ES2315667T3 - DEVICE FOR THE SEPARATION OF A TWO-PHASE INPUT CURRENT WITH THE DESIRED VAPOR / LIQUID RELATIONSHIP. - Google Patents

Abstract

The invention is a device (30) for splitting a two-phase inlet stream (41) into two or more outlet streams (42, 43). The device can be designed to maintain close to identical vapor to liquid ratio in each of the outlet streams. The inlet stream to the device is routed via an inlet pipe (32) to a separator vessel (31). Below the inlet pipe entrance in the vessel an impingement plate (33) is provided to break down the high velocity of the stream and to direct the stream towards the inner walls of the separator where liquid will impinge and separate from the vapor phase. In the separator vessel, separation of the liquid and vapor phases is achieved. Inside the separator two vertical suction channels (34, 35) are located. These suction channels are in fluid communication with the two outlet pipes (44, 45) through which the outlet streams are leaving the separator. The lower ends of the suction channels are submerged in the liquid phase (39). The suction channels are provided with apertures (36) in the side walls. Vapor is flowing though the fraction of the apertures that are above the liquid surface in the separator. When vapor is flowing through these apertures a pressure drop across the wall of the suction channel is generated. Consequently liquid is lifted up into the suction channel. The liquid is mixed with the vapor inside the suction channel and the two-phase mixture is flowing upwards through the channel and is leaving the separator and two-phase stream splitter through the outlet pipes.

Description

Device for separating a current Two-phase input with the desired vapor / liquid ratio.

Background of the invention Field of the Invention

The invention relates to a device for the separation of a two phase input current consisting of a light phase fluid and a heavy phase fluid, for example vapor and liquid, in two or more two-phase output streams. He device will ensure that the vapor / liquid ratio is obtained desired for each of the output currents. Flow rates totals of each output current do not necessarily need to be identical The invention is appropriate but not limited to the application of the separation of a process stream of two phases flowing in a pipe or channel in heat exchangers In parallel, boiler pipes, refrigeration equipment, chemical reactors or piping systems.

Related technique

In many process units the separation of a two phase current and historically they have used different types of solutions ranging from the use of symmetrical dividers for pipes or Ts more Sophisticated for two phase current separators.

The separation devices of a flow of Two phases can be divided into 6 general types:

Kind one

Symmetric pipe splitters that use Ts for pipes standards

The traditional way of separating a two-phase current is to build symmetric dividers to pipes using Ts standards for pipes and rely on phases to distribute evenly to each pipe branch. A example of a symmetrical pipe splitter for the separation of a two phase current in four output currents is shown in the isometric drawing of figure 1. The current of Two-phase inlet flows through inlet pipe 1.

Pipe 1 conducts the two-phase current towards the first T 3 where the current is divided into two currents output In the example shown, if you place an elbow 2 of 90º waters above T 3. Due to the centrifugal forces acting on the liquid, the liquid tends to flow near the radius wall greater than the elbow while steam tends to flow near the wall of the minor radius. In this way, an elbow causes the separation of phases and an uneven distribution of steam and liquid to through the cross section of the pipe. To minimize the negative effect on separation performance in T 3 caused by elbow 2 upstream, preferably pipe 1 will be perpendicular to the plane defined by elbow 3 as it is sample. In addition, each of the T 3 output currents is Divide into two output currents in Ts 5a and 5b. Upstream from T 5a there is an elbow 4a and upstream from T 5b there is an elbow 4b. Again in order to minimize the negative effect on the separation performance in Ts 5a and 5b caused by the phase separation at elbows 4a and 4b upstream, pipe 7 It is perpendicular to the two planes defined by Ts 5a and 5b. Thus, through the use of symmetrical pipe splitters the input current in pipe 1 has been divided into four product streams flowing through pipes 6a, 6b, 6c and 6d

Probably the symmetric pipe splitter it is the most widely used method to divide a current Two phase input into two or more output currents. Without However, history has shown that this principle has failed in the uniform distribution of liquid and steam in streams of outlet leading in many cases to a steam ratio to uneven liquid in the outflows. A very problem important with the symmetric pipe splitter in Ts standards for pipes is that the performance of the current splitter it depends on the flow regime in the upstream pipe and that does not it is always possible to remain within the dispersed flow regime desired in all relevant operating conditions. He dispersed flow rate is a flow rate within a channel or flow pipe with a uniform distribution of small drops of liquid in a phase of continuous steam or small bubbles steam in a continuous liquid phase (Bubble Flow). He too symmetric pipe splitter performance may depend on the presence of pipe fittings upstream of the splitter already mentioned. A very important limitation of the symmetric divisor of pipes is that the flow of the output streams should be almost identical to avoid significant differences in the relationship Liquid vapor from the streams. Another limitation is that the two-phase current can only be divided symmetrically into 2, 4, 8, 16, ... etc, output currents. Therefore it is not possible to prepare 3, 5, 6, 7, 9 ... etc, output currents.

The performance of the symmetric pipe splitter In Ts standards for pipes it has been suggested to improve by injecting chemicals to reduce the surface tension of the liquid upstream of the divider. When the surface tension is reduced of the liquid, the dispersed flow regimes will be achieved at lower flow rates. Therefore, a acceptable performance of the symmetric pipe splitter over a wider range of steam and liquid flow rates. In the US patent 5,190,105 gives an example where a water surfactant is injected above the divider of a two-phase stream of saturated steam and water to a plurality of injection wells to ensure a identical quality (vapor fraction) to each injection well and to improve oil recovery from the oil tank.

Kind 2

Use of special internal elements such as diffusers, deflectors or static mixers in Ts of pipelines

Various attempts have been made to improve splitter performance of a standard T pipe using internal pipe elements such as diffusers, baffles and static mixers.

A first example is given in US Pat. 4,396,063 where a static mixer is located just upstream of a T consisting of a branched Y-shaped duct. To get a good separation performance when the relationship vapor to liquid of each output stream is identical, it is preferable dispersed flow. In the dispersed flow regime, the Two phase mixing will act more or less like a single fluid phase. Small drops of liquid tend to follow the flow of steam at approximately the same speed or vice versa. For the therefore, in the dispersed flow regime a good result is often achieved separation performance in a pipe T. the use of a static mixer upstream of the T provides surfaces with a certain projected area perpendicular to the direction of the flow in the inlet pipe. The liquid will collide in these surfaces and in this way will separate from the vapor phase. For the Therefore, the use of static mixers alters the flow rate desired dispersed, if present, and leads to separation not desired liquid and vapor. The use of mixers static adds an additional pressure drop in the system process that may represent an added process cost due to the increased energy consumption in pumps and / or compressors. The static mixers are also susceptible to form inlays caused by contaminants such as corrosion and scale products.

A second example is shown in US Patent 4,824,614. This flow separator also includes a static mixer 22 located in the inlet pipe upstream of a T 14 where the inlet stream 30 is divided into two outlet streams 74 and 76. Between the static mixer 22 and the T 14 is located a horizontal stratifier 24. The stratifier collects fluids of six different levels. The fluids collected in the lowest level and first are sent to the output current 76, the fluids collected in the second level are sent to the output current 74, the fluids collected in the third level are sent to the output current 76 , etc. In the same undesirable way as for the mixer of the first example, the mixer of the present invention will tend to separate the liquid from the steam. The static mixer can also increase operating costs and be susceptible to scale. The stratifier that collects the fluids will work only if steam and liquid are evenly distributed across the cross section of the pipe that will not be the case in real applications. The mixer / stratifier assembly was tested in an application in the steam / water field described in US Patent 5,810,032. The result of the test was that it was obtained
a better division of steam and water in a standard impact T than with the mixer / stratifier assembly.

