FI81967B - OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. - Google Patents
OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. Download PDFInfo
- Publication number
- FI81967B FI81967B FI885530A FI885530A FI81967B FI 81967 B FI81967 B FI 81967B FI 885530 A FI885530 A FI 885530A FI 885530 A FI885530 A FI 885530A FI 81967 B FI81967 B FI 81967B
- Authority
- FI
- Finland
- Prior art keywords
- steam
- condenser
- gases
- condensed
- absorber
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0093—Removing and treatment of non condensable gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/263—Drying gases or vapours by absorption
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Sorption Type Refrigeration Machines (AREA)
Description
1 819671 81967
Menetelmä ja laite tiivistymättömien kaasujen erottamiseksi höyrystä.Method and apparatus for separating uncondensed gases from steam.
Tämä keksintö kohdistuu menetelmään ja laitteeseen erottaa 5 tiivistymättömiä kaasuja höyrystä isotermisen absorption avulla. Sen avulla voidaan tehostaa lauhduttimen ilmanpois-toa ja pienentää siihen tarvittavaa pumppausenergiaa.This invention relates to a method and apparatus for separating uncondensed gases from steam by isothermal absorption. It can be used to increase the efficiency of the condenser deaeration and to reduce the pumping energy required for it.
Tiivistymättömien kaasujen poistaminen lauhtuvasta höyrystä 10 on keskeinen ongelma kaikissa höyryä käsittelevissä prosesseissa. Yleisin tämän tyyppinen ongelma on vuotoilman poistaminen lauhdevoimalan lauhduttimesta. Vastaavasti meriveden tislauslaitoksissa veteen liuenneen ilman poistaminen on prosessin toimivuuden edellytys. Tämän ongelman 15 merkitys kasvaa sitä mukaa, mitä alemmassa paineessa höyryä lauhdutetaan.The removal of uncondensed gases from the condensing steam 10 is a key problem in all steam handling processes. The most common problem of this type is the removal of leaking air from the condenser of a condensing power plant. Similarly, in seawater distilleries, the removal of dissolved air is a prerequisite for the process to work. The importance of this problem 15 increases as the steam is condensed at a lower pressure.
Höyryn mukana lauhduttimeen kulkeutuvat tiivistymättömät kaasut voidaan tunnetusti erottaa höyrystä siten, että 20 höyryn ja näiden kaasujen seosta jäähdytetään. Tällöin höyryn paine laskee ja vastaavasti tiivistymättömien kaasujen osapaine kohoaa. Tällä tavoin höyryn osuus seoksessa saadaan vähenemään, mikä puolestaan pienentää ilmanpois-ton yhteydessä alipaineesta pois pumpattavan kaasun koko-25 naismäärää.It is known that the non-condensing gases entrained in the condenser with the steam can be separated from the steam by cooling the mixture of steam and these gases. In this case, the vapor pressure decreases and the partial pressure of the non-condensing gases increases accordingly. In this way, the proportion of steam in the mixture is reduced, which in turn reduces the total amount of gas pumped out of the vacuum during deaeration.
Höyryn jäähdyttäminen edellyttää varsin huolellista lauhduttimen suunnittelua, jotta kaasuseoksen virtausnopeus pysyisi koko ajan riittävänä tiivistymättömien kaasujen akkumuloitu-30 misen estämiseksi ja toisaalta virtaushäviöt pysyisivät riittävän pieninä. Jos esimerkiksi kaasuseosta jäähdytetään 2°C lämpötilasta 25 °C, laskee höyryn paine arvosta 31.7 mbar arvoon 28.1 mbar. Jos kokonaispaine alenee samalla virtaushäviöiden johdosta 1 mbar, on tiivistymättömien 35 kaasujen osapaine 2.6 mbar. Tiivistymättömien kaasujen mukana joudutaan tällöin poistamaan yli kymmenkertainen tilavuusvirta höyryä.Cooling the steam requires a very careful design of the condenser so that the flow rate of the gas mixture remains sufficient at all times to prevent the accumulation of uncondensed gases and, on the other hand, the flow losses remain sufficiently low. For example, if the gas mixture is cooled from 2 ° C to 25 ° C, the vapor pressure drops from 31.7 mbar to 28.1 mbar. If at the same time the total pressure decreases by 1 mbar due to flow losses, the partial pressure of the non-condensed gases is 2.6 mbar. Uncondensed gases then have to remove more than ten times the volume flow of steam.
