CN102792116A - Heat exchanger - Google Patents
Heat exchanger Download PDFInfo
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- CN102792116A CN102792116A CN2011800129055A CN201180012905A CN102792116A CN 102792116 A CN102792116 A CN 102792116A CN 2011800129055 A CN2011800129055 A CN 2011800129055A CN 201180012905 A CN201180012905 A CN 201180012905A CN 102792116 A CN102792116 A CN 102792116A
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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
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 through using the riser type heat exchanger and the second fluid heat exchange to make the liquid gasification.The present invention is particularly useful for air distillation installation.
Background technology
In the double tower type air distillation installation, the liquid oxygen in the jar of lower pressure column is through 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 operating pressure that the oxygen that certainly exists owing to the structure of heat exchanger and the temperature difference between the nitrogen have determined medium pressure column; Therefore, hope that this temperature difference is as far as possible little, so that make and compress the relevant expenditure of pending air that sprays in the medium pressure column and minimize.
The technology that is generally used for these phase transformation interchangers is the aluminium soldering plate fin type heat exchanger of the high compact member of the heat exchange area that can obtain to provide big.These interchangers are made up of plate, are inserted with corrugated plating (ondes) or fin between the said plate, thereby form folded gasification " path " and a condensation " path ".There are various corrugated platings, such as the corrugated plating (" Sawtooth waves card ") of straight corrugated plating, perforation corrugated plating or part skew.
Be in the situation of the gasifier that the falling liquid film mode is done that the part of equipment is used for distributing the liquid between the passage of gasification path and heat exchange corrugated plating.
This distribution to each gasifier is carried out according to the principle of describing among the document FR-A-2547898 usually: the gasification path is supplied to from the top of condensation pass.Oxygen passes through the delegation hole then, and said hole mainly distributes oxygen (first sub-distribution) in the gasification path.Flow through the then corrugated plating of a collection of horizontal bus of oxygen, its execution are called the distributing more accurately of secondary distribution (secondary distribution) (liquid being spread out in the path between the passage that is formed by corrugated plating).Gaseous nitrogen circulates in being parallel to " condensation " path of " gasification " path.Two kinds of fluids are in the total length cocycle of said path, so that make the thermo-contact maximization.
The liquid oxygen of gasification comprises the impurity that is dissolved form.Main impurity is nitrous oxide (N
2O), carbon dioxide (CO
2), hydrocarbon (C2, C3 etc.).Look operating conditions and decide, these impurity can be solid form or be liquid form and are deposited in the gasification path.On commercial scale, importantly control the formation of these solids or liquid precipitation thing, so that avoid any risk of explosion.
Every passage or every meter flow rate of liquid of treating wetting circumference are one of important parameters relevant with sedimentary formation.This be because, when the flow rate of liquid of every passage not high enough during with wetting wall, sediment by gasification to dry and form.
In this (film) gasifier, being distributed in its operation play an important role (performance and safety) of liquid oxygen.Therefore, need guarantee in all cases that liquid correctly is assigned in each passage.For this reason, liquid is distributed between the passage necessary full and uniform.Uneven liquid distributes the bad wetting of corrugated plating in the bottom that possibly cause interchanger especially, and therefore causes gasification to dry and form sediment.Difficulty is under the certain situation of the number of channels of every body and every path (550 passages/path, 55000 passages/body), to guarantee to keep in whole passages equal flow rate of liquid.
The quality that this liquid distributes depends on that the good design of distributor and good size confirm.
The main distribution of liquid (spreading out between path) obtains through the hole that is arranged in the liquid pool bottom that is positioned at the passage top through making liquid.The distribution (in each path, spreading out) that is called secondary distribution uses a collection of corrugated plating with horizontal bus and part skew to obtain usually.
Yet in final analysis, liquid is not in passage, to spread out all the time full and uniformly, and still has the risk of evaporate to dryness.
The problem that therefore, solve is to guarantee that liquid is assigned between the passage of and identical path better and reduces this risk.
Summary of the invention
For this reason, scheme of the present invention relates to a kind of being used for through making the heat exchanger of liquid gasification with the fluid heat exchange, and this heat exchanger comprises:
-body, it comprises the board component that is parallel to definite direction, is limited with a large amount of paths between the said plate, comprises first group of path, the second group path mobile with being used for said fluid that is used for said liquid flow;
-be used for receiving the holding tray of said liquid;
-main distribution member, it is used for said liquid, can and be designed to said liquid is assigned to said first group of path from said holding tray; And
-be positioned at a closure elements side, that be used to seal said second group each path identical with said holding tray; With the secondary distribution element that is used for said liquid that is arranged in said first group of path, and can and be designed to said liquid is assigned in each said first group path;
-said second group path at least 80%, 100% the comprising and can prevent said fluid mobile device in the zone of said second group said path of preferred said second group non-peripheral path; Said zone from said plate extend in the said plate another and between said device and said closure elements; In the said zone each all at least in part subtend belong in said first group near two in the said secondary distribution element of two paths in the said zone of being discussed; Said heat exchanger is characterised in that; Said heat exchanger comprises and can and be designed to establish the opening that said zone is connected with fluid between the gas container in the said interchanger outside, so that allow the isostasy between said reservoir and the said zone.