A third example is given in US Pat. 5,810,032. Different types of internal elements were tested for a standard T pipe both in the laboratory with air and water as in the field of separation of a vapor / water mixture to parallel injection wells to improve oil recovery In an oil tank. Three general types of internal elements: a static mixer upstream of a T standard, a vertical flow deflector upstream of a T standard and the use of flow restrictions or nozzles on both output branches of a standard T. Were also investigated combinations of these three types of internal elements. The conclusion was that the static mixer and the vertical baffle they only lead to a marginal improvement in the performance of the divisor. Be claims the use of flow restrictions or nozzles in the two output branches to give a splitter performance something superior for the fluid regimens tested. Not however it is clear that it makes the driving force for uniform distribution of the liquid in the nozzles and branches of exit of the T in the case of an uneven distribution of liquid and vapor in the cross section of the inlet pipe. None of the essays Laboratory flow were carried out in a flow regime dispersed or bubbled (droplets of liquid in a vapor phase continuous or gas bubbles in a continuous liquid phase) the flow regimes evaluated in laboratory tests are stratified flow, stratified flow with waves, flow with predicted stagnation and annular flow using the scheme of two-phase flow of Mr. Ovid Baker ("How to design pipes of process for a two-phase flow ", Processing with hydrocarbons, October 1969, pages 105-116). This is probably the reason for how it was found that the Splitter performance of a standard T with or without separators is better at low flow rates and low liquid fractions. Preferred high speed flow rates, Flow dispersed and bubbled, not tested. If the trials had been carried out in dispersed flow and bubble regimes the conclusion would have been very likely different.

Instead of using internal elements Specials in Ts pipe standards have been suggested Ts significantly modified. In JP patents 62059397A2, US 4,528,919 and US 4,512,368 show examples of modified Ts for pipes.

Kind 3

Devices that have a specific flow rate established upstream of the divisor

The prediction of the flow regimes in industrial applications is difficult due to the loss of accuracy of flow rate schemes. Most of the flow regime schemes are primarily data based of two-phase flow regimes for air and water in a pipe Small diameter (<2 inches) (0.0508 m). Therefore for example, in a hydrocarbon / hydrogen system at high pressures and temperatures as in a hydroprocessing unit the Flow regime schemes may be inaccurate.

In addition to the uncertainty in the schemes of flow regime is also the uncertainty in the models thermodynamics in relation to the prediction of quantities and properties of liquid and vapor. This uncertainty can be significant, for example, for hydrocarbon systems complexes where hydrocarbons are characterized by the use of pseudo components and where a state equation is used to Predict the degree of vaporization and fluid properties.

Often pipe systems in plants process are also complex systems with tube fittings type extensions, contractions, elbows, check valves, etc. Each time a two-phase current passes said accessory to tubes disrupts the general flow regime and may require run long straight pipes to restore the regimen of general flow For example, as mentioned previously, an elbow tends to separate the phases with the phase heavy liquid moving near the wall of the major radius of the elbow and lighter steam moving near the radius wall lower elbow.

For these three reasons it is not normally possible accurately predict the actual flow rate in a pipe or a flow channel. Additionally, due to variations in operating conditions such as temperature, pressure, flow rate and chemical composition of the fluid is not possible normally stay in a single flow regime for all the relevant operating conditions in the unit of process. However, many separators have been designed two-phase current to work only in a single regime of flow.

A first example of said separator of Two phase current is given in US Patent 4,516,986. He separator consists of an inner pipe 12 inserted in the main pipe 10. In the annular area between the inner pipes and principal is a deflector 13. The desired flow rate in The main pipe is the annular flow regime where the liquid flows in an annular ring near the pipe wall and the steam flows at high speed through the center of the pipe. Part of the liquid flowing near the pipe wall is attempted pick up at the volume of the closed end 14. From the volume of the closed end 14, the liquid is routed through a line external 15 through a control valve 23. The steam is collects from the annular steam volume 30 downstream of the deflector 13 and it is sent through the pipe branch 11 where it is combined with the control valve liquid. A flow meter 20 is used in the two-phase current in the pipe branch 11 to Control the flow of liquid. It is not described as the meter of Flow can accurately measure the vapor / liquid ratio. With the In order to measure the vapor / liquid ratio it would normally be necessary separate measures of flow of the steam flow and the flow of liquid. For other flow regimes other than annular flow such as, for example, the flow of stagnation the performance of the Device splitter can be low. Even if the annular flow is the dominant flow regime in the main pipe 10 any pipe fittings such as elbows upstream of the separator will alter the flow. Therefore, a certain section of straight pipe upstream of the separator that It can take up additional space in the process unit. Too there may be limitations on the distribution capacity of the flow. When the total flow is reduced below the value of distribution, pressure drop is rapidly reduced through of the deflector 13 and the pressure drop available through the control valve 23. At some point, the control valve It works fully open and does not have a greater capacity to Control the flow of the liquid. By introducing instrumentation and control valves, the system is no longer as simple and robust like other two phase flow separators and it Increase the pressure drop across the separator. Generally, higher pressure drops increase the cost of operation to pump and / or compress the process unit. The patent describes how to generate two output currents. Whether require three or more output currents, then two or more Serial separators would probably be necessary. Whether require many output currents, then the system of separators will be quite complex and the necessary pressure drop It would be excessive.

In the American patent US 4,800,921 shows a second example where provides horizontal collector 16 with output branches 14a, 14b, 14c, etc. and where the upstream branch is at a high level and the level of each downstream branch is reduce successively. The idea should be that if the ring flow is the flow rate in the collector, then, the different levels of the output branches should ensure that the thickness of the annular liquid ring is approximately the same at the point of each branch of exit. In this way, it is claimed that the vapor / liquid ratio in each branch stream that almost identical As mentioned, it is difficult to predict and stay within a given flow regime for all relevant operating conditions. Also, even if you can keep an annular flow on the main line, the relationship vapor / liquid is expected to be a function of the total flow in each branch line The higher the flow in a branch line, greater steam will be sucked into the pipe and, therefore, greater It will be the ratio of vapor to liquid. If the regime of flow during certain operating modes is different than expected, for example, stratified flow, then, the result is a severe poor distribution of the phases to the branches of exit.

A third third is shown in US Patent 4,574,837 example where a certain phase distribution in a pipe Horizontal principal 10 is assumed known. Are provided openings at different levels in the main pipe to allow that the fluids flow first into an annular chamber 12 and, at then also to a branch pipe 13. The vapor / liquid ratio of the current in the bypass pipe is fixed by selecting the appropriate flow areas of the openings in the head and tail of the pipe 10, respectively. The greater the area of flow in the head of the pipe with respect to the flow area in the tail, the greater the vapor to liquid ratio achieved in the bypass pipe. The device will work only during stratified flow and stratified flow regimes with waves. Also the device it will only generate a current divided with the steam ratio a desired liquid when the level of liquid in the main pipe Be predictable. Consequently, the device will only work for small flow rates and for properties and a relationship vapor / liquid set. Most commercial applications are characterized by having high flow rates and a variation significant in the properties and in the relationship vapor / liquid

In US Patent 4,574,827 and US Patent 5,437,299 show other examples of flow separators that they have a certain flow regime established upstream of the separator.

Kind 4

Devices that use centrifugal forces

US 5,059,226 describes a two phase centrifugal flow separator. Centrifugal separator it has an inlet 28 of tangential fluid towards a chamber of turbulence 23. At the bottom of the turbulence chamber there is a central node 38 and diffusers 39 that direct steam and liquid turbulent towards the exit openings 36 and towards the channels of exit 37. It is not easy to understand what the driving force does in the distribution of the liquid phase. The fluid inlet is not symmetric since there is only one entry 28 on one side of the device. The liquid is turbulent along the wall interior of the turbulence chamber but due to the design asymmetric is not expected a uniform flow and thickness of the liquid layer / film. Consequently, some of diffusers 39 collect more liquid than others which leads to a lower than optimal liquid distribution in the channels of exit 37.

Kind 5

Devices that use an external power source to generate dispersed flow

EP 0003202 B1 shows a example of such equipment. It uses a 32 engine and a device rotational agitation on a shaft 28 to disperse the liquid mixture and steam upstream of the separator where the inflow is separates towards the output channels 4a, 4b and 4c. The device it probably works since a flow regime can be generated dispersed by adding an axis effort towards axis 28 no variations in flow rates or fluid properties. He main problem with this type of equipment is to get a good closure between shaft 28 and pipe / curve 21 which is not an easy task (not an economical design) for high applications hydrocracking pressures (up to 300 bar). Also the cost initial, the maintenance cost of the rotating equipment and the cost of the energy consumption for the engine are all high.

