EP0061031B1 - Procédé de production de vapeur - Google Patents

Procédé de production de vapeur Download PDF

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Publication number
EP0061031B1
EP0061031B1 EP82101632A EP82101632A EP0061031B1 EP 0061031 B1 EP0061031 B1 EP 0061031B1 EP 82101632 A EP82101632 A EP 82101632A EP 82101632 A EP82101632 A EP 82101632A EP 0061031 B1 EP0061031 B1 EP 0061031B1
Authority
EP
European Patent Office
Prior art keywords
steam
pressure
bar
process according
compressed
Prior art date
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.)
Expired
Application number
EP82101632A
Other languages
German (de)
English (en)
Other versions
EP0061031A1 (fr
Inventor
Gerhard Dipl.-Ing. Link
Siegfried Dipl.-Ing. Jung
Reinhold Zapp
Helmut Dipl.-Ing. Bär
Herbert Ing. Grad. Mader
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Ticona Polymerwerke GmbH
Original Assignee
Uhde GmbH
Ticona Polymerwerke GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=6127619&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0061031(B1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Uhde GmbH, Ticona Polymerwerke GmbH filed Critical Uhde GmbH
Priority to AT82101632T priority Critical patent/ATE8174T1/de
Publication of EP0061031A1 publication Critical patent/EP0061031A1/fr
Application granted granted Critical
Publication of EP0061031B1 publication Critical patent/EP0061031B1/fr
Expired legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
    • F22B3/04—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass by drop in pressure of high-pressure hot water within pressure- reducing chambers, e.g. in accumulators
    • F22B3/045—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass by drop in pressure of high-pressure hot water within pressure- reducing chambers, e.g. in accumulators the drop in pressure being achieved by compressors, e.g. with steam jet pumps
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/16—Combination
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/21—Acrylic acid or ester