The damage that potential pressure differential between the each several part of the subtend shadow region location of the path that this can be avoided keeping owing to shadow region and for liquid causes.
In the situation of distillation, being used for balanced reservoir is the reservoir of gaseous oxygen.
Related liquid can belong to any kind.According to an embodiment, liquid oxygen produces from distillation.This oxygen is very pure usually.Fluid can belong to any kind.According to an embodiment, fluid is the nitrogen from distillation.Before heat exchange operation, fluid is gaseous state normally.Liquid is heated and becomes partially or completely and gasifies.Fluid cooling and partially or completely condensation.
Demarcation strip framework normally parallel and that form the interchanger body.Be limited with a plurality of smooth paths between the demarcation strip, because demarcation strip is in the direction of confirming or vertically and to be orthogonal on the direction of this direction be microscler.The direction that should confirm is the direction of when interchanger is operated, taking on average through the fluid of said path.In operating usually, this direction is a vertical direction.Fluid circulates along path on average vertically.Only imagining under the situation of interchangers that with the different orientations that for example are used to transport or store this direction of confirming just no longer is vertical, but becomes any direction.If the interchanger side down, then this direction more or less is a level.
Liquid cycles through the part of the straight path of the subclass that forms liquid reservation to be gasified usually downwards from the top.Fluid cycles through other path equally usually downwards from the top, this forms another subclass.Generally speaking, the path that is used for liquid or fluid is arranged alternately (alternate), so that make the heat exchange maximization.In principle, fluid cycles through whole paths.
Liquid at first is allowed to get into the holding tray (in operation usually) that is arranged in interchanger body top.The bottom of this dish more or less is orthogonal to definite direction, preferably is orthogonal to definite direction fully.Usually through with the mode of paving various combination of elements are obtained said bottom together: be used for the main distribution member to straight path dispense liquid, its effect is the permission certain amount of fluid, the liquid of same amount gets into each path (uniform distribution) in theory; Sealing is for the closure elements of the path of fluid reservation, such as rod.Demarcation strip also forms the part of these closure elements usually; Their top can constitute the part of the bottom of holding tray.
The secondary distribution element that is used for liquid has strides the function of liquid that this whole path is spread the said amount of the path that is allowed to get into first group out.These paths are orthogonal to the normally very smooth rectangle in cross section of definite direction.Therefore, flow must be striden this whole cross section and spread out.This realizes through using corrugated plating or fin.According to a specific embodiment, use to have to be orthogonal to the said mobile corrugated plating of flow direction and edge, so that obtain waterfall shape " champagne fountain " effect with bus of part skew.
The path that keeps for fluid at least 80% but preferably be mounted with in the 100% non-peripheral path in these paths (this means these paths 100% keep for fluid and between two paths) can prevent the device that fluid circulates in the specific region of the path of being discussed for the liquid reservation.This is forming so-called shadow region between the path closure elements of a side identical with holding tray and the device discussed.These devices have stopped up fluid passing through on the direction of confirming.These devices also can be regarded as second connector, and locking device is first connector.It is interior between these two connectors that shadow region extends to the path of being considered.
Shadow region is positioned at ad-hoc location.Its at least in part subtend be arranged in first group near two secondary distribution elements that are used for liquid of two paths of the shadow region of being 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, and then these paths are to be positioned at two contiguous paths of path wherein with shadow region.
At least a portion that wording " subtend at least in part " means on the one hand shadow region is arranged in one a part of identical height place with the secondary distribution element of being discussed with respect to the direction of confirming, is positioned at a part of identical height place with another secondary distribution element of being discussed and mean on the other hand that at least a portion (being not necessarily with a part) of shadow region is same with respect to definite direction.On mathematics, the projection of dead band on the direction of confirming is non-zero with a intersection point between the projection on definite direction in the secondary distribution element of being considered.Another secondary distribution element of being considered is like this equally.
