CN101258374A - Main condenser for cryogenic air separation system - Google Patents

Main condenser for cryogenic air separation system Download PDF

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Publication number
CN101258374A
CN101258374A CNA2006800323213A CN200680032321A CN101258374A CN 101258374 A CN101258374 A CN 101258374A CN A2006800323213 A CNA2006800323213 A CN A2006800323213A CN 200680032321 A CN200680032321 A CN 200680032321A CN 101258374 A CN101258374 A CN 101258374A
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CN
China
Prior art keywords
condenser
main condenser
pipe
liquid
steam
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CNA2006800323213A
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Chinese (zh)
Inventor
V·S·查克拉瓦蒂
M·J·洛克特
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Praxair Technology Inc
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Praxair Technology Inc
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Publication date
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Publication of CN101258374A publication Critical patent/CN101258374A/en
Pending legal-status Critical Current

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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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00—Tubular elements; Assemblies of tubular elements
    • F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/42—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00—Tubular elements; Assemblies of tubular elements
    • F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/42—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element
    • F28F1/422—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element with outside means integral with the tubular element and inside means integral with the tubular element
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/18—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by applying coatings, e.g. radiation-absorbing, radiation-reflecting; by surface treatment, e.g. polishing
    • F28F13/185—Heat-exchange surfaces provided with microstructures or with porous coatings
    • F28F13/187—Heat-exchange surfaces provided with microstructures or with porous coatings especially adapted for evaporator surfaces or condenser surfaces, e.g. with nucleation sites
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • 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
    • 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
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface

Abstract

The present invention provides a cryogenic air separation system having a main condenser (32) comprising a plurality of tubes having fluted external condensing surfaces upon which downf lowing nitrogen vapor (10) condenses, and having structured internal boiling surfaces upon which downf lowing oxygen liquid vaporizes. The main condenser (32) is employed as a condenser/reboiler located within a lower pressure column (31) to condense nitrogen vapor (10) from a higher pressure column (30) and partially vaporize oxygen liquid from the lower pressure column (31).