Kind 6

Devices that first separate steam and liquid in the stream input and then distribute each phase to streams output

A first example of a flow separator for the separation of a two-phase input current into three output streams using a vapor / liquid separator Conventional and conventional instrumentation is shown in Figure 2. A two phase input current flows through the line 11 towards a separator 10 where the liquid phase 13 separates from the steam phase 12. The steam phase is routed via the output line of steam 14 to parallel control valves 15a, 15b and 15c. The suction position or height of control valves are controls via flow controllers 16a, 16b and 16c to obtain the desired steam flow through each valve control. Flow measurements are obtained using any conventional method such as perforated plates or Venturi tubes combined with a ΔP transmitter. The drivers of flow are cascaded with a pressure controller 17. The Pressure controller is changing with the set points of flow to flow controllers 16a, 16b, 16c in order to maintain the desired pressure in the separator 10. The liquid phase 13 is directed via the liquid outlet line 18 to the valves of parallel control 19a, 19b and 19c. The position or height of aspiration of the control valves is controlled by the controllers of flow 20a, 20b and 20c to obtain the desired liquid flow rate at through each control valve. Flow measurements are obtained using any conventional method such as, for example, a perforated plate with a ΔP transmitter. The drivers of flow are cascaded with a level 21 controller. The level controller changes the flow setpoints to the flow controllers 19a, 19b and 19c in order to maintain the desired liquid level in separator 10. Finally, the steam streams of valves 15a, 15b and 15c are combined with the liquid streams of the valves 19a, 19b and 19c for generate the three output currents of two phases 22, 23 and 24.

The instrumentation for the separator of Two-phase current shown in Figure 2 is somewhat complex and a as complexity increases and the number of components such as transmitters, control valves and controllers too increases the risk of failure and loss of control. Some systems downstream can be damaged if the vapor to liquid ratio is too high or too low during said failure or loss of control in the control system. Examples are the risk of breakage of the pipe or coke formation in a boiler pipe due to the pipe overheating in the event that the ratio of vapor to liquid of the current flowing inside the pipe suddenly increase. Another example is the risk of rapid coke formation in catalytic hydroprocessing reactors in parallel if the reactor is running too low ratio of vapor to liquid resulting from a hydrogen deficiency, even in a short period of time. Also the complexity of control system and the large size of the separator vessel 10 It entails a high cost of the separator.

A second is shown in US Patent 4,293,025 example. This two phase flow separator includes a container of separation 10 having a two-phase inlet nozzle 11. A flow shock plate 14 is placed under the nozzle of input to interrupt the high speed of the current entry. Two or more chimneys 12 are provided in the separator. The upper ends open to allow steam to enter By the chimney. Openings 13 are provided in the chimneys for the entrance of liquid into the chimney. Stops are placed 16 by above the chimney openings to prevent the entry of Direct liquid in the chimney head. The flow of liquid from each chimney is determined by the overhead liquid above of the openings 13 and the flow area of the openings. For a liquid level given in the container, the flow of liquid in each chimney will be almost constant. Therefore, said separator of two phase current where the head liquid is the force motor for the distribution of liquid to the output streams Parallel will ensure a constant liquid flow in each stream output instead of a constant vapor and liquid ratio. Another problem with the current separators where the liquid from head is the driving force for distribution is a flexibility of limited liquid flow. The opening area 13 must designed to obtain an intermediate fluid level in the flow of designed liquid. If the liquid flow is said to be 50% superior during any of the operating modes, then, the liquid level should be approximately 2.25 times higher that the designed liquid level and then the liquid can overflow with chimneys and lead to poor distribution of liquid to the outlet streams. If the flow of liquid is said which is 50% lower than the designed liquid flow, then the liquid level will only be approximately 25% of the level of expected liquid At small levels of liquid, the performance of liquid distribution may be poor due to higher wave sensitivity, levelless installation and other tolerances of manufacturing. The flexibility of the liquid flow of the separator It can be expanded by providing openings at more levels. Without However, if openings are provided at more levels, then the liquid distribution performance at the designed point is reduces with respect to the separator with openings in a single level.

Other examples of separators where the level of liquid is the motor outside for even liquid distribution at each output current are given in US Patent 4,662,391; in the JP 03113251 A2; and in JP 02197768 A2.

A third example of flow separators with Liquid and vapor phase separation is shown in US Pat. 5,250,104. The two-phase mixture flowing in the pipe 14 is separates into separator 12. The vapor phase is divided into two streams at T 20. Each of the two steam streams is it passes through a hole 22 and 24. The liquid is collected in the sump 30 and is passed through the two lines of parallel liquid 32 and 34. The pressure drop of the steam flow, ΔPV, through the hole is almost proportional to the volumetric steam velocity squared. The pressure drop of liquid flow, ΔPL, through the lines of liquid 32 and 34 consists of a static term, ΔP_ {SL}, due to the difference in the unevenness of the liquid level in the sump 30 and the ends of the liquid pipe 40 and 42 and a friction term, \ DeltaP_ {FL}. \ DeltaP_ {FL} is almost proportional to the volumetric liquid flow rate squared. Market Stall that the vapor and liquid path through the separator are routes In parallel, the pressure drop must be identical:

Equation (1)

ΔP_ {V} = \ DeltaP_ {SL} + ΔP_ {FL}

The flow area of the steam holes and the Liquid pipes are designed for a given flow rate of steam QV and a certain flow rate of liquid flow QL. Now if, for example, the actual steam flow is 50% higher during some mode of operation then \ DeltaP_ {V} is 125% higher than expected. Since the flow of liquid has not changed, \ DeltaP_ {FL} doesn't change either. Therefore in order if equation (1) is completed, the \ DeltaP_ {SL} must be increased 1.25 x ΔPV. The result is that the level of liquid in sump 30 should be significantly reduced and at some point not there will be liquid level in the sump and both the steam and the liquid will enter liquid lines 32 and 34. In that case there will be a poor distribution of the liquid to parallel lines 32 and 34. On the other hand, if the steam flow is said to be 50% lower to the steam flow designed during some mode of operation, then, ΔP_ {V} will be 75% lower than expected. In this case, the level of liquid in the sump 30 will increase significantly and it will overflow the sump causing the liquid flow to holes 22 and 24 and a bad distribution. The separator it will only work properly in the steam flow and in the flow of liquid for which it was designed. The flexibility of the flow of Liquid and steam separator is insufficient for most industrial applications that are usually characterized by a significant variation in both the liquid flow rate and the steam flow and in the properties of liquid and steam such as density, viscosity and surface tension.

       \ vskip1.000000 \ baselineskip
    

Summary Description of the Invention

The invention is a device for separation of a two phase input current into two or more output currents The device can be designed to maintain close to identical the ratio of vapor to liquid in each of The output currents.

The separator of the present invention, in a embodiment, is shown in Figure 3A, 3B and 3C. The current of inlet is directed via an inlet pipe to a container of separation. Under the inlet of the inlet pipe in the vessel is provided a flow shock plate for interrupt the high speed of the current and to direct the current to the inner walls of the separator where the liquid will collide and separate from the vapor phase. In the bowl of separation, the separation of the liquid phases is achieved and steam.

Within the separator two channels of vertical suction These suction channels are in communication fluid with the two outlet pipes through which the Output currents leave the separator. The lower ends of The suction channels are submerged in the liquid phase. The suction channels are provided with openings in the walls lateral. The steam flows through the openings that are above the level of the liquid in the separator. When the steam flows through these openings a pressure drop is generated through from the wall of the suction channel. Consequently, the liquid will lifts in the suction channel. The liquid mixes with the steam inside the suction channel and the two phase mixture flows to up through the channel and out of the separator and the separator of Two phase current through the outlet pipes.

The liquid level in the separator is determined mainly because of the steam flow entering the vessel. TO low steam flows the liquid level is high and at high steam flows the liquid level is low. Liquid level It is almost never affected by the flow of liquid.

Despite the state of the art as it is described above, the invention presents each and every one of The following advantages:

TO)

He separator of the present invention can be designed to maintain almost identical the vapor to liquid ratio in the streams of exit. Alternatively, the separator can be designed to maintain specific and different vapor to liquid ratios in output currents

B)

He separator of the present invention can be designed for any separation ratio. The invention will also work if the actual separation ratio during some period of operation it is different from the separation ratio for which it was designed the separator

C)

He separator of the present invention will work equally well at all flow regimes in the inlet pipes.