2 819672,81967
Keksinnön mukaan tiivistymättömien kaasujen osapainetta voidaan korottaa isotermisen absorption avulla. Lauhdutti-mesta poistuva kaasuseos voidaan johtaa kontaktiin absorp-tioväliaineen kanssa, jossa väliaineessa höyryn paine on 5 pieni verrattuna höyryn paineeseen kaasuseoksessa. Tällaisia absorptioväliaineita voivat olla monien hyvin liukoisten suolojen vesiliuokset, kuten esimerkiksi natriumhydroksidin, litiumbromidin, litiumkloridin, kalsiumkloridin, kaliumkarbonaatin ja kaliumasetaatin. Kaasuseoksesta absorboituu 10 tällöin höyryä tällaiseen absorptioväliaineeseen ja tiivistymättömien kaasujen osOapaine vastaavasti kasvaa. Kun tiivistymättömät kaasut poistetaan tästä tilasta, joudutaan niiden mukana pumppaamaan alipaineesta vain vähäinen höyrymäärä.According to the invention, the partial pressure of the non-condensing gases can be increased by means of isothermal absorption. The gas mixture leaving the condenser can be brought into contact with an absorption medium in which the vapor pressure is low compared to the vapor pressure in the gas mixture. Such absorption media may include aqueous solutions of many highly soluble salts, such as sodium hydroxide, lithium bromide, lithium chloride, calcium chloride, potassium carbonate, and potassium acetate. Steam is then absorbed from the gas mixture into such an absorption medium and the partial pressure of the uncondensed gases increases accordingly. When uncondensed gases are removed from this space, only a small amount of steam has to be pumped from the vacuum with them.
15 Höyryn absorboituessa liuokseen se luovuttaa tälle absorp-tiolämpönsä, jolloin liuoksen lämpötila pyrkii kohoamaan ja vastaavasti sen höyrynpaine kasvamaan. Tämän estämiseksi absorptioväliainetta jäähdytetään epäsuorassa lämmönvaihdos-20 sa jäähdytysaineen, esimerkiksi jäähdytysveden kanssa, kuten tehdään absorptiolämpöpumpun absorbaattorissa. Tällöin höyryn absorptio tapahtuu olennaisesti isotermisesti ja liuoksen höyrynpaine pysyy matalana.As the steam is absorbed into the solution, it transfers to it its absorption heat, whereby the temperature of the solution tends to rise and its vapor pressure increases accordingly. To prevent this, the absorption medium is cooled in an indirect heat exchange with a coolant, for example cooling water, as is done in the absorber of an absorption heat pump. In this case, the vapor absorption takes place substantially isothermally and the vapor pressure of the solution remains low.
25 Jos esimerkiksi absorptioväliaineena on 30-prosenttinen natriumhydroksidiliuos lämpötilassa 25°C, on sen höyrynpaine n. 14 mbar. Kun tähän liuokseen absorboidaan vesihöyryä samassa lämpötilassa 25 °C ja oletetaan virtaushäviöksi sama 1 mbar kuin edellisessä esimerkisssä, nousee tiivisty-30 mättömien kaasujen osapaine arvoon 16.7 mbar. Tiivistymättömien kaasujen mukana joudutaan tällöin poistamaan vain 0.8-kertainen tilavuusvirta höyryä.For example, if the absorption medium is a 30% sodium hydroxide solution at 25 ° C, its vapor pressure is about 14 mbar. When water vapor is absorbed into this solution at the same temperature of 25 ° C and the flow loss is assumed to be the same 1 mbar as in the previous example, the partial pressure of the non-condensed gases rises to 16.7 mbar. With non-condensed gases, only 0.8 times the volume flow of steam has to be removed.
Absorptioväliaine laimenee höyryn absorboituessa siihen. 35 Se konsentroidaan höyrystämällä tästä absorptioväliaineesta vastaava määrä höyryä hieman korkeammassa lämpötilassa, samaan tapaan kuin absorptiolämpöpumpun höyrygeneraattoris-sa. Vapautuva höyry voidaan lauhduttaa erillisessä lauhdut- 3 81967 timessa. Lämpötila voidaan myös sovittaa siten, että vapautuvan höyryn paine on sama, kuin alkuperäisen absorboidun höyryn, jolloin tämä uudelleen höyrystetty höyry voidaan lauhduttaa samassa lauhduttimessa, josta höyryn ja 5 tiivistymättömien kaasujen seos poistettiin.The absorption medium dilutes as steam is absorbed therein. 35 It is concentrated by evaporating an equivalent amount of steam from this absorption medium at a slightly higher temperature, in the same way as in the steam generator of an absorption heat pump. The released steam can be condensed in a separate condenser. The temperature can also be adjusted so that the pressure of the released steam is the same as that of the original absorbed steam, whereby this re-vaporized steam can be condensed in the same condenser from which the mixture of steam and non-condensed gases was removed.
Jotta höyryllä ja absorptioväliaineella olisi riittävä lämmön- ja aineensiirtopinta ja toisaalta absorptioväliai-neen jäähdytys ja lämmitys tapahtuisi tehokkaasti, voidaan 10 sekä absorbaattori että generaattori käytännössä rakentaa vaakasuorista tuubeista, joiden ulkopinnalla absorptioväli-aine ohuena kalvona virtaa.In order for the steam and the absorption medium to have a sufficient heat and mass transfer surface and on the other hand for efficient cooling and heating of the absorption medium, both the absorber and the generator can in practice be constructed of horizontal tubes on the outer surface of which the absorption medium flows as a thin film.