Fully subtend will comprise shadow region and the secondary distribution element that is used for liquid will be positioned at the equal height place on the direction of confirming (being generally vertical direction).Shadow region also can be in the span that has the span (extension) on of extending beyond a little on the direction that the secondary distribution element that is used for liquid confirming and/or another meaning on the direction of confirming.
The advantage that shadow region provides is the heat exchange at their restrictions secondary distribution element place of being used for liquid and prevents or confined liquid gasifies at these elements.This has the effect of the secondary distribution of improving liquid, and wherein all other situation keep identical.Improve inadequate distribution and reduced the risk of evaporate to dryness.If think that it is desirable distributing, then can shorten the length of secondary distribution element, the material that perhaps workability can lower and in theory should be more cheap.
In addition, according to some specific embodiments, the present invention can have one or more in the following characteristic:
-said two secondary distribution elements have intended size on said definite direction, said zone more than or equal to, preferably be substantially equal to the said definite direction in the length upper edge of the longest dimension in the said intended size and extend.In operation, this can obtain better to distribute and the whole structure of the heat exchange between liquid and the fluid of can excessively not slowing down;
-be used for preventing that the said device that said fluid flows has the form of the metal rod that is orthogonal to said assigned direction in said zone.This metal bar bar is the most simply to install in theory;
-be used for preventing that the said device that said fluid flows is structurally identical with said closure elements in said zone.This is to be favourable because uses identical device to come on the one hand in liquid holding tray side and the path that stops up to the fluid reservation in fluid side on the other hand;
-said zone comprise with said plate in two at least one mechanical wave cards that contacts, said corrugated plating preferably has the bus on said definite direction.This can provide bigger mechanical strength in the scope of shadow region.
-interchanger comprises the secondary distribution element that is used for said fluid, and said secondary distribution element is arranged in said second group of path and can and be designed to said fluid is assigned to each said second group path;
-interchanger comprises outer wall, and said device can and be designed to establish the fluid of being made up of the opening in the closure elements at least one and connects;
-opening is positioned at the lower height place in said zone;
-said secondary distribution element comprise have the bus that is orthogonal to said definite direction, preferably at least one corrugated plating of said definite direction top skew;
-said main the distribution member that is used for said liquid is to wear porose rod.The path that they are usually located between many demarcation strips and partly block liquid is led to first group of path from holding tray.Orifice allowing liq through and can obtain the specific of liquid and spread out.According to a specified scheme, saidly spread that to stride said path be uniformly (amount of liquid is substantially the same in each path) out.
-interchanger also comprises the exchange corrugated plating that preferably has the bus on said definite direction, and said exchange corrugated plating is positioned at:
On the one hand, in each in the said first group said path, the said secondary distribution element of said first group said path on said definite direction between said exchange corrugated plating and said holding tray; And
On the other hand, in each in the said second group said path, the said secondary distribution element of said second group said path on said definite direction between said exchange corrugated plating and said closure elements.
According to a specific embodiment, shadow region has on the direction of confirming more than or equal near, the preferred length of the length of the secondary distribution element that is used for liquid being substantially equal to be positioned at.Generally speaking, the whole secondary distribution elements that are used for liquid be similar and all shadow regions have equal length.
The invention still further relates to a kind of equipment that is used for coming through distillation separation of air, this equipment comprises at least:
-be used for first destilling tower operated down at the pressure of confirming;
-be used for the after-fractionating tower of operation under the pressure that is lower than said definite pressure; And
-heat exchanger, this heat exchanger can and be designed to gasify at least in part through the jar liquid that head gas or air heat exchange with said first tower make said second tower;
Said equipment is characterised in that said heat exchanger is a heat exchanger as indicated above.
Description of drawings
Other details and advantage will become obvious after the description that provides that see figures.1.and.2 below the reading; Fig. 1 has illustrated the partial elevation view according to interchanger of the present invention in the cross section, Fig. 2 has illustrated the partial side view of the interchanger of the path of striding the gas of treating condensation in the cross section.Dotted line representes that the interchanger continuity surpasses these lines.
The specific embodiment
Interchanger 1 is made up of the assembly of parallel riser 3.They are parallel to definite direction 11, and this direction 11 of confirming by chance is vertical at this.Be limited with a large amount of straight paths 4 that keep for liquid oxygen between the plate 3 and be the path 5 of gaseous nitrogen reservation.Rod 6 partly stops up the top of path 4.Form is the top that the closure elements 9b of rod stops up path 5.The path of each is arranged alternately in the type 4 and 5.All these is defined by outer wall 10.
The liquid secondary distribution element 7a that flows through then.Their effect is to spread all over relevant path 4 to spread liquid equably out.Liquid flows as continuous falling liquid film along corrugated plating 8a then.Liquid is through being heated with the wall heat exchange and evaporation gradually.
