in the bottom for flow of fluid.Output stream 92 flows out by the output pipeline 98 that runs through container 31 sidewalls.Output pipeline 98 uses 90 ° of bend pipes 97 to be connected to suction passage 83 with leak-proof manner.Suction passage 83 has square cross section.Suction passage 83 is provided with four vee-cuts 93.Suction road 83 is open in the bottom for flow of fluid.Output stream 85 flows out by the output pipeline 100 that runs through container 31 base wall.Output pipeline 100 uses 180 ° of bend pipes 96 to be connected to suction passage 84 with leak-proof manner.Suction passage 84 has circular cross section and is provided with square hole 95.Suction passage 84 is sealing in the bottom for flow of fluid, all liquid thereby must flow through square hole 95.

In operating process, two-phase inlet flow 88 enters container 81 by pipeline 87.Two-phase jet collision manger board 86 has destroyed the two-forty of stream thigh and has caused being separated of some degree.Separate from vapour phase 89 container 81 inside, liquid phase 90.Liquid phase converges at container bottom, and vapour phase converges on container top.Steam 89 flows through respectively the hole 93,94 and 95 in suction passage 83,82 and 84 sides now.Flow of steam by the hole causes the pressure drop from the suction passage outside to suction passage inside, so liquid is raised and enters suction passage.Liquid 90 flows through the open end, bottom of suction passage 82 and 83, and flows through the part of container 81 subsurface holes 93,94 and 95.Liquid is in suction passage and vapor mixing, and biphasic mixture is in the suction passage internal flow and by output pipeline 98,99 and 100 flow containers 81.

The shunting performance of the present invention that is quantified as the %DVLR of equation (2) definition reduces in high vapour-liquid ratio is used.In high vapour-liquid ratio was used, performance of the present invention can be by significantly improving with the pressure drop of the two-phase flow of increase suction passage inside at the inner insert that uses of suction passage.Using one or more orifice plates in suction passage is this examples that are used to increase pressure drop and improve the insert of shunting performance.In addition, in suction passage, use insert that the two-phase flow pattern in the suction passage is had certain influence.For example, use orifice plate to help to eliminate the slug flow that unwanted liquid rod (liquid slugs) and steam pocket (vapor pockets) flow periodically in suction passage.Greatest improvement by using the suction passage insert to the shunting performance obtains in high vapour-liquid ratio is used, but has also obtained certain improvement for the application of low vapour-liquid ratio.The shunt 51 and 71 that for example comes from Fig. 4 and Fig. 5 has respectively just comprised insert in order to improve the shunting performance in suction passage.

Shunt 30,51,71 and 80 among Fig. 3 A, 3B, 3C, 4,5,6A, 6B and the 6C all has separator or the container of himself.The constituent element of other processing equipment of housing and pipeline thermal exchanger and chemical reactor and so on uses but the present invention for example also can be used as.

Fig. 7 A and 7B show an example as the shunt of the present invention of the constituent element of chemical dropping liquid bed bioreactor 110.Fig. 7 A shows the bottom of this dropping liquid bed bioreactor.Catalyst granules 103 is packed into and is had the cylindrical compression shell 101 of hemispherical head 102.Catalyzer supports graticule mesh by catalyzer or screen cloth 104 supports.It is that catalyst granules can not pass screen cloth and steam and liquid can pass that catalyzer supports graticule mesh/screen designs.Two vertical suction passages 107 are positioned at catalyzer to be supported below graticule mesh/screen cloth.Each suction passage is provided with eight grooves 108.Suction passage also is provided with the pressure drop that insert increases suction passage.These inserts comprise four orifice plates 109,110,111,112 of each suction passage.Each suction passage 107 is connected to an output mouth of pipe 105 with leak-proof manner by the path 10 6 that use has bend pipe.

In operating process, flow through bed of catalyst particles layer 103 under gas and liquid and the flow direction and support graticule mesh/screen cloth 104 by catalyzer.It is open spaces that catalyzer supports graticule mesh/screen cloth 104 belows, and liquid phase 113 is separated with vapour phase 114 at this place.Liquid phase 113 converges at reactor bottom.Flow through now groove 108 parts of liquid level top of steam 114.Make by groove 108 mobile innerly from the suction passage outside to suction passage to produce pressure drop, so liquid is raised and enters suction passage.The perforate of orifice plate 112 bottom liquid 113 is flowed through, and by subsurface groove 108 parts.Liquid in suction passage and vapor mixing, flow through suction passage and orifice plate, and by flowing out the mouth of pipe 105 outflow reactors 110.

Fig. 8 shows the example as the shunt of the present invention of the constituent element of housing and pipeline thermal exchanger 120.Housing and pipeline thermal exchanger 120 comprise:

● have the head 122 of cover plate 128, the pipe side input mouth of pipe 129 and the pipe side output mouth of pipe 130

● have the housing 121 of the input mouth of pipe 131 and two output mouths of pipe 125

● comprise the U-shaped tube bank of U-shaped pipe 124, tube sheet 135 and 13 flow baffles 132

The length of housing 121 has increase slightly than common heat exchanger designs, thinks that the two-phase flow shunt of the present invention on the shell side wall in 180 ° of bend pipe downstreams of last stream baffle plate downstream and U-shaped pipe 124 provides holding space.This shunt comprises two basic vertical suction passages that have hole 127 on wall 126.The bottom of suction passage 127 is open, can allow flow of fluid.