Definitions

  • the invention relates to a method for generating steam from 3.0 to 6.0 bar and from 140 ° C to 165 ° C from liquid heat transfer media of low temperature level by evaporation and compression.
  • a medium pressure level of approx. 15 to 25 bar and a low pressure level of 3 to 6 bar there is usually a medium pressure level of approx. 15 to 25 bar and a low pressure level of 3 to 6 bar.
  • Steam from the medium pressure stage can be used, among other things, as heating steam for the temperature range around 200 ° C, as motive steam for steam jet compressors or as drive steam for process steam turbines.
  • Steam of the low pressure level is generally only used as heating steam. Its pressure of 3 to 6 bar and its temperature, slightly above the saturated steam temperature, still allow it to be transported and used over long distances. If for some reason there is not enough low pressure steam available, you are forced.
  • Reduce steam from the medium pressure network to the pressure of the low pressure steam network by means of throttling devices and possibly inject condensate for steam cooling or for saturation. In this way, inevitably high quality energy, i. H. Steam with high thermodynamic quality, economically reduced.
  • EP-A-5 825 a process for the continuous generation of heating energy, cooling capacity and pure water from an available aqueous supply medium is known.
  • the supply medium usually water with z. B. ambient temperature
  • the steam jet pumps work with the same motive steam pressure, with graduated suction pressure and at the same compression end pressure, i.e. H. with increasing compression ratio.
  • the steam generated in this way with the final compression pressure of the steam jet pumps is compressed by means of a mechanical compressor at least up to the motive steam pressure of the steam jet.
  • the mechanical compressor must not only compress the steam generated from the supply medium but also the propellant steam, i. H. the output is inevitably increased considerably, and the motive steam is constantly circulated with considerable energy input.
  • the reference to a supply medium with increased temperature ie higher than ambient temperature, it is sometimes not necessary to connect a steam jet upstream of the mechanical compressor.
  • the system consists of partially thermodynamic and mechanical compression. Again, the mechanical compressor must compress the steam generated and the amount of motive steam. The motive steam is in turn circulated.
  • the invention is based on the object of eliminating the existing disadvantages of generating steam from 3.0 to 6.0 bar in chemical process plants and at the same time bringing resulting vapor of low thermodynamic quality to a higher energy level.
  • the advantages achieved by the invention are, in particular, that the heat content of liquid heat transfer media in the temperature level down to 80 ° C for generating steam from 3.0 to 6.0 bar is achieved with simple and very effective means. A temperature increase of approx. 50 ° C is achieved. The use of drive energy and motive steam reaches a minimal value.
  • the combination of mechanical and thermodynamic vapor compression is particularly flexible. With the help of an intake throttle on the mechanical compressor, its final pressure can be kept constant with changing steam quantities. This also means that the suction pressure of the steam jet compressors remains constant, and there is no need for additional motive steam because the pressure ratio also remains constant. Due to an overheating of approx. 25 ° C of the steam leaving the last stage of the mechanical compressor, favorable conditions result for the steam jet compressors.
  • the mechanical compressor usually a multi-stage, can have several entries, it can also be used at different suction pressures, i.e. H. evaporate at different temperatures.
  • the use of a multi-stage turbocompressor enables several steam flows, even of different pressure and temperature levels, to be brought to a uniform pressure and temperature level with simple means and with optimal energy efficiency.
  • this uniform pressure level for the combined amounts of steam enables the energetically optimal further compression of partial quantities by using several steam jets. Since the steam jets are operated with propellant steam of the same state and also work at the same final pressure, this solution is also advantageous from an operational point of view in terms of part-load behavior by switching individual steam jets on or off.
  • a low temperature level is to be understood as a temperature range from 80 to 115 ° C., preferably from 90 to 105 ° C.
  • the liquid heat transfer medium is preferably evaporated at a low temperature level and low pressure, in the case of water as heat transfer medium at a subatmospheric pressure from 0.5 bar, preferably from 0.7 bar.
  • the pressure increase by means of the steam jet injector is preferably 1.5 to 1.8 times.
  • Mechanical compression should preferably be understood to mean compression by means of a multi-stage turbocompressor.
  • known types of compressor such. B. screw compressor can be used.
  • Thermodynamic compression means compression by means of motive steam in a steam jet compressor.
  • the steam sucked in by the multi-stage mechanical compressor is gradually cooled by condensate injection.
  • the compression work is immediately converted into steam and can be used to advantage.
  • the liquid heat transfer medium is hot condensate, by means of vapors or other heat sources, such as. B. exhaust gases or vapors, heated feed water and / or a mixture of both.
  • Liquid heat transfer media are usually water, which means that according to the invention the steam is usually water vapor.
  • the invention is not limited to water vapor, but suction steam and motive steam should be of the same basic liquid.
  • the essence of the invention is not changed if a fluid other than water is selected or can be used as the heat transfer medium.
  • Indirect heating medium for feed water can be any other substance with a sufficient temperature level.
  • expansion steam of the same or higher pressure is added to the mechanically compressed steam.
  • the flash steam is e.g. B. obtained by relaxing condensate under higher pressure. If you want to reduce the overheating of the steam from the steam jet compressors, a corresponding amount of condensate is supplied to the steam from 3.0 to 6.0 bar in a known manner.
  • feed water is evaporated at a vacuum of 0.84 bar and 94 ° C.
  • steam is generated from several condensate collection tanks, which are under pressures of up to 2.9 bar, by relaxing to 0.84 bar. A total of 12,500 kg / h of saturated steam are produced by vapor evaporation and expansion.
  • This total steam in the amount of 12,500 kg / h is compressed by a multi-stage turbo compressor up to 2.45 bar.
  • the turbocompressor is driven by a counter-pressure steam turbine, the exhaust steam of which is produced at 16 bar and 205 ° C.
  • the steam superheated by the respective compression in the individual stages is cooled between the stages by condensate injection. This means that the drive energy is also directly converted into steam.
  • This injection of condensate increases the amount of steam by a further 735 kg / h to a total of 13 235 kg / h. After the last compressor stage, the superheated compressed steam is 22 ° C.
  • the steam jet compressors deliver a total of 32 055 kg / h of slightly superheated steam at 3.8 bar and 154 ° C. Since a slight temperature reduction is still possible in the present case, an additional 500 kg / h of condensate of 95 ° C are injected into the superheated steam and thereby converted again into steam. According to the process of the invention, a total of 32 555 kg / h of heating steam of 3.8 bar and 145 ° C, d. H. slightly overheated, won.
  • a further comparison calculation shows that steam of 16 bar and approx. 205 ° C. from the medium-pressure steam network can be used more energetically advantageously in a steam jet compressor after a turbo compressor than that it can be used as drive steam in a turbine for a further turbo compressor to increase the heating steam pressure of 2. 3 can serve at 3.8 bar. If it is expanded as drive steam for a turbine down to the wet steam area, it can only be used partially as heating steam, since the condensing water portion must be drawn off. Relaxation to 3.8 bar and approx. 142 ° C, i.e. H. no saturated steam yet, only results in a convertible energy difference of approx. 63 KJ / kg.
  • the work required for the above-mentioned pressure increase of the pre-compressed steam in a total steam quantity of 14 335 kg / h is 450 kW.
  • the combination according to the invention enables an advantageous utilization of waste heat from a low temperature level in connection with the thermally advantageous use of medium pressure steam.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Sorption Type Refrigeration Machines (AREA)

Claims (8)