Description

The main condenser that is used for Cryognic air separation system
Technical field
Relate generally to Cryogenic air separation of the present invention, and more specifically relate to the Cryogenic air separation of using double tower.
Background technology
Use have the high pass buret simultaneously effectively the Cryognic air separation system of the main condenser that flows downward of operation may have one or more shortcomings.Shortcoming is relevant with porous coating expensive.In addition, any porous coating heterogeneous will cause the changes of properties of seething with excitement.
Summary of the invention
One aspect of the present invention is:
Be used to move the method for low temp air fractionation system, this low temp air fractionation system has high-pressure tower, lower pressure column and main condenser with a plurality of pipes, each of wherein said pipe has the outer surface and the structurized inner surface of trough of belt, described method comprises makes the nitrogen steam lead to the top part of main condenser from high-pressure tower, make oxygen liquid flow to the top part of the pipe of main condenser from the separating part of lower pressure column, make the nitrogen steam along main condenser downwards by and contact with the outer surface of pipe, the nitrogen steam that oxygen liquid is flowed downward along the Guan Yiyu of main condenser has heat exchanging relation to be passed through downwards, at least some of the oxygen liquid that wherein flows downward but not all evaporations, and oxygen steam and the oxygen liquid mass flow ratio with liquid in from 0.05 to 10 the scope and steam reclaimed from main condenser.
Another aspect of the present invention is:
Downflow condenser is suitable as the main condenser of column cryogenic air separation plant especially, and downflow condenser has a plurality of pipes, and each of wherein said pipe has the outer surface and the structurized inner surface of trough of belt.
As used herein, term " separating part " tower tray that meaned comprising of tower and/or filler and be positioned at the part of main condenser top.
As used herein, term " enhancing surface " means the particular surface geometry of the per unit surface area heat transfer that provides higher than general surface.
As used herein, term " tower " means distillation or fractionating column or district, be contact tower or district, wherein liquid contacts to realize separating of fluid mixture upstream with vapor phase mutually, for example by making vapor phase and liquid on the tower tray that vertically separate or column plate of series installation in tower, and/or on the packing component of for example structurized or at random filler, contact.The term double tower is used to mean that high-pressure tower makes its upper end become heat exchanging relation with the lower end of lower pressure column.
The contact separation process of steam and liquid depends on the difference of the vapour pressure of composition.High vapour pressure (more volatilization or lower boiling) composition will trend towards concentrating in the vapor phase, and low-vapor pressure (or more nonvolatile or high boiling) composition will trend towards concentrating on liquid mutually in.Partial condensation is separation process, and the cooling of steam mixture can be used for volatile ingredient (a plurality of composition) is concentrated in the vapor phase thus, and therefore more nonvolatile composition (a plurality of composition) is concentrated on liquid mutually in.Rectifying or continuous still are such separation processes, and it will be as part evaporation in succession and the condensation combination that obtains mutually by countercurrent treatment vapor phase and liquid.Vapor phase generally is adiabatic with liquid counter current contacting mutually, and can comprise two integration (classification) contact or differential (continuously) contacts between the phase.Utilize the rectifying principle to come the separation process device of separating mixture often to be called rectifying column, destilling tower or fractionating column interchangeably.Cryogenic rectification is the distillation process that carries out in 150 degree Kelvins (K) or following temperature at least in part.
Description of drawings
Fig. 1 is the simplification representative schematic diagram of a preferred embodiment of Cryognic air separation system of the present invention.
Fig. 2 is the phantom of an embodiment of two reinforced pipes, and this pipe can use in practice of the present invention.
Each illustrates the preferred construction boiling surface with the side view that highly amplifies Fig. 3 and Fig. 4, and this boiling surface can be used as the inner surface of the pipe of the main condenser that flows downward in practice of the present invention.At present, on the commercial outer surface that is manufactured on pipe in these surfaces.
The specific embodiment
The present invention includes the heat exchanger of the novelty that defines two reinforced pipe surfaces and in column cryogenic air separation plant, be used as main condenser.Pipe is characterised in that to have the boiling surface of enhancing and strengthen condensing surface.Strengthen condensing surface and comprise groove to small part for length of tube.Strengthening boiling surface is patterned surface.The structuring boiling surface is the enhancing boiling surface that is processed to form by metal, and being formed into nuclear location on heat exchange surface, heat exchange surface is characterised in that a plurality of chambeies of the boiling of low wall under overheated of having caught steam and initialization.
