• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Heat pumps, refrigerating units, thermal transformers and the like, actuated by means of a dual working material, particularly a mixture of ammonia and water, according to the resorption principle, operate with two solution cycles (I, II) wherein the working medium in liquid phase is brought from a lower pressure level to a higher pressure level and is expanded to a new lower pressure level, a connection (38, 40) existing respectively for the lower pressure and the upper pressure between the solution cycles (I, II), wherein the working medium in a vapour phase is exchanged. To compensate all the differences of concentration and quantity of the working medium in the two solution cycles (I, II) which occur during operation, there is provided in parallel to one of the two connections (38, 40) for the working medium in the vapour state a compensation connection (44) for the flowing liquid substance having a different concentration. The quantitative flow (Y) of the liquid working medium flowing in the compensation connection (44) is regulated by means of a central computer (48) as a function of the concentrations of the working medium flowing in the connections (38, 40) between the solution cycles (I, II), as well as of the amount (2) of the working medium in the vapour state circulating in one of the connections and of the concentration of the liquid working medium circulating in the compensation line (44).
    公开号:SU1347872A3
    申请号:SU853936953
    申请日:1985-08-07
    公开日:1987-10-23
    发明作者:Мусич Винко
    申请人:Ткх-Термо-Консультинг-Хайдельберг Гмбх (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to heat-using devices, namely, resorption heat-conversion plants, and can be used in heat pumps, chillers or thermotransformers operating on an ammonia-water mixture.
    The purpose of the invention is to increase the operational reliability of the installation.
    FIG. 1 shows a scheme of a resorption heat conversion installation operating as a heat pump or a refrigerating machine; in fig. 2 is a diagram of a resorption heat-conversion installation operating as a thermotransformer.
    The installation operating as a heat pump or chiller (Fig. 1) contains the first circuit 1 of the circulation of the solution with the branches of high 2 and low 3 pressure, which includes degasser 4, pump 5, resorber 6 and throttle 7, second circuit 8 circulation of the solution with its branches of high 9 and low 10 pressures, where absorber 11 is turned on. pump 12, desorber 13 and choke 14 In addition, the installation contains lines 15 and 16 of vapor refrigerant, solution line 17 with control valve 18, central computer 19 , sensors 20-22 pressure sensors 2 3-25 temperature and flow meter 26.
    The installation operating as a thermal transformer (Fig. 2) contains the first circuit 27 of the circulation of the solution with the branches of the high 28 and the low 29 pressure j where the low-pressure absorber 30, the pump 31, the high-pressure degasser 32 and the throttle 33 are included, the second circuit 34 circulation of the solution with high pressure 35 and low pressure 36 branches, where gas separator 37, pump 38, high pressure resorber 39 and choke 40 enter. In addition, the installation contains refrigerant vapor lines 41 and 42, flow line 43 with a control valve 44 and central computer liter 45.
    Resorption heat transfer unit to the installation as a heat pump or chiller (figure 1 works as follows.
    The energy available at a lower temperature level t is 1
    to
    15
    20
    25
    .
    | -
    l-)

    3478722
    It is located to the degasser 4, included in the circuit 1 of the circulation of the solution, where the evaporation of ammonia from the mixture occurs. Ammonia in X at DE Concentration
    The 15 vapor refrigerant is directed to the absorber 11 and is there absorbed by the solution of circuit 8 with energy recovered at the required (higher) temperature level t,. Thus, the concentration of the solution circulating in circuit 8 in the absorber 11 increases accordingly. The pump 14 increases the pressure of the solution and delivers it to the desorber 13 through the high-pressure branch 9,
    in which ammonia (when energy is supplied with a temperature tj) is again released from the solution and through the main
    16 vapor-refrigerant in the amount of Z at a concentration of DD should be in the resorber 6.
    The depleted solution remaining in the desorber 13 expands in the throttle 12 and returns along the low pressure branch 10 to the absorber 11.