Element 7a is the corrugated plating with horizontal bus and part offset of vertical (the coarse mode of zigzag (serrated hardway)).Element 8a is the corrugated plating with vertical bus, preferably is perforated.
Simultaneously, the fluid that can be gaseous nitrogen flows downward along path 5 via distributing the corrugated plating (not shown) to arrive in the interchanger then.Simultaneously, the gaseous nitrogen heat radiation of the liquid oxygen in adjacent path 4 gradually is so that the oxygen evaporation makes the nitrogen condensation simultaneously.Nitrogen also passes through element 7b and 8b, is similar to the element 7a and the 8a of path 4.
In the path 5 of maximum quantity, at least 80% in these paths and preferred 100% non-peripheral path---be its between two paths 4, be provided with the device 9a identical with element 9b, its anti-fluid circulates in the zone 14 of the path of being discussed 5.This zone is called shadow region.This zone is extended another and is extended to element 9b from device 9a from a plate 3.This zone 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 that influenced by shadow region 14 5, fluid just is introduced into below this zone 14.Under the situation that does not have the dead band, fluid can be introduced into below closure elements 9b.
For the purpose of their structural intergrity, zone 14 comprises the corrugated plating 12 with corrugated plating 8a or 8b same type.Their atmosphere also is arranged to contact with the reservoir of the gaseous oxygen of airdistillation unit, and liquid to be evaporated also is derived from said airdistillation unit via the opening that is positioned at the interchanger either side 15.This can be avoided existing the mechanical stress that is caused by the pressure differential in the zone 14.
Fig. 2 strides to be the gas of the treating condensation cross section of the path that keeps of gaseous nitrogen for example.Form is the top that the closure elements 9b of rod stops up path.The path of each is arranged alternately in the type 4 and 5.
All these is defined by outer wall 17.
Simultaneously, the fluid that can be gaseous nitrogen flows downward along path via distributing the corrugated plating (not shown) to arrive interchanger then.Simultaneously, the gaseous nitrogen heat radiation of the liquid oxygen in adjacent path 4 gradually is so that the oxygen evaporation makes the nitrogen condensation simultaneously.Nitrogen also passes through element 7b and 8b, is similar to the element 7a and the 8a of path 4.
In the path 5 of maximum quantity, at least 80% in these paths and preferred 100% non-peripheral path---be its between two paths 4, be provided with the device 9a identical with element 9b, its anti-fluid circulates in the zone 14 of the path of being discussed 5.This zone is called shadow region.This zone is extended another and is extended to element 9b from device 9a from a plate 3.This zone subtend is positioned at two the element 7a and subtend two closure elements 9c, the 9d shown in Figure 2 of either side shown in Figure 1.Its length L on (vertically) direction 11 is slightly larger than the length of element 7a.
In the path that influenced by shadow region 14, fluid just is introduced into below this zone 14.Under the situation that does not have the dead band, fluid can be introduced into below closure elements 9b.
For the purpose of their structural intergrity, zone 14 comprises the corrugated plating 12 with corrugated plating 8a or 8b same type.Their atmosphere also is arranged to contact with reservoir from the gaseous oxygen of the airdistillation unit of the bottom that is generally lower pressure column; Liquid to be evaporated also is derived from said airdistillation unit via the opening 15 that is positioned at the interchanger either side below element 9c, the 9d; Said element 9c, 9d are that form is the element of rod, and in the vertical direction has the height less than L.The height of element 9c, 9d is in 60% to 90% the scope of L, so that allow gaseous oxygen to get into zone 14.This can be avoided existing the mechanical stress that is caused by the pressure differential in the scope in zone 14.
Claims (11)
1. one kind is used for comprising through making the heat exchanger (1) of liquid gasification with the fluid heat exchange:
-body; It comprises the assembly of the plate (3) that is parallel to definite direction (11); Be limited with a large amount of paths (4,5) between the said plate (3), comprise the first group of path (4) that is used for said liquid flow and be used for second group of path (5) that said fluid flows;
-be used for receiving the holding tray (2) of said liquid;
-main distribution member (6), it is used for said liquid, can and be designed to said liquid is assigned to said first group of path (4) from said holding tray (2); And
-be positioned at closure elements (9b) side identical, that be used to seal said second group each path (5) with said holding tray (2); With the secondary distribution element (7a) that is used for said liquid that is arranged in said first group of path (4), and can and be designed to said liquid is assigned in said first group each path (4); Said second group path (5) at least 80%, 100% the comprising and can prevent said fluid mobile device (9a) the zone (14) of said second group said path (5) in of preferred said second group non-peripheral path (5); Said zone (14) from said plate (3) extend in the said plate (3) another and between said device (9a) and said closure elements (9b); In the said zone (14) each all at least in part subtend belong in said first group near two in the said secondary distribution element (7a) of two paths (4) in the said zone (14) of being discussed; Said heat exchanger is characterised in that; Said heat exchanger comprises the device (15) that the fluid between the gas container outside can and being designed to establish said zone (14) and be positioned at said interchanger (1) is connected, so that allow the isostasy between said reservoir and said zone (14).
