CN102792116B - Heat exchanger - Google Patents
Heat exchanger Download PDFInfo
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- CN102792116B CN102792116B CN201180012905.5A CN201180012905A CN102792116B CN 102792116 B CN102792116 B CN 102792116B CN 201180012905 A CN201180012905 A CN 201180012905A CN 102792116 B CN102792116 B CN 102792116B
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
- F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
- F28F9/027—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes
- F28F9/0273—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes with multiple holes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a heat exchanger (1) for vaporising a liquid by exchanging heat with a fluid, comprising: a body including an assembly of plates (3) disposed parallel to a pre-determined direction (11) defining therebetween a plurality of passages (4, 5), comprising a first group of passages (4) intended for the flow of the liquid and a second set of passages (5) intended for the flow of the fluid; a retention tank (2) for receiving the liquid; elements (6) for the primary distribution of the liquid, designed to distribute the liquid from the retention tank (2) to the first group of passages (4); elements (7a) for the secondary distribution of the liquid, located in the first group of passages (4); and means for establishing fluid connections between particular zones (14) and a gas tank located outside the exchanger (1), such as to allow pressure balancing between the tank and the zones (14).
Description
Technical field
The present invention relates to by using perpendicular plate heat exchanger and second fluid heat exchange to make liquid gasification.The present invention is particularly useful for air distillation installation.
Background technology
In double tower type air distillation installation, the liquid oxygen in the tank of lower pressure column is by gasifying with the gaseous nitrogen heat exchange of therefrom pressing top of tower to flow out.For the given operating pressure of lower pressure column, the temperature difference between the oxygen certainly existed due to the structure of heat exchanger and nitrogen determines the operating pressure of medium pressure column, therefore, wish that this temperature difference is little as far as possible, to make the expenditure relevant to compressing the pending air sprayed in medium pressure column minimize.
The technology being generally used for these phase transformation interchangers is the aluminium soldering plate fin type heat exchanger of the compact component of height that can obtain the heat exchange area providing large.These interchangers are made up of plate, are inserted with corrugated plating (ondes) or fin between described plate, thus form folded gasification " path " and a condensation " path ".There is various corrugated plating, such as the corrugated plating (" Sawtooth waves card ") of straight corrugated plating, perforation corrugated plating or partial offset.
In the situation of the gasifier operated under being falling liquid film pattern, a part for equipment is for distributing the liquid in gasification path and between the passage of heat exchange corrugated plating.
This distribution for each gasifier performs according to the principle described in document FR-A-2547898 usually: gasification path is supplied to from the top of condensation pass.Oxygen is then through a perform hole, and oxygen is mainly distributed (first sub-distribution) in gasification path by described hole.Then oxygen flow through the corrugated plating of a collection of horizontal bus, and it performs the distribution (being spread out by liquid in the path between the passage formed by corrugated plating) being more accurately called secondary distribution (secondary distribution).Gaseous nitrogen circulates in " condensation " path being parallel to " gasification " path.Two kinds of fluids in the total length cocycle of described path, to make thermo-contact maximize.
The liquid oxygen of gasification comprises the impurity in dissolved form.Main impurity is nitrous oxide (N
2o), carbon dioxide (CO
2), hydrocarbon (C2, C3 etc.).Depending on operating conditions, these impurity can be deposited in gasification path in solid form or in liquid form.At industrial scale, importantly control the formation of these solids or liquid precipitation thing, to avoid any risk of explosion.
The flow rate of liquid of every passage or every meter of circumference to be moistened is one of important parameter relevant with sedimentary formation.This is because, when the flow rate of liquid of every passage not high enough with wetting wall time, sediment is by gasifying to dry and formed.
In this (film) gasifier, the distribution of liquid oxygen plays an important role in their operations (performance and safety).Therefore, need to guarantee that liquid is correctly assigned in each passage in all cases.For this reason, Liquid distribution between channels must be full and uniform.Uneven Liquid distribution may cause the bad wetting of the corrugated plating in the bottom of especially interchanger, and therefore causes gasification to form sediment to drying.Difficulty is to guarantee to keep equal flow rate of liquid in whole passage when the number of channels of every body and every path (550 passages/path, 55000 passages/body) is certain.
The quality of this Liquid distribution depends on that the good design of distributor and good size are determined.