1. Procédé de production de vapeur par évaporation et compression à la pression de 3,0 à 6,0 bar, de préférence de 3,5 à 4,5 bar et à la température de 140 à 165° C, à partir d'agents caloporteurs liquides à basse température et basse pression, caractérisé en ce que
a) les caloporteurs liquides sont évaporés à une température située entre 80° C et 1150 C, de préférence entre 90°C et 105°C, et à une pression inférieure à la pression atmosphérique allant jusqu'à 0,5 bar, de préférence à 0,7 bar;
b) les courants de vapeur produits sont d'abord comprimés mécaniquement à une pression intermédiaire, le facteur d'augmentation de la pression étant de 2,0 à 3,5;
c) la vapeur comprimée suivant b) subit par voie thermodynamique une augmentation de la pression de 1,4 au moins à l'aide de vapeur ayant une pression supérieure.
2. Procédé selon la revendication 1, caractérisé en ce que les courants de vapeurs produits sont comprimés à une pression intermédiaire, le facteur d'augmentation de la pression étant de préférence de 2,0 à 3,0.
3. Procédé selon les revendications 1 et 2, caractérisé en ce que le courant de vapeur comprimé selon la phase b) de procédé est divisé en plusieurs courants partiels qui subissent séparément une augmentation de la pression par voie thermodynamique.
4. Procédé selon la revendication 1, caractérisé en ce que les vapeurs comprimées mécaniquement sont désurchauffées progressivement par l'injection de condensat.
5. Procédé selon la revendication 1, caractérisé en ce que les agents caloporteurs liquides sont constitués par du condensat.
6. Procédé selon revendication 1, caractérisé en ce que les agents caloporteurs liquides sont constitués par de l'eau d'alimentation chaude.
7. Procédé selon la revendication 1, caractérisé en ce que les agents caloporteurs liquides sont en partie de condensat et en partie de l'eau d'alimentation chaude.
8. Procédé slon les revendications 1 et 2, caractérisé en ce que de la vapeur de détente dont la pression est égale ou supérieure à celle de la vapeur comprimée par voir mécanique est mélangée à cette dernière.
EP82101632A 1981-03-18 1982-03-03 Procédé de production de vapeur Expired EP0061031B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT82101632T ATE8174T1 (de) 1981-03-18 1982-03-03 Verfahren zur erzeugung von dampf.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3110520 1981-03-18
DE19813110520 DE3110520A1 (de) 1981-03-18 1981-03-18 Verfahren zur erzeugung von dampf

Publications (2)

Publication Number Publication Date
EP0061031A1 EP0061031A1 (fr) 1982-09-29
EP0061031B1 true EP0061031B1 (fr) 1984-06-27

Family

ID=6127619

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82101632A Expired EP0061031B1 (fr) 1981-03-18 1982-03-03 Procédé de production de vapeur

Country Status (6)

Country Link
US (1) US4438730A (fr)
EP (1) EP0061031B1 (fr)
JP (1) JPS57172102A (fr)
AT (1) ATE8174T1 (fr)
DE (2) DE3110520A1 (fr)
ES (1) ES8303656A1 (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60221601A (ja) * 1984-04-18 1985-11-06 三井造船株式会社 蒸気製造方法
JPS60221602A (ja) * 1984-04-18 1985-11-06 三井造船株式会社 蒸気製造方法
CS247740B1 (en) * 1984-04-24 1987-01-15 Ivan Petrovsky Hot water into heating and technological steam transformation circuit connection
US4690733A (en) * 1985-03-20 1987-09-01 Union Carbide Corporation Process for the separation of hydrocarbons from a mixed feedstock
US5102504A (en) * 1989-10-23 1992-04-07 Tetsuya Saito Device for solvent recovery in an ultrasonic cleaning device
US5587054A (en) * 1994-10-11 1996-12-24 Grano Environmental Corporation Vapor compression distillation system
US7748219B2 (en) * 2005-03-23 2010-07-06 Pdm Solar, Inc. method and apparatus to convert low temperature thermal energy to electricity

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE529464C (de) * 1927-02-26 1931-07-13 Philipp Mueller G M B H Verfahren zum Gewinnen von Dampf, Waerme und Destillat aus Kesselschlammwasser
US3962873A (en) * 1974-05-20 1976-06-15 Thermo Electron Corporation Solar steam generator
JPS52124504A (en) * 1976-04-12 1977-10-19 Sasakura Eng Co Ltd Steam compression system vaporing method
US4239603A (en) * 1978-02-22 1980-12-16 Dan Egosi Fuel-efficient generation of ejecting steam
US4282070A (en) * 1978-05-30 1981-08-04 Dan Egosi Energy conversion method with water recovery
LU80899A1 (fr) * 1979-02-08 1980-09-24 Laguilharre R Procede de concentration par mise en oeuvre d'un evaporateur mixte a thermocompression de vapeur-compression de vapeur
JPS55160274A (en) * 1979-04-25 1980-12-13 Gen Electric Heat recovery method
DE2920661A1 (de) * 1979-05-22 1980-12-04 Linde Ag Verfahren zur erzeugung von dampf

Also Published As

Publication number Publication date
DE3110520A1 (de) 1982-10-07
JPS57172102A (en) 1982-10-22
EP0061031A1 (fr) 1982-09-29
US4438730A (en) 1984-03-27
DE3260287D1 (en) 1984-08-02
ATE8174T1 (de) 1984-07-15
ES510518A0 (es) 1983-02-01
ES8303656A1 (es) 1983-02-01

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