The present invention will be described with reference to the accompanying drawings more completely.With reference now to Fig. 1,, there is shown the part schematic diagram of column cryogenic air separation plant, column cryogenic air separation plant has high-pressure tower 30 and lower pressure column 31, and there is shown the placement of main condenser 32 in lower pressure column that is also referred to as condenser/reboiler.Main condenser of the present invention (a plurality of main condenser) can be the heat exchanger of shell-and-tube type, or the aluminium heater type of brazing.Main condenser/reboiler connects high-pressure tower and lower pressure column heat.The nitrogen steam that usually has the pressure in from 45 to 300 pound per square inch absolute pressure (psia) scopes leads to the top part of main condenser or a plurality of main condensers from high-pressure tower 30 in pipeline 10, wherein when nitrogen steam and two fluids of oxygen liquid are downward through main condenser (a plurality of main condenser), the oxygen liquid heat exchange in nitrogen steam and the pipe.The oxygen liquid that usually has the pressure in from 1 to 100 pound per square inch gage (psig) scope partly evaporates and consequent oxygen steam and remaining oxygen liquid reclaim from main condenser (a plurality of main condenser), as illustrating with flow arrow 34 and 33 respectively.The nitrogen steam since flow downward by main condenser condensation fully and consequent nitrogen liquid pipeline 11 in from the main condenser recovery, and when being back to high-pressure tower and lower pressure column, in pipeline 35 and 36, pass through respectively.
In lower pressure column 31, be collected in the collector/distributor 13 along the oxygen liquid of tower decline by filler 12 or tower tray (not shown).The rising head 14 of opening extends upward from the bottom surface of collector box, and the oxygen steam that generates in main condenser is upwards flowed by tower.Flow through distributor tube 15 and be collected in the dispenser portion 16 of independent module from the oxygen liquid of gatherer.Oxygen liquid from the flow distributor part flows through independent pipe, and it partly evaporates herein.These passages have the boiling surface of enhancing, promptly structurized inner surface, and this ability and having reduced that has increased the surface of the moistening boiling side of liquid significantly realizes the amount of moistening required liquid flow.Unevaporated liquid 17 is collected in the bottom of tower and reclaims from tower as product in pipeline 38.Product boiler pump 18 is used to raise the pressure of oxygen to the product pressure of wishing.If wish, then flowing 38 part 40 can and be recycled to main condenser (a plurality of main condenser) by valve 41.In the scope from 0.05 to 10 of the mass flow ratio (L/V) of the exit of main condenser tubes or evaporation channel liquid and steam, and preferably in from 0.2 to 2.0 scope.
Each condenser/reboiler 32 comprises the pipe of a plurality of portrait orientations, is under the heat exchanger situation of shell-and-tube type at main condenser, and the pipe of portrait orientation uses usually and is attached to top tube sheet and bottom tube sheet.Tube sheet is not shown in Fig. 1.Each pipe has inner surface and outer surface.The outer surface trough of belt of each pipe, promptly it has the groove of a plurality of length along pipe (preferably on whole length) trend, to strengthen condensing heat-exchange.The nitrogen steam is downward through pipe and condensation, preferably total condensation when the length of its process pipe.Consequent condensate, promptly nitrogen liquid reclaims from the outlet at bottom of shell-side.Nitrogen liquid leads to outside the condenser/boilers 32 in pipeline 11, and feeds in the top part of high-pressure tower, and also feeds in the top part of lower pressure column to carry out cryogenic rectification as withdrawing fluid.Be to simplify, in Fig. 1, only show from condenser/reboiler 32 to pipeline one of connection of 11.If wish, then the part of nitrogen liquid can be used as product nitrogen and fetches.
The inner surface of each pipe has boiling surface enhancing or structurized, it is characterized in that a plurality of chambeies or depression, and their degree of depth is usually in from 0.5 to 2.0 millimeter scope.Two examples in such chamber illustrate with the cross section in Fig. 3 and Fig. 4.The boiling surface of enhancing that has recessed chamber is by moving at chamber IT steam, the boiling with the low tube wall of initialization under overheated, and tube wall is overheated to be defined as temperature contrast between the saturation temperature of tube wall surface temperature and fluid to be evaporated.Oxygen liquid along the inner surface of pipe flow downward and with the aforesaid condensation that flows downward in nitrogen steam indirect heat exchange in the same way.When oxygen liquid when the enhancing of pipe boiling inner surface flows downward, the part boiling or the evaporation of the oxygen liquid that flows downward, as in Fig. 1, illustrating, and in Fig. 1, be collected in the storage pond of upper column, as illustrating with liquid cell 17 with the remaining liquid shown in the arrow L by arrow G.From the oxygen steam of the inner surface of pipe boiling as steam upwards stream make progress mobile to be used for cryogenic rectification by upper column.If wish that the part of oxygen steam can be used as the product gaseous oxygen and fetches.If wish that the part of remaining oxygen liquid 17 can be used as product liquid oxygen and fetches.Alternatively, remaining oxygen liquid 17 is recycled to pipe, keeps moistening with the boiling surface that guarantees pipe, has therefore avoided being boiled to drying regime, and drying regime is invalid and also is dangerous when liquid comprises liquid oxygen.Be recirculation flow, oxygen liquid 17 is from upper column 31 recovery and by liquid recirculation pump 18 pumpings.
Typically, in practice of the present invention, pipe will have the internal diameter in from 15 to 25 millimeters scope.Fig. 2 illustrates two reinforced pipes to use with the present invention, and this pair reinforced pipe has the outer surface 45 and the structurized inner surface 46 of trough of belt.Condenser will typically comprise from about 300 to 800 such pipes.Condenser also can comprise one or more other pipes that do not have so two features that strengthen the surface.Fig. 3 and Fig. 4 show the side view of two exemplary embodiments of the structuring boiling surface that uses with the present invention.The surperficial commercial GEWA surface that is known as shown in Figure 3.The shape in chamber is called concave-concave and goes into the chamber and catch steam very effectively.Surface shown in Figure 4 is typical Wolverine Turbo-B TMPipe.Fin at first forms from the teeth outwards and they are revised to provide the desirable shape in chamber by cold working.
Though the present invention describes in detail with reference to certain preferred embodiment, one of ordinary skill in the art will appreciate that to have other embodiment of the present invention in the spirit and scope of claims.