The main distribution (spreading out between path) of liquid obtains through being arranged in the hole bottom the liquid pool be positioned at above passage by making liquid.Be called that the distribution (spreading out in each path) of secondary distribution uses a collection of corrugated plating with horizontal bus and partial offset to obtain usually.
But in final analysis, liquid is not spread out sufficiently uniformly all the time in passage, and still there is the risk of evaporate to dryness.
Therefore, the problem that solve guarantees that liquid is assigned to one better and reduces this risk between the passage of identical path.
Summary of the invention
For this reason, the solution of the present invention relates to a kind of for by making the heat exchanger of liquid gasification with fluid heat transfer, and this heat exchanger comprises:
-body, it comprises the board component being parallel to the direction determined, is limited with a large amount of path between described plate, comprises for first group of path of described liquid flow and second group of path flowing for described fluid;
-be used for receiving the holding tray of described liquid;
-main distribution member, it is for described liquid, can and be designed to described liquid to be assigned to described first group of path from described holding tray; And
-be positioned at the side identical with described holding tray, the closure elements of each path for closing described second group, with the secondary distribution element for described liquid being arranged in described first group of path, and can and be designed to described Liquid distribution in each path of described first group;
At least 80% of the path of-described second group, preferably described second group non-circumferential path 100% comprise the device that can prevent described fluid from flowing in the region of the described path of described second group, described region from described plate extend in described plate another and between described device and described closure elements, in described region each at least in part subtend belong in described first group closest to two in the described secondary distribution element of two paths in described region discussed, the feature of described heat exchanger is, described heat exchanger comprise can and be designed to establish the opening that the fluid between described region with the gas container outside described interchanger is connected, to allow the isostasy between described reservoir and described region.
This can be avoided potential pressure differential between each several part of locating due to shadow region and the subtend shadow region of path that retains for liquid and the damage caused.
In the situation of distillation, the reservoir for equilibrium is the reservoir of gaseous oxygen.
Involved liquid can belong to any type.According to an embodiment, liquid oxygen produces from distillation.This oxygen is usually very pure.Fluid can belong to any type.According to an embodiment, fluid is the nitrogen from distillation.Before heat exchange operation, fluid normally gaseous state.Liquid is heated and is become and partially or completely gasified.Fluid cooling also partially or completely condensation.
Demarcation strip normally parallel and form the framework of interchanger body.Be limited with multiple smooth path between demarcation strip because demarcation strip the direction determined or longitudinally on and be microscler on the direction being orthogonal to this direction.This direction determined is by direction that the fluid of described path is taked on average when interchanger operates.In usually operating, this direction is vertical direction.Fluid circulates vertically along path on average.Only when imagining interchanger with the difference orientation such as transporting or storing, this direction determined is no longer just vertical, but becomes any direction.If interchanger side down, then this direction is more or less level.
Liquid cycles through a part for the flat channel of the subset of the liquid reservation being formed as to be gasified usually downwards from top.Fluid is usual equally cycles through other path downwards from top, and this forms another subset.Generally speaking, the path for liquid or fluid is arranged alternately (alternate), to make heat exchange maximize.In principle, fluid cycles through whole path.
First liquid be allowed to enter the holding tray (in operation usually) be arranged in above interchanger body.The bottom of this dish is more or less orthogonal to the direction determined, is preferably orthogonal to the direction determined completely.Usually by various combination of elements being obtained described bottom in the mode of paving together: for the main distribution member to flat channel dispense liquid, its effect allows a certain amount of liquid, the in theory liquid of identical amount to enter each path (uniform distribution); Close the closure elements of the path for fluid reservation, such as rod.Demarcation strip also forms a part for these closure elements usually; Their top can form a part for the bottom of holding tray.
Secondary distribution element for liquid has the function of the liquid spreading the described amount of the path being allowed to enter first group across this whole path out.These paths are orthogonal to the normally very smooth rectangle in the cross section in the direction determined.Therefore, liquid stream must be spread out across this whole cross section.This realizes by using corrugated plating or fin.According to a specific embodiment, use and have and be orthogonal to flow direction and the corrugated plating along described flowing with the bus of partial offset, to obtain waterfall shape " champagne fountain " effect.