    In the resorber 6, the incoming ammonia vapors are absorbed by the solution of circuit 1 with the release of energy at the temperature level t. The solution enriched in this way is then directed to high pressure branch 2 to throttle 7, expands there and returns to degasser 4. After the degasser 4, the solution with reduced concentration will relieve its pressure by means of pump 5 and through branch 2 is fed to resorber 6.
    Such an installation cycle can only be maintained continuously, when, in addition to the energy balance, the mass of the refrigerant is also provided to ensure its concentrations, respectively, the pressures in degasser 4, absorber 11, desorber 13 and resorber 6.
    Since there is no distillation column at the outlet of desorber 13, the DD concentration of ammonia in line 16 usually becomes lower than the C DE concentration in line 15, which leads to mass imbalance. This situation is eliminated by the presence on the low pressure side of the line -17 of the solution with the regulating ventil 18, which is controlled from the central computer 19. The latter receives current information on the concentrations DD, DE
    thirty
    star
    40
    45
    50
    and ЕАЕ according to indications of pressure sensors 20–22 and temperature sensors 23–25, as well as on mass flow rate Z of refrigerant vapor through line 16 using flow meter 26 (Venturi nozzles or diaphragms).
    The computer 19 generates a signal that drives the valve 18, with the result that the weak solution is flowed from the degassing A to the absorber 11, continuously maintaining the required mass balance.
    The resorption heat transfer installation as a thermal transformer (Fig. 2) works as follows.
    Energy at an average temperature level t is supplied to the degasser 32 in circuit 27, which causes refrigerant (ammonia) to escape from the solution and, with flow X and VOH concentration along line 41, is sent to high pressure resorber 39 in circuit 34. The depleted solution after the degasser 32 is expanded in throttle 33 and branch 29 goes to low pressure absorber 30 and absorbs refrigerant vapors from gas separator 37 at lower temperature level t
    The solution circulating in the circuit 34 after the gas separator 37 is directed by the pump 38 to the high-pressure resorber 39, where the absorption of refrigerant (ammonia) vapor released in the degasser 32 occurs. In this case, energy is released at the highest (required) temperature level ty. The resulting strong solution is then choked to a low pressure in the throttle 40 and goes to the gas separator 37.
    As in the first case, due to the absence of a distillation column, there is an inequality in the DH concentration of ammonia in line 41 and the DN concentration of ammonia in line 42, which makes it impossible to implement a thermal transformer cycle
    In order to eliminate the imbalance of the masses arising from the presence of the difference of the indicated concentrations, the installation contains a solution line 43 for bypassing the latter with a concentration E aE with flow rate from loop 27 to loop 34 on the high pressure side. Bypassing the required amount of solution is provided by regulating
    valve 44, which is controlled by the central computer 45.
    The latter receives information on the concentrations fDH, DN, and aE and on the mass flow rate Z through the line
    42 (similar to the case of operation of the unit as a heat pump or chiller) and generates a signal to valve 44. Thus, by controlling the flow rate U through the line
    The differences in the quantities and concentrations in circuits 27 and 34 are compensated for and, therefore, the thermo transformer is continuously operated.
    The proposed thermoconverter installation is higher. what operational reliability
    due to the automatic observance of mass balances and concentrations of the solution and refrigerant during operation.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    Resorptional heat transfer to a plant operating as a heat pump, a refrigeration machine or
    a thermotransformer on a two-component working fluid consisting of a refrigerant and an absorbent, mainly on an ammonia-water mixture, containing two circuits of circulation of the solution with high and low pressure branches, and in the heat pump and refrigerating machine the high pressure branches of each circuit are connected between as a vapor refrigerant main line, low pressure branches with its vapor refrigerant main line and a parallel solution line switched on, and in the thermotransformer of the high pressure branch a master and the low pressure branch with its vapor refrigerant main, all lines and lines serve to equalize the mass balance of the vapor refrigerant flowing between the two circuits, in order to improve operational reliability, In addition, it contains pressure and temperature sensors, installed in pairs in all magnets of the vapor refrigerant and solution lines, regulating the valve.