Claims (9)

1. method that is used to move low temp air fractionation system, this low temp air fractionation system has high-pressure tower, lower pressure column and main condenser with a plurality of pipes, each of wherein said pipe has the outer surface and the structurized inner surface of trough of belt, described method comprises makes the nitrogen steam lead to the top part of main condenser from high-pressure tower, make oxygen liquid flow to the top part of the pipe of main condenser from the separating part of lower pressure column, make the nitrogen steam along main condenser downwards by and contact with the outer surface of pipe, the nitrogen steam that oxygen liquid is flowed downward along the Guan Yiyu of main condenser has heat exchanging relation to be passed through downwards, at least some of the oxygen liquid that wherein flows downward but not all evaporations, and oxygen steam and the oxygen liquid mass flow ratio with liquid in from 0.05 to 10 the scope and steam reclaimed from main condenser.
2. method according to claim 1, wherein the mass flow ratio of liquid and steam is in from 0.2 to 2.0 scope.
3. method according to claim 1, wherein main condenser is the shell-and-tube heat exchanger.
4. method according to claim 1, wherein main condenser is the aluminium heater of brazing.
5. method according to claim 1, wherein main condenser comprises a plurality of condenser module.
6. downflow condenser is suitable as the main condenser of column cryogenic air separation plant especially, and downflow condenser has a plurality of pipes, and each of wherein said pipe has the outer surface and the structurized inner surface of trough of belt.
7. condenser according to claim 6 has from 300 to 800 pipes.
8. condenser according to claim 6, wherein structurized inner surface have the chamber of the degree of depth in from 0.5 to 2.0 millimeter scope.
9. condenser according to claim 6, wherein the internal diameter of pipe is in from 15 to 25 millimeters scope.
CNA2006800323213A 2005-08-04 2006-08-02 Main condenser for cryogenic air separation system Pending CN101258374A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US11/196,405 US20070028649A1 (en) 2005-08-04 2005-08-04 Cryogenic air separation main condenser system with enhanced boiling and condensing surfaces
US11/196,405 2005-08-04

Publications (1)

Publication Number Publication Date
CN101258374A true CN101258374A (en) 2008-09-03

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US (1) US20070028649A1 (en)
EP (1) EP1929228A2 (en)
CN (1) CN101258374A (en)
BR (1) BRPI0614531A2 (en)
WO (1) WO2007019299A2 (en)

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BRPI0614531A2 (en) 2016-11-08
EP1929228A2 (en) 2008-06-11
WO2007019299A3 (en) 2007-11-08
US20070028649A1 (en) 2007-02-08
WO2007019299A2 (en) 2007-02-15

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