The path retained for fluid at least 80% but preferably 100% non-circumferential path in these paths (this means these paths 100% for fluid retain and between two paths retained for liquid) in be mounted with can anti-fluid at the device of the specific region Inner eycle of discussed path.This is forming so-called shadow region between the path closure elements and the device discussed of the side identical with holding tray.These devices plug fluid passing through in a certain direction.These devices also can be regarded as the second connector, and locking device is the first connector.It is interior between these two connectors that shadow region extends to considered path.
Shadow region is positioned at ad-hoc location.Its at least in part subtend be arranged in first group of two secondary distribution element for liquid closest to two paths of shadow region discussed.If the path of first group and second group is arranged alternately---this is from the most useful scheme of thermal viewpoint in theory, then these paths are positioned at two contiguous paths of path wherein.
What wording " at least in part subtend " meaned on the one hand shadow region is arranged in the At The Height identical with the part of of discussed secondary distribution element relative to the direction determined at least partially, and means that (not necessarily with a part) at least partially of shadow region is positioned at the At The Height identical with a part for another discussed secondary distribution element relative to the direction determined equally on the other hand.Mathematically, the intersection point between one in dead band projection in a certain direction and the secondary distribution element considered projection is in a certain direction non-zero.Another secondary distribution element of considering is like this equally.
Shadow region and the secondary distribution element that is used for liquid are positioned at identical At The Height by comprising by complete subtend on the direction determined (being generally vertical direction).Shadow region also can have the span of the span (extension) extended slightly beyond on the secondary distribution element in a certain direction and/or another meaning of liquid in a certain direction.
The advantage that shadow region provides is that their restrictions to prevent or confined liquid gasifies in these elements for the heat exchange at the secondary distribution element place of liquid.This has the effect of the secondary distribution improving liquid, and wherein other situations all keep identical.Improve insufficient distribution and reduce the risk of evaporate to dryness.If think distribute be desirable, then can shorten the length of secondary distribution element, or workability can lower and in theory should be more cheap material.
In addition, according to some specific embodiments, it is one or more that the present invention can have in following characteristics:
-described two secondary distribution elements have intended size on the described direction determined, described region extends along the described direction determined in the length being more than or equal to, being preferably substantially equal to the longest dimension in described intended size.In operation, this can obtain and better distribute and the whole structure of the heat exchange between liquid and fluid of can not excessively slowing down;
-be used for preventing described device that described fluid flows in described region to have the form of the metal rod being orthogonal to described assigned direction.This metal bar bar is the simplest device in theory;
-described the device that is used for preventing described fluid from flowing in described region is structurally identical with described closure elements.This is because use identical device to come on the one hand in liquid holding tray side and the path retained for fluid in fluid side blocking is on the other hand favourable;
-described region comprises at least one the mechanical wave card contacted with two in described plate, and described corrugated plating preferably has the bus on the described direction determined.This can provide larger mechanical strength in the scope of shadow region.
-interchanger comprises the secondary distribution element for described fluid, described secondary distribution element be arranged in described second group of path and can and be designed to described fluid to be assigned to each path of described second group;
-interchanger comprises outer wall, and described device can and be designed to establish be made up of the opening at least one in closure elements fluid connection;
-opening is positioned at the lower height place in described region;
-described secondary distribution element comprise have be orthogonal to the described direction determined bus, preferably at least one corrugated plating of the described direction upper part skew determined;
-be wear porose rod for the described main distribution member of described liquid.They are usually located between many demarcation strips and partly block liquid leads to the path of first group of path from holding tray.Orifice allowing liq passes through and can obtain the specific of liquid to spread out.According to a specified scheme, described in spread out across described path be uniform (in each path, the amount of liquid is substantially the same).
-interchanger also comprises the exchange corrugated plating of the bus preferably had on the described direction determined, described exchange corrugated plating is positioned at:
On the one hand, in each in the described path of described first group, the described secondary distribution element of the described path of described first group on the described direction determined between described exchange corrugated plating and described holding tray; And
On the other hand, in each in the described path of described second group, the described secondary distribution element of the described path of described second group on the described direction determined between described exchange corrugated plating and described closure elements.
According to a specific embodiment, shadow region has the length being more than or equal to, being preferably substantially equal to the length being positioned at the neighbouring secondary distribution element for liquid in a certain direction.Generally speaking, the whole secondary distribution elements for liquid are that similar and whole shadow region has equal length.