Claims (4)
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FI885530A FI81967C (en) | 1988-11-29 | 1988-11-29 | OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. |
EP89912819A EP0446229A1 (en) | 1988-11-29 | 1989-11-22 | Method and apparatus for separating non-condensable gases from vapor |
PCT/FI1989/000214 WO1990006163A1 (en) | 1988-11-29 | 1989-11-22 | Method and apparatus for separating non-condensable gases from vapor |
AU46213/89A AU4621389A (en) | 1988-11-29 | 1989-11-22 | Method and apparatus for separating non-condensable gases from vapor |
CA002004032A CA2004032A1 (en) | 1988-11-29 | 1989-11-28 | Method and apparatus for separating non-condensable gases from vapor |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FI885530 | 1988-11-29 | ||
FI885530A FI81967C (en) | 1988-11-29 | 1988-11-29 | OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. |
Publications (4)
Publication Number | Publication Date |
---|---|
FI885530A0 FI885530A0 (en) | 1988-11-29 |
FI885530A FI885530A (en) | 1990-05-30 |
FI81967B true FI81967B (en) | 1990-09-28 |
FI81967C FI81967C (en) | 1991-01-10 |
Family
ID=8527485
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
FI885530A FI81967C (en) | 1988-11-29 | 1988-11-29 | OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP0446229A1 (en) |
AU (1) | AU4621389A (en) |
CA (1) | CA2004032A1 (en) |
FI (1) | FI81967C (en) |
WO (1) | WO1990006163A1 (en) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FI100506B (en) * | 1991-10-16 | 1997-12-31 | Kh Innovations Oy | Separation and concentration method based on selective absorption |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
SE313293B (en) * | 1966-07-28 | 1969-08-11 | S Bogatykh | |
SE459716B (en) * | 1987-11-20 | 1989-07-31 | Lars Gunnar Hellman | PROCEDURES FOR CONDITIONING OF HUMID GAS |
-
1988
- 1988-11-29 FI FI885530A patent/FI81967C/en not_active IP Right Cessation
-
1989
- 1989-11-22 EP EP89912819A patent/EP0446229A1/en not_active Withdrawn
- 1989-11-22 AU AU46213/89A patent/AU4621389A/en not_active Abandoned
- 1989-11-22 WO PCT/FI1989/000214 patent/WO1990006163A1/en not_active Application Discontinuation
- 1989-11-28 CA CA002004032A patent/CA2004032A1/en not_active Abandoned
Also Published As
Publication number | Publication date |
---|---|
FI885530A0 (en) | 1988-11-29 |
CA2004032A1 (en) | 1990-05-29 |
AU4621389A (en) | 1990-06-26 |
FI885530A (en) | 1990-05-30 |
FI81967C (en) | 1991-01-10 |
EP0446229A1 (en) | 1991-09-18 |
WO1990006163A1 (en) | 1990-06-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6076369A (en) | Evaporative concentration apparatus for waste water | |
US4963231A (en) | Method for evaporation of liquids | |
US4195485A (en) | Distillation/absorption engine | |
US4467623A (en) | Counterflow absorber for an absorption refrigeration system | |
US4860548A (en) | Air conditioning process and apparatus therefor | |
US6212890B1 (en) | Geothermal power plant and condenser therefor | |
FI81967C (en) | OVER ANALYZING FOR SEPARATION OF OAKING CONDITIONERS GASER AND AONGA. | |
JPH04505880A (en) | two stage condenser | |
FR2351681A1 (en) | Single stage evaporator for concentrating solns - operates with refrigerant as heating gas is suitable esp. for small units | |
US4615177A (en) | Solution heat pump apparatus and method | |
EP0200782A1 (en) | Solution heat pump apparatus and method | |
US5628190A (en) | Geothermal power plant and condenser therefor | |
KR940011907A (en) | Refrigerant Gas Injection Air Cooling Absorption System | |
CN113357660B (en) | Cooling and heating system based on plume elimination and waste heat recovery of gas boiler flue gas | |
CN115608118B (en) | Composite absorption tower and absorption type carbon capture pressure increasing system and process | |
JPH07198222A (en) | Heat pump including reverse rectifying part | |
JPS6321284Y2 (en) | ||
JPH0148203B2 (en) | ||
JPH09112214A (en) | Power generating system | |
JPS57127484A (en) | Vacuum distillation device | |
RU2086875C1 (en) | Method of contactless transfer of heat | |
JPS5820679B2 (en) | watermelon watermelon | |
JPS5858384B2 (en) | Absorption heat pump | |
SU1041837A1 (en) | Drying plant | |
SU1038607A1 (en) | Compression plant |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
MM | Patent lapsed |
Owner name: INVENTIO OY |