D)

He separator of the present invention is not sensitive to the layout of the upstream or downstream pipe systems. For example, him performance is not modified by the presence of accessories elbow type pipes or valves upstream of the separator.

AND)

By using the separator of the present invention any number of currents of  exit. While symmetric pipe separators that use an impact T can only produce 2, 4, 8, ... etc. output currents, the present invention can also produce 3, 5, 6, 7, 9 ... etc. output currents

F)

He separator of the present invention represents a simple design and strong. It has no instrumentation or moving parts. Only need a small maintenance and non-surveillance of the operators of plant.

G)

He separator of the present invention is an open system, which is not liable to form scale. Therefore, the use of separator in a process unit will not affect the philosophy of overpressure protection. For the units of hydroprocessing, the equipment located upstream of the separator can still be protected by overpressure by means of valves security located downstream of the separator.

H)

The Separator pressure drop is small (-0.05 bar in the designed conditions) and can not find how to raise the fall of downstream systems pressure.

I)

He separator of the present invention represents an efficient design in Cost and compact.

Brief description of the figures

Figure 1 represents the state of the art and is an isometric view of a pipe system involved in a symmetric pipe separation. In the example shown of a symmetric pipe separation, the input current separates in 4 output currents using three T for pipes standard.

Figure 2 also represents the state of the technique and is a process flow sketch of a separator steam / liquid with instrumentation used to separate the input current in three output currents.

Figure 3A, 3B and 3C represents an embodiment of the present invention. Figure 3A is a sectional view. side of the embodiment taken along the line A-A Figure 3B is a sectional view. cross section taken along line B-B. The Figure 3C is an elevation view taken along the line DC.

Figure 4 is a process flow sketch which shows a first example of an application of the separator of the present invention The separator is used to separate a two-phase current in three parallel process systems that consist of heat exchangers, instrumentation and pipes of boilers.

Figure 5 is a process flow sketch which shows a second example of a separator application from The present invention. The separator is used to separate a two-phase current in two chemical drip bed reactors in parallel.

Figure 6A, 6B and 6C represents an embodiment of the present invention and illustrates channel designs of Alternative suction Figure 6A is a sectional view. cross section of the embodiment taken along the line A-A Figure 6B is a side sectional view. taken along the B-B line. Figure 6C is a side sectional view taken along the line DC.

Figure 7A and 7B represent an embodiment of the present invention where the separator has been Built as an integral part of a chemical reactor. The figure 7A is a side sectional view of the bottom part of a chemical reactor Figure 7B is a cross-sectional view. of the suction channel taken along the line A-A of Figure 7A.

Figure 8 represents an embodiment of the present invention where the separator has been constructed as a integral part of a pipe and shell heat exchanger. Figure 8 is a side sectional view of the heat exchanger. heat and separator.

Alternative embodiments of this invention include but are not limited to the designs shown in the figures.

       \ vskip1.000000 \ baselineskip
    

Background of the invention

The separation of a two-phase current in two or more output streams with identical steam ratio at liquid in each output stream is necessary in many types of industrial process equipment. Are examples:

?

In boiler pipes Parallel blast furnaces are used very often for fluids of processes in order to avoid a boiler pipe diameter excessive and to allow an economical boiler design.

?

They are often used in trains Parallels of modern process plants of heat exchangers heat such as pipe heat exchanger trains and housings It involves avoiding excessive diameters of the set of pipes and / or optimize the integration of heat in a plant process.

?

Team sets of refrigeration are very often organized in parallel due to the limitations in the set size and due to the poor distribution of fluids to the equipment pipes of parallel cooling in case of excessive collector lengths input

?

Such chemical reactors as drip bed reactors can be arranged in a parallel configuration. In applications with high pressures this may involve reducing the diameter of the reactor and therefore the total reactor cost. In the modernization of process plants where it is necessary to add a larger volume of catalyst to the existing plant, the addition of a new chemical reactor in parallel  instead of in series with an existing one it is often very attractive from an economic point of view. The reason is that if you add a new reactor in series with the existing one then the fall of Total reactor pressure increases significantly. This can lead to the need to make expensive substitutions and improve the performance of the pumps and / or compressors. On the other hand, if add a new reactor in parallel, then the pressure drop can actually be reduced to increase production at the plant even with the same pumps and compressors.

       \ vskip1.000000 \ baselineskip
    

History has shown that attempts to separation of a two-phase current in many cases has failed to produce output currents of equal ratio of vapor to liquid. Examples of the consequences of a relationship Uneven vapor to liquid in the output streams are:

For boilers

The boiler pipes that receive the current with a high vapor to liquid ratio receive higher heat than boiler pipes that receive current with a low vapor to liquid ratio due to the lower capacity of steam heating with respect to the liquid. Therefore, the maximum allowable pipe metal temperature can reached even below the heating value for which The boiler was designed. In this way, the boiler may not transfer the heat for which it was originally designed. The consequences They can be low production flow of the process units. In hydrocarbon operation a higher metal temperature of the pipe entails an increase in the formation speed of Coke on the wall of the pipes. The result can be the closing premature unit due to the need to decoke the boiler pipes. Finally, if the vapor and the liquid are distributes to each pipe of the parallel boiler through systems automatic control such as flow control valves, then, in case of failure of the control system one or more pipes from the boiler may suddenly receive no power from liquid. The consequence could be overheating and breakage of the boiler pipe.

For heat exchangers and refrigeration equipment

For parallel heat exchangers and refrigeration equipment overall thermal efficiency is reduced significantly in the case of an unequal vapor ratio to liquid. Especially in critical applications with a approach of temperatures between cold currents And heat. For example, if a heat transfer system It consists of two heat exchangers in parallel A and B, and the exchanger A receives a current with a vapor ratio to high liquid while exchanger B receives a current with a low vapor to liquid ratio. The \ DeltaT driving in exchanger A is lower due to the lower capacity of heating of this current. Therefore, the function of heat transferred in exchanger A is lower. In the exchanger B the ΔT conduction is superior due to the greater capacity of heating this current. Therefore, the function of Heat transferred in exchanger B is higher. But nevertheless, increased heat transfer in exchanger B does not is high enough to compensate for the low transfer of heat in the exchanger A. The total effect is a reduction significant of the total heat transferred in the exchangers. The consequence of a heat transfer lower than the expected in the exchangers can be a speed of inferior production of the process unit that has consequences serious economic

In some cases an unequal distribution of liquid to parallel exchangers can also represent scale, plugging and / or corrosion. An example they are heat exchangers in parallel with vaporization of a liquid. Normally, process plants are designed so that complete vaporization inside the exchanger is avoided. In other words it is impossible to reach the drying point. The reason is that there will always be contaminants in process streams that do not They will evaporate. If the drying point occurs in any area of the exchanger these pollutants would be deposited in the surfaces of the heat exchanger so that the liquid that these originally contained dissolved or dispersed there would be missing. Now, if one of the exchangers in parallel receives significantly less liquid than expected then you can reach the drying point in this exchanger even if it is not I would have planned in the design of the plant. The result can be serious inlays and / or plugging problems in this exchanger followed by low heat transfer speed and the need for premature closure of the unit for cleaning The exchangers.

Another example is the set of equipment air cooling in a hydroprocessing unit. When the effluent is cooled, the ammonium salts type NH4Cl and NH4HS will precipitate and may cause severe corrosion and clogging problems Therefore, wash water is added to dissolve these salts. However, history has shown that the separation of the process stream including water from washing refrigeration equipment sets leads to a poor distribution of washing water and corrosion problems and plugging in the assemblies that receive little or no water from washed.

For chemical reactors

For parallel chemical reactors such as drip bed reactors in a unit of hydroprocessing that achieve an identical steam ratio at Liquid at the inlet of each reactor is of the highest importance. In a hydroprocessing reactor such as a reactor hydrocracking or hydrogen treatment where the components of hydrocarbon react with hydrogen in the presence of a catalyst  solid to a feed with a low vapor to liquid ratio towards a reactor will lead to a hydrogen partial pressure more low which will again lead to a lower reaction rate, a higher coke formation speed and a deactivation of the catalyst. Even short periods of operation with too low vapor to liquid ratio of the feed to reactor can represent serious damage to the face load of catalyst particles in the reactors.