The invention still further relates to a kind of equipment for being separated air by distillation, this equipment at least comprises:
-the first destilling tower for operating under the pressure determined;
-after-fractionating tower for operating under the pressure lower than the described pressure determined; And
-heat exchanger, this heat exchanger can and be designed by with the Head gas of described first tower or air heat-exchange to make the tank liquid of described second tower vaporization at least partly;
The feature of described equipment is, described heat exchanger is heat exchanger as described above.
Accompanying drawing explanation
Other details and advantage become obvious by after reading the description provided referring to Fig. 1 and Fig. 2, Fig. 1 has illustrated the partial elevation view according to interchanger of the present invention in cross section, and Fig. 2 has illustrated the partial side view of the interchanger of the path across gas to be condensed in cross section.Dotted line represents that interchanger continues beyond these lines.
Detailed description of the invention
Interchanger 1 is made up of the assembly of parallel riser 3.They are parallel to the direction 11 determined, this direction 11 determined is by chance vertical at this.Be limited with between plate 3 is the flat channel 4 of liquid oxygen reservation and the path 5 for gaseous nitrogen reservation in a large number.Rod 6 partly blocks the top of path 4.Form is the top of the closure elements 9b blocking path 5 of rod.In type 4 and 5, the path of each is arranged alternately.All these is defined by outer wall 10.
Element 3,6 and 9b are formed and are used for the bottom 2a of holding tray 2 of receiving fluids.Rod 6 is designed to perform liquid to be mainly assigned to element in path 4.They have the hole 6a be evenly spaced apart allowing liquid to pass through.This liquid can be oxygen.
Then liquid flow through secondary distribution element 7a.Their effect spreads liquid out equably throughout relevant path 4.Liquid then along corrugated plating 8a as continuous film evaporation device.Liquid by with wall heat exchange and heated and evaporate gradually.
Element 7a is the corrugated plating with horizontal bus and straightened portion skew (zigzag coarse fashion (serratedhardway)).Element 8a is the corrugated plating with vertical bus, is preferably perforated.
Meanwhile, can be that the fluid of gaseous nitrogen arrives in interchanger via distribution corrugated plating (not shown), then flow downward along path 5.Meanwhile, gaseous nitrogen to the liquid oxygen heat radiation in adjacent path 4, to make oxygen evaporate, makes nitrogen condensation gradually simultaneously.Nitrogen, also through element 7b and 8b, is similar to element 7a and 8a of path 4.
In the path 5 of maximum quantity, in these paths at least 80% and preferably 100% non-circumferential path---namely it is between two paths 4, be provided with the device 9a identical with element 9b, its anti-fluid circulates in the region 14 of discussed path 5.This region is called shadow region.This region extends another from a plate 3 and extends to element 9b from device 9a.This region subtend is positioned at two element 7a of either side.Its length L on (vertically) direction 11 is slightly larger than the length of element 7a.
In the path 5 affected by shadow region 14, fluid is just introduced into below this region 14.When there is not dead band, fluid can be introduced into below closure elements 9b.
For the purpose of their structural intergrity, region 14 comprises the corrugated plating 12 of type identical with corrugated plating 8a or 8b.Their atmosphere is also arranged to contact with the reservoir of the gaseous oxygen of airdistillation unit, and liquid to be evaporated is also derived from described airdistillation unit via the opening 15 being positioned at interchanger either side.This can be avoided there is the mechanical stress caused by the pressure differential in region 14.
Fig. 2 is the cross section across the path retained for gas to be condensed such as gaseous nitrogen.Form is the top of the closure elements 9b blocking path of rod.In type 4 and 5, the path of each is arranged alternately.
All these is defined by outer wall 17.
Meanwhile, can be that the fluid of gaseous nitrogen arrives interchanger via distribution corrugated plating (not shown), then flow downward along path.Meanwhile, gaseous nitrogen to the liquid oxygen heat radiation in adjacent path 4, to make oxygen evaporate, makes nitrogen condensation gradually simultaneously.Nitrogen, also through element 7b and 8b, is similar to element 7a and 8a of path 4.
In the path 5 of maximum quantity, in these paths at least 80% and preferably 100% non-circumferential path---namely it is between two paths 4, be provided with the device 9a identical with element 9b, its anti-fluid circulates in the region 14 of discussed path 5.This region is called shadow region.This region extends another from a plate 3 and extends to element 9b from device 9a.This region subtend is positioned at two element 7a of the either side shown in Fig. 1 and two shown in subtend Fig. 2 closure elements 9c, 9d.Its length L on (vertically) direction 11 is slightly larger than the length of element 7a.