In operating process, the fluid of pipe side enters exchanger by the mouth of pipe 129, in the inner process of U-shaped pipe, and by the mouth of pipe 130 outflow exchangers.The fluid of housing side enters exchanger by the mouth of pipe 131, can be single-phase or two-phase flow.Condensation or vaporization also may take place outside transmitting in heat extraction in exchanger.The fluid of housing side flows in the U-shaped tube outside.Flow baffles 132 produces some cross flow one cross section, and at this place, the fluid of housing side is forced to flow through along the direction perpendicular to pipeline.Behind last stream baffle plate, two-phase flow enters separated space, and here liquid 133 separates with steam 134.Liquid phase 133 converges in housing 121 bottoms.Flow through now hole 127 parts of liquid level top of steam 134.Flow of steam by these holes makes and inboardly from the suction passage outside to suction passage produces pressure drop, so liquid is raised and enters suction passage.Liquid 133 the flow through bottom of opening of suction passage 126 and hole 127 parts of the liquid level below of flowing through.Liquid is in suction passage and vapor mixing, and the suction passage of flowing through, and flows out exchangers 120 by the mouth of pipe 125.

In the example that Figure 4 and 5 provide, the two-phase inlet flow is divided to downstream line system and processing equipment in parallel.But the present invention also can be used on processing equipment inside, with steam and liquid mean allocation in the equipment in the passage in parallel.An example is to use the present invention in the input collector of heat exchanger or air-cooler, with steam and liquid mean allocation in the exchanger in the pipeline in parallel.

In all examples of the present invention given herein, have only a suction passage to be connected to each output pipeline of shunt.But each output stream also can use the suction passage more than.If each output stream uses the suction passage more than, the suction passage that is connected to output stream so needn't need identical.For example, be designed to that the shunt of two output streams of two-phase inlet flow shunting becoming can be had the suction passage of five different sizes altogether, three suction passages all are connected to first output stream, and remaining two suction passage is connected to second output stream.In some situation, the suction road of use different size is connected to identical output stream can make the shunting performance improve.

In all that provide application examples of the present invention, has only an inlet flow input shunt herein.But also can use the SEPARATOR OR SEAL CHAMBER that flow into shunt more than one inlet flow.Also can use the single-phase input of only carrying steam or only carrying liquid.

Except separating the two-phase liquid-vapor mixture, shunt of the present invention also can be used for immiscible liquid biphasic mixture, and as hydrocarbon liquid phase and water soluble liquid phase, shunting becomes two or more output streams, and each output stream has the oil-water ratio that needs.

Generally speaking, about the present invention, should be noted that following some:

The present invention relates to be used for and will comprise the two-phase inlet flow shunting of light phase and heavy phase or be divided into the part flow arrangement of two or more output streams, wherein each output stream has required weight and compares.This part flow arrangement comprises that one has the separation vessel or the container of one or more inlet.In container, carry out partially or completely separating of light phase and heavy phase.Container is provided with at least two hollow suction passages with lower end and open end, top.

The hole of each suction passage side is arranged at least one height between lower end and the upper end.The lower end of described suction passage is submerged in the heavy phase, and during the upper end of described suction passage is in gently mutually, and is connected to down-stream system in watertight mode by flow channel.

Suction passage must have vertical part, thereby in operation, the part of hole area rises to the top of interphase boundary horizontal plane at least.In operation, gently flow through the hole area part of interphase boundary horizontal plane top and cause pressure drop thus mutually from the suction passage outside to the inboard.Because this pressure drop, heavy phase is raised by any one open end, bottom and by the hole that any one is positioned at interphase boundary horizontal plane lower, planar and enters suction passage.In suction passage, heavy phase and gently mixing mutually.This two-phase flow is flowed through suction passage also by described flow channel arrival down-stream system.

Can use insert or throttle valve to increase pressure drop and change two-phase flowing state in the suction passage in that suction passage is inner.

Described insert can be the orifice plate with circular flow hole.

The suction passage lower end can be sealed, need the flow through hole of the suction passage side that is positioned at interphase boundary horizontal plane below of all heavy phases.

Except that the shunting purpose, these vessel or container can be the constituent elements that is used to finish other other processing equipment of purpose of chemical reaction or heat exchange and so on.

Described down-stream system can be and the flow channel that is in the parallel connection of same section with shunt as the equipment of its constituent element.

Described down-stream system can be the processing system that comprises pipeline, instrument and equipment.

Described suction passage can have circular cross section.

The hole of suction passage side can be circle hole or rectangle groove.

Vertically highly being preferably in 100mm and the 1500mm of hole from the suction passage bottom to maximum height.