       \ vskip1.000000 \ baselineskip
    

Detailed description

The separator of the present invention can be designed to be manipulated to any separation relationship required The separation ratio is defined as mass flow total of an output current divided by mass flow Total input current. For example, the invention may be designed for a 50% / 50% separation but also for a 5% / 95% separation. Since the two phase separator is a open system without any control valve and with little drop of global pressure, is the hydraulic power of the flow systems downstream and not the two phase separator itself that marks the separation ratio. When the separator is properly designed ensure that the ratio of vapor to liquid in each of the output current are close to equal even if the ratio of separation deviates from the one that designed the separator two phases The reason is described below:

That is to say that a current separator has been designed to separate a two-phase input current into two output currents with separation ratios of 30% / 70% for the suction channel A and B respectively. Said design normally represents openings of different sizes in the two channels of suction and a different cross-sectional area of the two suction channels. Now for some operating modes the separation ratio could be 40% / 60% instead of 30% / 70% for which the two phase separator was designed. In that case, more steam flows than originally intended through the openings on the side of the suction channel A. The pressure drop from the outside with respect to the inside of the suction channel A is therefore so much bigger Consequently, more liquid is collected inside the suction channel. Less steam than originally planned flows to through the openings on the side of the suction channel B due to The lower separation ratio for this suction channel. The pressure drop from outside with respect to the inside of the channel Suction B is therefore inferior. Consequently, less is collected liquid inside the suction channel. In this way, the design It tends to compensate for the different separation ratio.

If the separation ratio for a channel of Suction given during certain modes of operation is higher than expected then the upper steam flow will lead to a superior liquid flow. Similarly, if the ratio of separation of a given suction channel is less than expected then the lower steam flow will lead to a liquid flow lower. The result is that the ratio of vapor to liquid in the outlet pipe is only affected by the separation ratio That has changed to a small degree.

A first example of the capacity of the separator of maintaining the vapor to liquid ratios identical in the Output currents are given in Figure 4 which shows a sketch of a process flow of a process system with exchangers of parallel heat, instrumentation and boiler pipes. The cold two-phase power supply 50 must be heated by heat exchanger with hot currents 58 and 65 and by using boiler 61. First, the cold stream 50 in three streams 52, 53 and 54 by the use of separator 51 of the present invention. The current output 52 is passed through line A which consists of the sides of the heat exchanger housing of pipes and casing 55a, 55b, 55c and 55d and pipe passage 67 of the boiler 61. The output current 53 is passed through the line B consisting of the sides of the housing of the pipe and shell heat exchangers 56a, 56b, 56c and 56d and the pipe passage 68 of the boiler 61. The output current 54 is passed through line C consisting of the sides of pipe heat exchanger pipes and casing 57a, 57b and 57c and control valve 69. Output currents 62, 63 and 60 of line A, B and C respectively combine in the stream of product 64. The designed steam and liquid flow rates and properties of separator 51 are given in table 1.

       \ vskip1.000000 \ baselineskip
    

TABLE 1 Steam and liquid flow rates designed and properties of separator 51 in Figure 4

one

       \ vskip1.000000 \ baselineskip
    

The separator 51 was designed for a ratio of 40% / 40% / 20% separation on line A, B and C respectively. He objective was an identical vapor to liquid ratio of each of the output currents 52, 53 and 54. When the ratio of actual separation is identical to the designed separation ratio of 40% / 40% / 20% the ratio of vapor to liquid in the three streams Exit 52, 53 and 54 will be close to equality. But nevertheless, it happened that the pressure drop for a given flow rate was 20% higher on line A of the planned one. The difference in resistance to flow was due to a different pipe layout and a slightly different exchanger and boiler design for two parallel lines A and B. Also, it happened that the pressure drop  for a given flow rate it was 30% lower on line C of the originally planned. The low resistance to flow of the C line it was due to higher flow requirements controlled by the valve of control 69. Due to the different resistance to flow of the parallel flow systems the separation ratio was different than expected

Now, the difference in steam ratio to liquid in each parallel line caused by the difference from the expected flow resistance of line A and line C was evaluated during 9 points of the flow of steam and liquid. The points of steam and liquid flow rates evaluated and the results are shown in Table 2. Vapor and liquid flows correspond to 50%, 100% and 200% of the designed steam and liquid flow rates respectively. Evaluation results such as ΔP through the separator, ΔP through the three lines, the volumetric ratio of vapor to liquid for currents 52, 53 and 54 and% DVLR are also shown in the Table 2. The percentage of the difference in the steam to Liquid (% DVLR) is defined as:

Equation (2)

2

Where VL_ {i}, and VL_ {feed} are the relationship of volumetric liquid vapor of the output stream "i" and the feed current "input" respectively, and where "Nsplit" (number of separations) is the number of output currents of the separator.

As shown in Table 2, the design of the given separator shows excellent performance over a very wide range of steam and liquid flow rates even when the flow resistance of downstream systems are different from The originally designed.

The vapor to liquid ratio varies from 1.3 to 21.5 and the pressure drop of the lines varies from 1.3 bar to 20.9 pubs. The average% DVLR due to the top 20% flow resistance of line A and at 30% lower resistance to line flow B is as low as 2.97%.

       \ vskip1.000000 \ baselineskip
    

TABLE 2 Performance of separator 51 with flow resistance different than expected downstream systems

3

       \ vskip1.000000 \ baselineskip
    

The performance of the separator is affected by the mechanical tolerances during the manufacture and installation of the separator. THE relative evaluation of the suction channels and the flow area of the openings in the suction channels affects especially to performance.

A second example of an application of separator of the present invention is shown in the diagram of process flow in Figure 5. A drip bed reactor 75 located with 190 m3 of catalyst particles is too much Small to produce the desired product at the desired flow rate. For the therefore, 90 m3 of additional catalyst volume should be added Instead of adding the new catalyst volume in series with the existing reactor a new reactor 74 is installed in parallel to the existing reactor 75. The separator 71 of the the present invention to separate the feed current from two phases 70 in two output currents 72 and 73 that are fed to reactors 75 and 74 respectively. The separation ratio is 32% / 68% to reactor 74 and 75 respectively. Downstream of the reactors, the output current 76 of the reactor 74 is combined with the output current 77 of the reactor 75 within the current of product 78. The suction channels in the separator are attempted 71 are at the same level but in this example the suction channel A corresponding to the current 72 rises 10 mm above the of suction channel B corresponding to current 73. Also The flow area of the openings in the suction channel A is 2% greater than desired and the flow area of the openings in the channel Suction B is 2% lower than desired. Both the difference of level of the suction channels as the difference in the area of opening flow will increase the vapor to liquid ratio of the current 72 with respect to the current 73.

The separator 71 is designed for flow rates of vapor and liquid and with the properties given in table 3.

       \ vskip1.000000 \ baselineskip
    

TABLE 3 Designed steam and liquid flow rates and properties for the separator of figure 5

4

       \ vskip1.000000 \ baselineskip
    

Now the difference in steam ratio to liquid,% DVLR, as defined in equation (2) due to the manufacturing mentioned above and to the tolerances of installation is evaluated for a wide range of conditions of functioning. The operating conditions evaluated are given in Table 4 and correspond to 50%, 100% and 200% of flows designed steam and liquid respectively. The results of the evaluation such as ΔP through the separator, ΔP a through the reactors, the volumetric ratio of vapor to liquid for currents 72 and 73 and% DVLR are also given in the Table Four.

       \ vskip1.000000 \ baselineskip
    

       \ vskip1.000000 \ baselineskip
    

       \ vskip1.000000 \ baselineskip
    

(Table goes to page next)

TABLE 4 Separator performance with the worst case manufacturing and installation tolerances

5

As can be seen from Table 4, they are achieved excellent separation yields over a very wide range of steam and liquid flow rates even with the worst manufacturing case and installation tolerances.