In the path affected by shadow region 14, fluid is just introduced into below this region 14.When there is not dead band, fluid can be introduced into below closure elements 9b.
For the purpose of their structural intergrity, region 14 comprises the corrugated plating 12 of type identical with corrugated plating 8a or 8b.Their atmosphere is also arranged to contact with the reservoir of gaseous oxygen of airdistillation unit from the bottom being generally lower pressure column, liquid to be evaporated is also derived from described airdistillation unit via the opening 15 being positioned at interchanger either side below element 9c, 9d, the element of described element 9c, 9d to be form be rod, in the vertical direction has the height being less than L.The height of element 9c, 9d from the scope of 60% to 90% of L, to allow gaseous oxygen to enter region 14.This can be avoided there is the mechanical stress caused by the pressure differential in the scope in region 14.
Claims (15)
1. one kind for by making the heat exchanger (1) of liquid gasification with fluid heat transfer, comprising:
-body, it comprises the assembly of the plate (3) being parallel to the direction (11) determined, a large amount of path (4 is limited with between described plate (3), 5), comprise for first group of path (4) of described liquid flow and second group of path (5) flowing for described fluid;
-be used for receiving the holding tray (2) of described liquid;
-main distribution member (6), it is for described liquid, can and be designed to described liquid to be assigned to described first group of path (4) from described holding tray (2); And
-be positioned at the side identical with described holding tray (2), the closure elements (9b) of each path (5) for closing described second group, with the secondary distribution element (7a) for described liquid being arranged in described first group of path (4), and this secondary distribution element (7a) can and be designed to described Liquid distribution in each path (4) of described first group, at least 80% of the path (5) of described second group comprises the device (9a) that can prevent described fluid from flowing in the region (14) of the described path (5) of described second group, described region (14) from described plate (3) extend in described plate (3) another and between described device (9a) and described closure elements (9b), in described region (14) each at least in part subtend belong in described first group closest to two in the described secondary distribution element (7a) of two paths (4) in described region (14) of discussing, the feature of described heat exchanger is, described heat exchanger comprise can and be designed to establish the device (15) that described region (14) is connected with the fluid between the gas container being positioned at described heat exchanger (1) outside, to allow the isostasy between described gas container and described region (14).
2. heat exchanger as claimed in claim 1, it is characterized in that, when described two secondary distribution elements (7a) have intended size on the described direction (11) determined, described region (14) extend along the described direction (11) determined in the length (L) being greater than or being substantially equal to the longest dimension in described intended size.
3. heat exchanger as claimed in claim 1 or 2, it is characterized in that, for the form preventing the described device (9a) of described fluid flowing in described region (14) to have the metal rod being orthogonal to described assigned direction (11).
4. heat exchanger as claimed in claim 1 or 2, it is characterized in that, the described device (9a) flowed in described region (14) for preventing described fluid is structurally identical with described closure elements (9b).
5. heat exchanger as claimed in claim 1 or 2, it is characterized in that, described region (14) comprise at least one the mechanical wave card (12) contacted with two in described plate (3).
6. heat exchanger as claimed in claim 1 or 2, it is characterized in that, described heat exchanger comprises outer wall (10,17), and described can and be designed to establish the device that fluid connects and be made up of the opening (15) at least one in described closure elements (9c, 9d).
7. heat exchanger as claimed in claim 6, wherein, described opening (15) is positioned at the lower height place in described region (14).
8. heat exchanger as claimed in claim 1 or 2, is characterized in that:
-described heat exchanger comprises the secondary distribution element (7b) for described fluid, described secondary distribution element (7b) be arranged in described second group of path (5) and can and be designed to described fluid to be assigned to each path (5) of described second group; And
-described secondary distribution element (7a, 7b) comprises at least one corrugated plating with the bus being orthogonal to the described direction (11) determined.
9. heat exchanger as claimed in claim 1 or 2, it is characterized in that, the described main distribution member (6) for described liquid is the rod wearing porose (6a).