In at least one serviceability, sliding (no-slip) two-phase flow speed of the nothing of suction passage upper end is preferably between 0.5m/s and the 15m/s.

One or more suction passage can be connected to each down-stream system.

Described device can be advantageously used in the two-phase vapor/liquid mixture is diverted to heat exchanger in parallel.

Described device can be advantageously used in the two-phase vapor/liquid mixture is diverted to boiler tube in parallel.

Described device can be advantageously used in the two-phase vapor/liquid mixture is diverted to chemical reactor in parallel.

Described device can be advantageously used in the two-phase vapor/liquid mixture is diverted to air-cooler in parallel.

Described device can be advantageously used in the heat exchange duct or the passage of the parallel connection in two-phase heat exchanger or the air-cooler of steam and liquid distribution.

Claims (21)

1, a kind of two-phase inlet flow that one or more is comprised light phase fluid and heavy phase fluid of being used for splits into two or more output streams, and each output stream has the required light part flow arrangement of the ratio of heavy phase relatively, and this device comprises:

Be separated vessel or container, it comprises: one or more is used for inlet flow inlet of described inlet flow, and heavy phase converges the zone, with converge in described heavy phase the zone more the high position gently converge the zone mutually, described inlet flow inlet is positioned at and gently converges the zone mutually; With

Two or more suction passages or pipeline, at least one is used for each described output stream, each suction passage or pipeline comprise: converge at least one heavy liquid inlet that the zone communicates with described heavy phase, with described gently converge mutually the zone communicate and be positioned at than described at least one heavy liquid inlet more at least one of high position gently inlet and at least one output stream of being used for communicating with the output stream flow duct in device downstream export mutually; Described at least one gently enter the mouth mutually between described at least one heavy liquid inlet and the outlet of described at least one output stream.

2, according to the device of claim 1, wherein, intake line comprises wall defined an elongated pipe member that is provided with one or more hole by top, and described pipe member is the pipeline with circle or rectangular cross section.

3, according to the device of claim 2, wherein, the lower end of described pipe member is open.

4, according to the device of claim 2, wherein, the shape in described one or more hole is to comprise circle, ellipse, avette, rectangle and the leg-of-mutton shape from one group selecting.

5, according to the device of claim 1, wherein, light inlet mutually and heavy liquid inlet have the single hole that significantly vertically extends by one and constitute, or are a groove along described intake line longitudinal extension.

6, according to the device of claim 5, wherein, the width of described groove increases along the direction to described output stream outlet.

7, according to the device of claim 5, wherein, the width of described groove is actually constant.

8, according to the device of claim 1, wherein, current-limiting apparatus is set to increase the described light pressure drop of inlet mutually at described suction passage or pipe interior.

9, want 8 device according to right, wherein, described current-limiting apparatus comprises a baffle plate, has one or more hole on it, thereby the flow restriction that makes intake line is to described one or more hole.

10, according to the device of claim 1, wherein, be provided with the impact flow device so that described inlet flow impacts described impact flow device near described inlet flow ingress.

11, according to the device of claim 1, wherein, the vertical distance between the highest part of the lowermost portion of described one or more heavy liquid inlet and described one or more light inlet mutually is at least near 100mm, is at most near 1500mm.

12, implement the physical or chemical treatment device therefor, utilize two-phase flow and according to the treatment device of the part flow arrangement of any one in the claim 1 to 10 a kind of comprising, the inlet of described part flow arrangement and described equipment or export is communicated with.

13, according to the device of claim 12, wherein, described equipment comprises a stove, and this stove comprises the boiler tube that a cover is connected with described output stream outlet.

14, according to the device of claim 12, wherein, described equipment comprises the heat exchanger of the parallel connection that is connected with described output stream outlet.

15, according to the device of claim 12, wherein, described equipment comprises the chemical reactor of the parallel connection that is connected with described output stream outlet.

16, according to the device of claim 12, wherein, described equipment comprises the air-cooler of the parallel connection that is connected with described output stream outlet.

17, a kind of biphasic reaction device, it comprises according to any one part flow arrangement in the claim 1 to 10.

18, according to the reactor of claim 17, it comprises an external casing, and wherein, described phase separation container is positioned at described external casing inside.

19, a kind of heat exchanger comprises according to any one part flow arrangement in the claim 1 to 10.

20, according to the heat exchanger of claim 19, it comprises an external casing, and wherein, described phase separation container is positioned at described external casing inside.

21, a kind ofly adopt part flow arrangement as claimed in claim 1 that one or more is comprised the two-phase inlet flow of light phase fluid and heavy phase fluid, split into two or more output streams, and each output stream has the required light method of the ratio of heavy phase relatively, and this method comprises the steps:

At least in part inlet flow is separated into the heavy phase part in the heavy phase zone that is positioned at interphase boundary face below and the light part mutually of the light alpha region that is positioned at interphase boundary face top;

Two places in described light alpha region or many places more will be mixed with light phase fluid from described light part mutually from the heavy phase fluid of described heavy phase part, have the two-phase output stream of the ratio of required light relative heavy phase respectively to form described two or more.

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