For the two examples in Figure 4 and 5, the separator was designed to produce output currents with identical vapor to liquid ratios. The current separator It can also be designed to produce output currents from different ratios of vapor to liquid. For example, the separator could be designed to separate a two phase input current in three output currents with separation ratios of 20% / 20% / 60% and with volumetric ratios of steam to liquid of 12/10/20. However, in most industrial applications it is desirable in the current separators current separators of two phases with identical vapor to liquid ratio.

The separation of steam and liquid in the separator of the present invention should not necessarily be as good as in a traditional phase separator. It is enough that the part of Liquid mass separates from steam. Drops of smaller liquid that pass with steam into the channels of suction also even if the steam is eventually distributed. For the Thus, the separation of the two-phase current separator can be designed for higher linear steam speeds and of this way smaller cross-sectional area than the traditional phase separators. Also, the delay time of required liquid is significantly lower for separation with the two phase current separator that stops a separation Traditional instrumentation like the one shown in Figure 2. Traditional instrumentation dividers have a liquid delay time of 5-20 minutes to allow during the response time for the control system level and to allow operators to perform manual actions in case of failure of the automatic control system. For him Two phase current separator is set more or less Instantly and mainly fixed by the steam load. By therefore, the delay time of the liquid in the separation with the Two phase current separator can be as small as 5 seconds. The total result is that the separation with the separator Two-phase current is very compact compared to traditional phase separations used in the industry process. As an example, the size and cost of the container is compared pressure gauge 51 of Figure 4 designed for steam and liquid flow rates and properties in Table 1 with the size and cost of the pressure vessel of a phase separation conventional as shown in Figure 2. Phase separation Conventional is also designed for vapor and liquid flows and properties of Table 1. The results are given in Table 5.

TABLE 5 Comparison of the size and cost of the container pressure of a separator and a separation conventional

6

The cost given in Table 5 is the cost of Container plus internal elements such as suction channels. He installation cost including foundation, building, insulation, piping systems and instrumentation etc. no this included. The total installation cost is usually 3 to 4 times the cost of the equipment given in Table 5. As can be seen of Table 5, the separator of the present invention represents a low cost and compact option regarding the use of a conventional phase separation.

Figures 3A, 3B, 3C, 6A, 6B, 6C, 7A, 7B and 8 represent alternative structures of the separator of the present invention. The figures are represented only to exemplify the invention and alternatives. These are not intended to limit the scope of the concepts described in the invention or serve as work graphics. These should not be constructed as limits of capacity of the scope of the inventive concept of the invention. The relative dimensions shown in the drawings should not be considered equal or proportional to commercial achievements.

Reference will now be made to the figures of the embodiments of the present invention. The separator 30 shown in Figure 3A, 3B and 3C is a separator for separation of an input current 41 in two output currents 42 and 43. The separator 30 consists of a container 31 with a pipe of inlet 32 and two outlet pipes 44 and 45. The inlet pipe 32 is connected to the wall of the container 31 with a gasket fluid tightness. The lower end of the pipe 32 is open to allow input current 42 to enter the container 31. Under the inlet pipe 32 there is a plate of flow shock 33 with side walls 40. The shock plate of flow 33 and side walls 40 form a flow channel that first divide the input current 41 into two currents and, then, they direct these two currents towards the cylindrical wall of the container 31. Two vertical suction channels 34 and 35 in the container 31. Each suction channel consists of a Circular pipe with open upper and lower ends. He lower end of the suction channel is submerged in the liquid 39. The upper or outlet end of the suction channel 34 is connected to outlet pipe 44 and the upper end or of suction channel outlet 35 is connected to the pipeline outlet 45 to form two flow channels out of the container 31. The fluid tight seals are provided between the walls of the container 31 and the outlet pipes 44 and 45. The channel of suction 34 is provided with openings 37 on the sides of the pipe and suction channel 35 is provided with openings 36 in The side of the pipe.

Then during operation, the two-phase input current 41 enters container 31 a through the pipe 32. The two-phase jet hits the plate flow shock 33 that slows the high velocity of the current and directs the current to the cylindrical walls of the container 31. Inside the container 31 the liquid phase 39 is separated from the phase steam 38. The liquid phase is collected in the phase collection zone Weighed at the bottom of the container while the vapor phase is located in the light phase collection zone in the part container top. Next, steam 38 flows through of the fraction of openings 36 and 37 on the sides of the suction channels that are above the surface of the liquid. The flow through the openings has a drop of pressure from outside the suction channel into the suction channel and, therefore, the liquid rises inside the suction channel. Liquid 39 flows through the ends lower openings of suction channels 34 and 35 and through the fraction of openings 36 and 37 that are below the surface of the liquid in the container 31. The liquid is mixed with the steam in the suction channels and the mixing of the two phases flows upwards through the inside of the suction channels towards the exits thereof and out of the container 31 through the outlet pipes 44 and 45.

Preferably, the power input is symmetrically positioned between the suction channels as indicated in figure 3A. This will represent the smallest section area required cross section of the vessel for separation of vapor / liquid and will also distribute small drops of liquid that They are in the vapor path more evenly. Preferably, the separator is designed so that the input current of feed shock or impact the plates and walls as shown in Figures 3B and 3C. When the power supply inlet collides the plates and walls, the liquid tends to separate of the vapor phase and the inlet jet is also prevented from high speed reach the liquid surface in the container what which could represent a reentry of the liquid and the formation of waves.

The total area of the openings in the channels of suction is selected to obtain the desired liquid level in the recipient. A larger area of openings leads to a smaller vapor pressure drop and, therefore, a higher level of liquid, so that the small pressure drop is related With the vertical height that the liquid should rise. The other way, a smaller area leads to a lower liquid level. The area of the openings in each suction channel can be used to establish the vapor to liquid ratio of the output stream of said suction channel. If the area of the openings in a channel of suction A is increased in relation to the area of the openings in another suction channel B, then, the vapor to liquid ratio of the output current of the suction channel A increases in relation to to the vapor to liquid ratio of the suction channel B. The area of cross section and the shape of each suction channel also affects the level of liquid in the container and the ratio of steam to liquid of each output stream.

The openings in the suction channels shown in Figure 3A are circular holes. But nevertheless, these openings can also be vertical slots or have other V-shaped, triangular, rectangular, polygonal shapes, ellipsoidal, etc. The openings area does not necessarily it needs to be uniformly distributed over the entire height of the suction channel. For example, a suction channel can have a smaller area of the openings near the bottom end and a largest area of openings near the head end.

The suction channels shown in Figure 3A and 3B have circular cross sections but the channels of suction can also have many other section shapes transverse such as triangular, rectangular, ellipsoidal, polygonal, etc. Also the cross-sectional area of the suction channels may vary along the length of the channel suction

The tail ends of the suction channels shown in Figure 3A are open for fluid flow. However, in many cases the improved separation performance can be achieved if the tail ends of the suction channels they are closed and, therefore, all the liquid must pass through of the openings on the sides of the suction channels that They are below the surface of the liquid.

The separator suction channels shown in Figure 3A and 3B are vertical. However, the channels of Suction need not be completely vertical. It's enough so that the suction channel has a vertical component or, in other words, that the liquid is forced through the suction channel to flow up in front of the openings for the entrance of steam before reaching the main suction channel outlet inside one of the outlet pipes 44 and 45.

The container 31 of the separator in Figure 3A, 3B and 3C is a horizontal cylindrical container with head ellipsoidal However, the separator or container of the present Invention can have any form and orientation. Other examples of container shapes and orientations are cylindrical containers vertical, spherical containers, box-shaped containers with rectangular cross sections, etc.

The input and output currents enter and they exit through the head wall of the container 31 in the Figure 4. However, the input and output currents can enter through other walls such as the back walls or lateral.