2. interchanger as claimed in claim 1; It is characterized in that; Have under the situation of intended size on said definite direction (11) at said two secondary distribution elements (7a), is extending more than or equal to, length (L) the said definite direction in upper edge (11) that preferably is substantially equal to the longest dimension in the said intended size said zone (14).
3. like each described interchanger in the claim 1 and 2, it is characterized in that, be used for preventing that the said device (9a) that said fluid flows in said zone (14) has the form of the metal rod that is orthogonal to said assigned direction (11).
4. like each described interchanger in the claim 1 to 3, it is characterized in that, be used to prevent that the said device (9a) that said fluid flows is structurally identical with said closure elements (9b) in said zone (14).
5. like each described interchanger in the claim 1 to 4; It is characterized in that; Said zone (14) comprise with said plate (3) in two at least one mechanical wave cards (12) that contacts, said corrugated plating (12) preferably has the bus on said definite direction (11).
6. like each described interchanger in the claim 1 to 5; It is characterized in that said interchanger comprises outer wall (10,17); And said device can and be designed to establish, and (9c, the fluid that the opening (15) at least one in 9d) is formed connects by said closure elements.
7. interchanger as claimed in claim 6, wherein, said opening (15) is positioned at the lower height place in said zone (14).
8. like each described interchanger in the claim 1 to 7, it is characterized in that:
-said interchanger comprises the secondary distribution element (7b) that is used for said fluid, and said secondary distribution element (7b) is arranged in said second group of path (5) and can and be designed to said fluid is assigned to said second group each path (5); And
-said secondary distribution element (7a, 7b) comprise have the bus that is orthogonal to said definite direction (11), preferably at least one corrugated plating of said definite direction (11) top skew.
9. like each described interchanger in the claim 1 to 8, it is characterized in that the said main distribution member (6) that is used for said liquid is the rod that wears porose (6a).
10. like each described interchanger in the claim 1 to 9, it is characterized in that, said interchanger also comprise the exchange corrugated plating that preferably has the bus on said definite direction (11) (8a, 8b), said exchange corrugated plating (8a 8b) is positioned at:
-on the one hand; In in the said first group said path (4) each, the said secondary distribution element (7a) of said first group said path (4) is being positioned on said definite direction (11) between said exchange corrugated plating (8a) and the said holding tray (2); And
-on the other hand; In in the said second group said path (5) each, the said secondary distribution element (7b) of said second group said path (5) is being positioned on said definite direction (11) between said exchange corrugated plating (8b) and the said closure elements (9b).
11. an equipment that is used for coming through distillation separation of air comprises at least:
-be used for first destilling tower operated down at the pressure of confirming;
-being used for the after-fractionating tower of operation under the pressure that is lower than said definite pressure, it comprises or constitutes the reservoir of gaseous oxygen; And
-heat exchanger, said heat exchanger can and be designed to gasify at least in part through the jar liquid that head gas or air heat exchange with said first tower make said second tower;
Said equipment is characterised in that said heat exchanger is like each described heat exchanger in the claim 1 to 10.
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 true CN102792116A (en) | 2012-11-21 |
| CN102792116B CN102792116B (en) | 2015-04-08 |
Family
ID=43415362
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) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106415184A (en) * | 2014-06-19 | 2017-02-15 | 火石工程有限公司 | Heat transfer apparatus |
Families Citing this family (3)
| 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 |
| FR3032521B1 (en) * | 2015-02-06 | 2017-02-17 | Air Liquide | HEAT EXCHANGER COMPRISING A REFRIGERANT LIQUID DISPENSING DEVICE |
| EP3517878B1 (en) * | 2018-01-25 | 2020-11-04 | Air Products and Chemicals, Inc. | Distributor for plate-fin heat exchanger |
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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106415184A (en) * | 2014-06-19 | 2017-02-15 | 火石工程有限公司 | Heat transfer apparatus |
| CN106415184B (en) * | 2014-06-19 | 2019-11-05 | 火石工程有限公司 | Heat-transfer arrangement |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102792116B (en) | 2015-04-08 |
| WO2011110782A1 (en) | 2011-09-15 |
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