    0
    0
    five
    0
    installed in the solution lines, the flow meter installed in the heat pump and refrigeration machine on the refrigerant vapor line connecting the high-pressure branches, and in the thermotransformer on the magistra ro
    LP
    Editor A. Kozoriz Tehred M. Didyk,
    Order 5130/53 Circulation 475 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, st. Project, 4
    There is a vapor refrigerant connecting the low pressure branches and a central computer electrically connected to the pressure and temperature sensors, the flow meter, and the regulating valve.
    sixteen
    2B
    FIG. /
    Proofreader L. Pilipenko
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    同族专利:
    公开号 | 公开日
    US4594857A|1986-06-17|
    EP0164382B1|1988-05-18|
    AU3786985A|1985-06-26|
    DE3344599C1|1985-01-24|
    JPH0557505B2|1993-08-24|
    JPS61500629A|1986-04-03|
    WO1985002669A1|1985-06-20|
    EP0164382A1|1985-12-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3837174A|1973-03-16|1974-09-24|Sanyo Electric Co|Control device for an absorption system hot and cold water supply apparatus|
    FR2412798A1|1977-08-10|1979-07-20|Vaillant Sa|SORPTION HEAT PUMP|
    DE2748415C2|1977-10-28|1986-10-09|Naamloze Vennootschap Nederlandse Gasunie, Groningen|Heating method and bimodal heating system for heating buildings|
    DE3018739A1|1980-05-16|1981-11-26|Buderus Ag, 6330 Wetzlar|Resorption heat pump or refrigerator - has equalisation pipes between resorption and absorption sections|
    DE3048056C2|1980-12-19|1982-12-23|M.A.N. Maschinenfabrik Augsburg-Nürnberg AG, 8000 München|Absorption heat pump|
    DE3100348A1|1981-01-08|1982-08-05|Dieter Dr.-Ing. 5064 Rösrath Markfort|"RESORPTION SYSTEM FOR THE HEAT TRANSFORMATION"|
    JPS58500333A|1981-03-14|1983-03-03|
    DE3141538A1|1981-10-20|1983-05-19|Steag Fernwärme GmbH, 4300 Essen|Method and arrangement for transmitting heat from a first distant heat network with a higher forward run temperature to at least a second distant heat network with a low forward run temperature|
    EP0086768B1|1982-02-04|1985-08-28|Sanyo Electric Co., Ltd|Absorption heat pump system|
    US4487026A|1982-03-12|1984-12-11|Alfano Vincent J|Refrigeration system energy management control device and method|
    NL8204161A|1982-10-28|1984-05-16|Philips Nv|METHOD FOR OPERATING A BIMODAL HEAT PUMP AND BIMODAL HEAT PUMP FOR APPLYING THE SAID METHOD.|DE3536953C1|1985-10-17|1987-01-29|Thermo Consulting Heidelberg|Resorption-type heat converter installation with two solution circuits|
    US4712075A|1985-11-27|1987-12-08|Polaroid Corporation|Optical amplifier|
    DE3723938C2|1987-07-20|1989-05-03|Tch Thermo-Consulting-Heidelberg Gmbh, 6900 Heidelberg, De|
    US4921515A|1988-10-20|1990-05-01|Kim Dao|Advanced regenerative absorption refrigeration cycles|
    DE4104263C1|1991-02-13|1992-04-09|Tch Thermo-Consulting-Heidelberg Gmbh, 6900 Heidelberg, De|
    US5127234A|1991-08-02|1992-07-07|Gas Research Institute|Combined absorption cooling/heating|
    US5360320A|1992-02-27|1994-11-01|Isco, Inc.|Multiple solvent delivery system|
    CN102721230B|2011-03-31|2014-08-20|中国科学院工程热物理研究所|Thermodynamic cycle system and method for ammonia water mixed working medium power cooling combined supply|
    CN104501458B|2014-12-15|2017-01-25|安徽中家智锐科技有限公司|Saline energy-gathering tower heat pump system and saline concentration adjusting method thereof|
    DE102020117462A1|2020-07-02|2022-01-05|Andreas Bangheri|Method for operating an absorption heat pump|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3344599A|DE3344599C1|1983-12-09|1983-12-09|Resorption heat converter system|
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