Examples of variations of the present invention they are illustrated in the separator shown in Figure 6A, 6B and 6C. He separator 80 consists of a vertical cylindrical container 81. The separator has an input current 88 that enters via pipe 87 through the side wall of vessel 81. Downstream of this entrance is placed a vertical impact plate 86. The separator has three output currents 91, 92 and 85. The current outlet 91 flows via outlet pipe 99 through the wall top of container 31. Outlet pipe 99 is connected to a tight form to the suction channel 82. The suction channel 82 it has a circular cross section and narrows so that The cross-sectional area of the channel decreases downwards. He suction channel 82 is provided with four vertical slots 94. The suction channel 82 is open for the liquid to flow to the tail end The output current 92 flows via the pipeline exit 98 through the side wall of the container 31. The pipe output 98 is connected in a sealed manner to the suction channel 83 using a 90º 97 curve. Suction channel 83 has a square cross section. Suction channel 83 is provided with four V-shaped slots 93. Suction channel 83 is open for the liquid to flow to the tail end. The current outlet 85 flows through the pipe 100 through the wall bottom of container 31. Outlet pipe 100 is connected to a tight form to the suction channel 84 using a curve of 180º 96. Suction channel 84 has a cross section circular and is provided with 95 square openings. The channel of suction 84 is closed to the flow of liquid at the tail end and, therefore, all the liquid must flow through the square openings 95.

During operation the current of two-phase inlet 88 enters container 81 through the pipe 87. The two-phase jet hits the impact plate 86 which slows the high speed of the current and entails in a certain way degree to phase separation. Inside the container 81, the liquid phase 90 is separated from vapor phase 89. The liquid phase is collects at the bottom of the container while the vapor phase is in the top of the container. Next, steam 89 flows to through openings 93, 94 and 95 on the sides of the channels suction 83, 82 and 84 respectively. Steam flow through of the openings causes a pressure drop from outside the suction channel to the inside of the suction channel and, therefore Thus, the liquid rises inside the suction channel. The liquid 90 flows through the lower open ends of the suction channels 82 and 83 and through the opening fraction 93, 94 and 95 that are below the liquid surface of the vessel 81. The liquid is mixed with the steam in the channels of suction and the two-phase mixture flows into the channels of suction and out of the container 81 through the outlet pipes 98, 99 and 100.

The separation performance of the present invention is quantified as% DVLR as defined in the Equation (2) is reduced in applications with a high ratio of vapor to liquid. In applications with high steam ratio a liquid, the performance of the present invention can improve significantly using internal elements within suction channels to increase the pressure drop in the flow of Two phases inside the suction channel. One of the examples of sayings internal elements to increase the pressure drop is the use of one or more holes in the suction channel and for improve separation performance. In addition, the use of internal elements within the suction channel has an effect on the two-phase flow model in the suction channel. By For example, the use of holes tends to eliminate the flow with unwanted stagnation when liquid stagnates and vapor Saved periodically flows into the suction channel. The biggest improvement in separation performance due to the use of elements internal in the suction channel is achieved in applications with a high vapor to liquid ratio but some are also achieved improvement in applications with low vapor to liquid ratio. By example, separators 51 and 71 of Figure 4 and 5 respectively included internal elements in the suction channels to improve separation performance.

All separators 30, 51, 71 and 80 in the Figure 3A, 3B, 3C, 4, 5, 6A, 6B and 6C have their own separator or container. However, the present invention can be used as an integral part of other process equipment such as, by example, pipe and shell heat exchangers and chemical reactors

Figure 7A and 7B shows an example of a separator of the present invention which is an integral part of a chemical drip bed reactor 110. Figure 7A shows the bottom part of this drip bed reactor. The particles of catalyst 103 are loaded into the pressure housing cylindrical 101 with hemispherical heads 102. The catalyst is supported by a grid or catalyst support screen 104. The catalyst support grid or sieve is designed in so that the catalyst particles cannot move through of the sieve but the vapor and the liquid. Under the rack or catalyst support sieve two suction channels are placed vertical 107. Each suction channel is provided with eight slots 108. Suction channels are also provided with elements internal to increase the pressure drop of the suction channel. These internal elements consist of four holes 109, 110, 111 and 112 for each suction channel. Each suction channel 107 is connected to an outlet nozzle 105 tightly using 106 channels with curves.

During operation steam and liquid they flow down this moment through the bed of particles of catalyst 103 and through the support grid or sieve of the catalyst 104. Under the support grid or sieve of the catalyst 104 there is an open space where liquid phase 113 is separates from the vapor phase 114. The liquid phase 113 is collected in the bottom of the reactor. Next, steam 114 flows through the small part of the slots 108 that are above the liquid surface. The flow through the grooves causes a pressure drop from the outside of the suction channel to the  inside the suction channel and therefore the liquid is lifts inside the suction channel. Liquid 113 flows through of the opening of the lower holes 112 and through the small part of the slots 108 that are below the surface of the liquid The liquid mixes with the steam in the channel suction and flows through the suction channel and the holes and exits the reactor 110 through the nozzles 105.

Figure 8 shows an example of a separator according to the present invention which is an integral part of a pipe and shell heat exchanger 120. The exchanger Pipe and shell heat consists of:

?

A head 122 with a plate cover 128, a side pipe inlet nozzle 129 and a side pipe outlet nozzle 130.

?

A housing 121 with a nozzle input 131 and two outlet nozzles 125.

?

A set of shaped pipes of U consisting of U-shaped pipes 124, a tubular plate 135 and thirteen flow deflectors 132.

       \ vskip1.000000 \ baselineskip
    

The length of the housing 121 has been increased slightly compared to normal exchanger designs of heat to have space for a two-phase separator according to the present invention on the housing side downstream of the last flow deflector and downstream of the 180º curves of the U-shaped pipes 124. The separator consists essentially of two vertical suction channels 126 with holes 127 in the walls. The tail end of the suction channels 127 are open and available for fluid flow.

During operation the lateral fluid of the pipe enters the exchanger through the nozzle 129 and is directs through and inside the U-shaped pipes and exits the exchanger through the nozzle 130. The fluid side of the housing enters the exchanger through the nozzle 131 and can be a single phase or two current phases In addition to heat transfer, it can take place in the condenser or vaporization exchanger. The lateral fluid of the housing flows through the outside of the pipes in the form of U. Flow deflectors 132 generate different sections of transverse flow where the lateral fluid of the housing is forced to flow through perpendicular to the pipes. After of passing the last flow baffle, the two-phase current enters the separation space where the liquid 133 separates from the steam 134. Liquid phase 133 is collected in the tail of the housing 121. Next, steam 134 flows through the fraction of holes 127 that are above the surface of the liquid. He steam flows through these holes causing a fall of pressure from the outside of the suction channel inwards from the suction channel and, therefore, the liquid rises towards up in the suction channel. Liquid 133 flows through the open tail end of suction channels 126 and through the small part of holes 127 that are below the liquid surface. The liquid mixes with the steam in the suction channel and flows through the suction channel and leaves the exchanger 120 through nozzle 125.

In the examples given in Figures 4 and 5, distributes a two-phase input current to systems of parallel downstream pipes and process equipment. But nevertheless, the present invention can also be used within the equipment of process to distribute steam and liquid evenly towards the parallel steps in the team. An example is the use of the present invention in the inlet manifold.

In all the examples of the invention given here there is only one suction channel connected to each outlet pipe from the separator. However, more than one channel of suction by output current. If more than one channel is used suction by output current, then, the suction channels connected to an output current will not necessarily need Be identical For example, a separator designed for the separation of a two-phase input current into two output currents can have a total of five channels of suction of different sizes with three suction channels all connected to a first output current and the two channels of remaining suction connected to the second output current. In some cases, the use of suction channels with sizes different for the same output current can lead to a Improved separation performance.

In all examples of applications according to invention given here there is only one input current to the separator. However, more than one current of inlet to separator separator vessel. They can also used single phase inputs that transfer only steam or liquid only

In addition to the separation capacity of a two-phase vapor-liquid mixture, the separator the present invention can also be used to separate a mixing of two phases of immiscible liquids such as one phase hydrocarbon liquid and an aqueous liquid phase in two or more output currents with the desired oil to water ratio in each output current

In general terms, it can be highlighted in the Present invention the following:

The invention relates to a device of separation for separation or division of a current of two phase input consisting of a light phase and a phase weighed in two or more output currents with the phase relationship Light to heavy desired at each output current. The device separation consists of a container or separation container With one or more entries. Separation takes place in the container partial or complete of the light and heavy phases. The container is provides with at least two hollow suction channels with a lower end and an open upper end.

Openings are provided on the side of each section channel at least one level between the ends lower and upper. The lower end of the suction channel is submerged in the heavy phase while the open end upper suction channel is in the light and connected phase of waterproof way through flow channels to downstream systems.