10. heat exchanger as claimed in claim 1 or 2, is characterized in that, described heat exchanger also comprises exchange corrugated plating (8a, 8b), and described exchange corrugated plating (8a, 8b) is positioned at:
-on the one hand, in each in the described path (4) of described first group, the described secondary distribution element (7a) of the described path (4) of described first group is positioned between described exchange corrugated plating (8a) and described holding tray (2) on the described direction (11) determined; And
-on the other hand, in each in the described path (5) of described second group, the described secondary distribution element (7b) of the described path (5) of described second group is positioned between described exchange corrugated plating (8b) and described closure elements (9b) on the described direction (11) determined.
11. heat exchangers as claimed in claim 1, it is characterized in that, 100% of the non-circumferential path (5) of described second group comprises the device (9a) that can prevent described fluid from flowing in the region (14) of the described path (5) of described second group.
12. heat exchangers as claimed in claim 5, is characterized in that, described corrugated plating (12) has the bus on the described direction (11) determined.
13. heat exchangers as claimed in claim 8, is characterized in that, at least one corrugated plating described has the partial offset on the described direction (11) determined.
14. heat exchangers as claimed in claim 10, is characterized in that, described exchange corrugated plating (8a, 8b) has the bus on the described direction (11) determined.
15. 1 kinds, for being separated the equipment of air by distillation, are at least comprised:
-the first destilling tower for operating under the pressure determined;
-after-fractionating tower for operating under the pressure lower than the described pressure determined, it comprises or forms the gas container of gaseous oxygen; And
-heat exchanger, described heat exchanger can and be designed by with the Head gas of described first destilling tower or air heat-exchange to make the tank liquid of described after-fractionating tower vaporization at least partly;
The feature of described equipment is, described heat exchanger is the heat exchanger according to any one of claim 1 to 14.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1051662 | 2010-03-08 | ||
| FR1051662 | 2010-03-08 | ||
| PCT/FR2011/050471 WO2011110782A1 (en) | 2010-03-08 | 2011-03-07 | Heat exchanger |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102792116A CN102792116A (en) | 2012-11-21 |
| CN102792116B true CN102792116B (en) | 2015-04-08 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201180012905.5A Active CN102792116B (en) | 2010-03-08 | 2011-03-07 | Heat exchanger |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN102792116B (en) |
| WO (1) | WO2011110782A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102914204B (en) * | 2012-10-19 | 2014-12-24 | 中国海洋石油总公司 | Distributor and plate-fin heat exchanger with same |
| GB2527338B (en) * | 2014-06-19 | 2018-11-07 | ECONOTHERM UK Ltd | Heat transfer apparatus |
| FR3032521B1 (en) * | 2015-02-06 | 2017-02-17 | Air Liquide | HEAT EXCHANGER COMPRISING A REFRIGERANT LIQUID DISPENSING DEVICE |
| ES2837323T3 (en) * | 2018-01-25 | 2021-06-30 | Air Prod & Chem | Plate Fin Heat Exchanger Manifold |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0130122A1 (en) * | 1983-06-24 | 1985-01-02 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device for evaporating a liquid by heat exchange with a second fluid and air distillation unit comprising such a device |
| CN1165286A (en) * | 1996-03-18 | 1997-11-19 | 波克股份有限公司 | Heat exchanger |
| EP1099922A2 (en) * | 1999-11-09 | 2001-05-16 | Air Products And Chemicals, Inc. | Process for the production of intermediate pressure oxygen |
| US6338384B1 (en) * | 1998-10-05 | 2002-01-15 | Nippon Sanso Corporation | Downflow liquid film type condensation evaporator |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2786858B1 (en) * | 1998-12-07 | 2001-01-19 | Air Liquide | HEAT EXCHANGER |
-
2011
- 2011-03-07 CN CN201180012905.5A patent/CN102792116B/en active Active
- 2011-03-07 WO PCT/FR2011/050471 patent/WO2011110782A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0130122A1 (en) * | 1983-06-24 | 1985-01-02 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device for evaporating a liquid by heat exchange with a second fluid and air distillation unit comprising such a device |
| CN1165286A (en) * | 1996-03-18 | 1997-11-19 | 波克股份有限公司 | Heat exchanger |
| US6338384B1 (en) * | 1998-10-05 | 2002-01-15 | Nippon Sanso Corporation | Downflow liquid film type condensation evaporator |
| EP1099922A2 (en) * | 1999-11-09 | 2001-05-16 | Air Products And Chemicals, Inc. | Process for the production of intermediate pressure oxygen |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102792116A (en) | 2012-11-21 |
| WO2011110782A1 (en) | 2011-09-15 |
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