The suction channels must have a vertical component so that during operation so less a part of the opening area is level above of the interface level. During operation the light phase flows through the part of the area of the openings that is most above the interface level and in this way a fall is created of outside pressure that affects the suction channel. Because said pressure drop the heavy phase rises upward in the suction channel through any open bottom end and to through any opening that is located at levels below of the interface level. In the suction channel, the heavy phase is Mix with the light phase. The two phase current flows through of the suction channel and through said flow channels to downstream systems.

Internal elements can be used or flow restrictions within the suction channels to increase the pressure drop and modify the flow rate of two phases in the suction channel.

The internal elements can be holes with circular flow openings.

The tail end of the suction channel can be closed and the entire heavy phase must flow through the openings on the side of the suction channels that are located below the interface level.

The container or container can be a part integrated from other process equipment used for other purposes such as carrying out chemical reactions or heat exchange In addition to the purpose of separating a current.

These downstream systems can be steps of parallel flow in the same part of the equipment as the separator be integrated

These downstream systems can be system of process consisting of pipes, instrumentation and equipment.

Suction channels can have sections circular cross sections.

The openings on the side of the channels Suction can be circular holes or rectangular grooves.

Preferably, the vertical height of the tail of the suction channel at the highest opening is between 100 mm and 1500 mm

Preferably, the two phase flow rate at the upper end of the suction channels is between
0.5 m / s and 15 m / s for at least one phase of operation.

One or more channels of suction to each downstream system.

Advantageously, the device can be used to separate a two-phase vapor / liquid mixture to heat exchangers in parallel.

Advantageously, the device can be used to separate a two-phase vapor / liquid mixture to pipes of parallel boiler.

Advantageously, the device can be used to separate a two-phase vapor / liquid mixture to reactors Chemicals in parallel.

Advantageously, the device can be used to separate a two-phase vapor / liquid mixture to equipment parallel cooling

Advantageously, the device can be used to distribute steam and liquid to pipes or channels of heat exchange in parallel in a heat exchanger of Two phases or refrigeration equipment.

       \ vskip1.000000 \ baselineskip
    

References cited in the description

This list of references cited by the applicant is intended solely to help the reader and not It is part of the European patent document. Although it has been put maximum care in its realization, errors cannot be excluded or omissions and the EPO declines any responsibility in this respect.

Patent documents cited in the description

US 5190105 A [0007]

US 4396063 A [0009]

US 4824614 A [0010]

US 5810032 A [0010] [0011]

JP 62059397 A [0012]

US 4528919 A [0012]

US 4512368 A [0012]

US 4516986 A [0017]

US 4800921 A [0018]

US 4574837 A [0019]

US 4574827 A [0020]

US 5437299 A [0020]

US 5059226 A [0021]

EP 0003202 B1 [0022]

US 4293025 A [0025]

US 4662391 A [0026]

JP 03113251 A [0026]

JP 02197768 A [0026]

US 5250104 A [0027]

Documents that are not patents cited in the description

MR. OVID BAKER How to size process piping for two-phase flow. Hydrocarbon Processing , October 1969 , 105-116 [0011]

Claims (21)

         \ global \ parskip0.950000 \ baselineskip
      

1. Device (30,80,110,120) for separating a current to separate one or more input currents from two phases (41.88) consisting of a light phase fluid and a fluid heavy phase, for example a two-phase vapor / liquid mixture, in two or more two-phase output currents (42.43; 91.92; 129) with the desired ratio of light phase to heavy phase in each output current, the device comprising: - a container or separation container of phases (31; 81; 101,102; 121) comprising:

-

one or plus input current inputs (32,87,119) for said input current (41.88),

-

a heavy phase collection zone (39,90,113,133), and

-

a Light phase collection zone (38,89,114,134) at one level greater than that of said heavy phase collection zone (39,90,113,133), and

- two or more channels or suction ducts (85) (34.35; 82.84.87; 106; 126), at least one for each of said output currents (42.43; 91.92; 125), each comprising suction channel or duct:

-

for the minus one heavy phase input in communication with the zone of collection of said heavy phase (39,90,113,133),

-

for the minus one light phase input in communication with the zone of collection of said light phase (38,89,114,134) and located at a level greater than that of at least one heavy phase input, Y

-

for the minus one output current output (44.45; 98.99; 105.125) for communicate with the outflow streams of water outlets down the device,

being located said at least an entry of the light phase between said at least one input of the heavy phase and said at least one current output of output (44.45; 98.99; 105; 125). 2. Device according to claim 1, wherein a suction duct (34.35; 82.83.84; 106; 126) comprises a elongated tubular element defined by a wall that has one or more openings (36.37; 93.94; 95; 108; 127) inside, being said tubular element for example a pipe or a conduit with a circular or rectangular cross section. 3. Device according to claim 2, wherein the lower end of said tubular element is open. 4. Device according to claim 2 or 3, where the form of said one or more openings (36.37; 93.94.95; 108; 127) is selected from the group of forms comprising the Circular, elliptical, oval, rectangular and triangular shapes. 5. Device according to any of the previous claims, wherein a light phase input and a heavy phase input consist of a single opening (93.94; 108) which has an appreciable vertical extent, preferably a groove that extends in the direction longitudinal of said suction duct. 6. Device according to claim 5, wherein the width of said slot (93) increases in the direction towards said output current output. 7. Device according to claim 5, wherein said width of said slot (94,108) is substantially constant. 8. Device according to any of the preceding claims, wherein the flow restriction means (109,
110,111) are disposed within said suction ducts (106) to increase the pressure drop in said light phase through a light phase inlet. 9. Device according to claim 8, wherein said flow restriction means (109,110,111) comprise a cross plate with one or more holes there such that the flow is forces one or more to pass through the suction line (106) holes 10. Device according to any of the previous claims, wherein the flow impact means (33) are provided adjacent to said current input of input (32) such that said input current (41) impacts said flow impact means (33). 11. Device according to any of the previous claims, wherein the vertical distance between the lower part of said one or more heavy phase inputs and the highest part of said one or more light phase inputs is by at least about 100 mm and even more about 1500 mm, preferably between 400 mm and 600 mm, even more preferably about 500 mm.

         \ global \ parskip1.000000 \ baselineskip
      

12. Processing facility comprising a team to carry out a physical or chemical procedure using a two phase current and a separation device of a current according to any one of claims 1 to 10, said device being interconnected to an input or an output of said team. 13. Installation according to claim 12 wherein said equipment comprises a boiler (61) comprising an assembly of boiler ducts (62.63) connected to said outlets of output current (52.53). 14. Installation according to claim 12, where said equipment comprises heat exchangers in parallel (55,56,57) connected to said output flow outputs (52.53.54). 15. Installation according to claim 12, where said equipment comprises chemical reactors in parallel (74.75) connected to said output current outputs (72.73). 16. Installation according to claim 12, where said equipment comprises air coolers connected to said output current outputs. 17. Two phase reactor, such as for example a drip bed reactor (110) or a catalytic reactor, which it comprises a device for separating a current according to any of claims 1 to 10. 18. Reactor according to claim 17 which it also comprises an outer shell (101,102), where said separation vessel of said phases is located within said reactor housing. 19. Heat exchanger comprising a device for separating a current according to any of the claims 1-10. 20. Heat exchanger according to claim 19 further comprising an outer shell, wherein said separation vessel of said phases is located inside of said heat exchanger housing. 21. Separation procedure of one or more two-phase input currents (41.88) consisting of a fluid light phase and a heavy phase fluid, for example a mixture two-phase vapor / liquid, in two or more output streams of two phases (42.43; 91.92; 125) at the desired light phase ratio regarding heavy phase in each output current, comprising the Procedure the following stages:

-

for the minus the partial separation of the input current (91.88) in a heavy phase part located in a heavy phase zone (39,90,113,133) below a boundary area of inter-phase and in a light phase part located in a light phase zone (38,89,114,134) above said surface inter-phase limit, and

-

he mixing the heavy phase fluid of said heavy phase part with the light phase fluid of said light phase part in two or more sites in said light phase zone to form said two or more two-phase output currents (42.43; 91.92; 125).