• 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:
    1481751 Automatic process control TEXACO DEVELOPMENT CORP 11 April 1975 [3 May 1974] 14900/75 Heading G3R A plant in which components are removed from a gas stream by absorption in liquid solvent includes at least two absorbers. The flow-rate and composition of the feed gases and solvents and the effluent gases are measured for each absorber and used together with economic value signals for the gas components to calculate flow control signals which will ensure that the plant operates in an economically optimum manner. As shown in Fig. 1, a hydrocarbon separation plant includes two absorbers 2, 3 receiving feed gases over lines 4, 5 and solvent on lines 8, 9. Effluent gases flow out by way of lines 11, 12. Chromatograph devices 20, 20A, 20B monitor the compositions of the feed and effluent gases and feed solvent, and provide signals representing mole fractions to a control unit 28 and further signals to a programmer 27. Corresponding fluidflow rates are measured by devices 35-37, 35A- 37A, which also supply signals to the control unit 28. The input flow-rates of gas and solvent are directly controlled by devices 45-45C, the set points for which are determined by the unit 28, which includes pulse counting and logic circuitry, A/D converters, and sample and hold circuits. A signal representing total profit is computed and cyclically compared with a stored previous value. A pulse output causes storage of the new signal in digital form if greater than the previous value, and corresponding parameter control values are also stored.
    公开号:SU715010A1
    申请号:SU2136247
    申请日:1975-04-30
    公开日:1980-02-05
    发明作者:Юджин Свини Дональд (Младший)
    申请人:Тексако Дивелопмент Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    , .-- the number of moles of a component of 1 g in the outgoing gas from the absorbent j, referred to the prayer of the supplied gas to the absorber .j; the number of moles dissolve l free from the component entering the absorber j per unit time; —the number of moles of gas supplied to the absorber j per unit time; - deviation from equilibrium for component-j in absorber j - theoretical number of plates for absorber i; The member of equation (1) X, is determined from the formula: x ,, .- the number of moles of a component in the feed solvent to the absorber; molar share of the solvent is free from the component in the solvent supplied to the absorber j f%. The term of equation (1) 1 defines c from the formula:, where Z is the molar fraction of the component in the outgoing gas from. absorber j; the number of moles of gas escaping from the absorber and per unit time. Member of equation (1) L; defines c from the formula: where. R- is the volume of the feed stream. solvent to the absorber per unit of time; F; - molar conversion factor for absorberJ F; is determined by the formula: ff-2 5) J g - iq .V - (YVI r- -N4 where V is the molar volume of the solvent 1 free from the component, unit volume from time; -: molar. volume of component i , units of volume in mole; S is the molar fraction of solvent component i,%. The weights for formulas (| - V) can be obtained by measuring the parameters, transforming formula (I) to obtain the formula:
    The Xv1 value of Lc in this case can be compared with the reference values corresponding to the limits on the individual solvent free of the component supplied to the respective absorbers to make sure. The general economic value can be obtained by the formulas: I I%, 1 :, de P - the total economic value; D- - economic value of the component. Formula (VII.) Can be represented by solving formula il relatively in order to obtain the formula: .w 4-7: Ny Cl (c) The total flow rate of the solvent component entering the absorber can be obtained by cyiyiMHpOBANI individual flow rates of the ratertel free of the component, as is done in the equation: (Q) de L- is the rate of a separate solvent stream, free from the component; L. is the total flow rate of the growth solvent. . The total flow rate of the feed gas to the absorber can be obtained by summing the individual flow rates of the feed gas, as is done in the formula: Y tio) where G. is the total flow rate of the feed gas; G- - the speed of a separate feed gas stream. A new flow rate of the solvent free of the component fed to the absorber K can be obtained by adding a predetermined allowable change in the flow rate of the solvent free of the component fed to the absorber K, as shown in the formula: ..U. The individual flow rates of the solvent, free of the component, to other absorbers can be determined from the formula: that the inequality conditions are met: H, If the inequality conditions (xjji) are not met, a new value is determined for L, and L; recalculated again using the formula: Jl.-ub. Similarly, new flow rates for the feed gas are determined using the formulas:, K GI GG bj C IK e.:--Q., Ksha determines the new values for L- and G-, is calculated a new total benefit. If the new total benefit is greater than the previous total benefit, the values for LJ and Gy are remembered. The new flow rate for each solvent feed is determined by the formula: The stored values for the flow rates of the feed solvent and the flow rates of the feed gas associated with the stored total benefit are fed to the absorption system. Obviously, due to the various combinations of i components and j absorbers, the previous basic formulas give complex hardware. Therefore, in explaining the present shadow image, a system of two absorbers will be described, absorbing three components. Pipeline 1 supplies the absorbers 2 and 3 of the gas to be treated through pipelines 4 and 5, respectively. The solvent, which is fed through pipeline b, leads from to absorbers 2 and 3 through pipelines 7 and 8, respectively. Absorbers 2 and 3 provide a vent gas outlet through pipelines 9 and 10 to a common outlet pipe 11. For convenience, absorbers 2 and 3 are shown with common pipelines for feed gas, feed solvent and effluent gas, while the device offered by the formulas offers separate piping for feed gas, solvent feed and effluent gas for each absorber. Consequently, in the formulas where, for example, there is a separate component of the feed gas for absorber 2 and a separate component for absorber 3, in fact in the example below, a single signal is generated using a chromatograph. Thus, for ease of understanding, in a chromatograph it will be divided into two signals . Chromatograph 12 selects the supplied gas from pipeline 1 and provides the signal corresponding to the analysis for signal generation device 13 J. Signal generation device 13 receives control pulses and provides signals corresponding to the equal 5t,, y, Ct A2 C2 members supplied to control unit 14. Chromatograph 12 also provides a pulse signal to the chromatograph programming device 15. Each pulse in the specified signal corresponds to a maximum in the signal for device 13. Programming device 15 also provides control pulses to device 16 for generating signal Z. All elements with the same name, but producing different signals (for example, X, Y, Z), work this way the same way. Chromatograph 17 selects the outflowing gas flowing through conduit 11 and provides the appropriate signal for signal generation device 16 and pulse signal to paping device 15. Signal generation device 16 receives control pulses from programming device 15 and provides signals corresponding to the terms of equations 2D, Zg ,, Zg2 on control unit 14. Chromatograph 18 selects the solvent supplied from pipeline b and provides the appropriate signal for signal generation device 19 and a pulse signal for programmer 15. Signal generation device 16 receives control pulses from programmer 15 and provides signals for control unit 14 corresponding to components of the equations X, B2. Bl C1 "Sensors 20 and 21 flow velocities, perceiving the flow rates of gas supplied in pipelines 4 and 5, respectively, flow sensors 22 and 23, sensing the flow rates of solvent supplied in pipelines 7 and 8, respectively, and sensors 24 and 25, perceiving Flow rates flowing out in pipelines 9 and 10, respectively, provide the signals available in control unit 14. Control devices 26-29 provide signals for valves 30-
    权利要求:
    Claims (1)
    [1]
    Claim
    A method for automatically controlling the absorption process by determining the flow rates of the supplied solvent, incoming and outgoing gases, and determining a predetermined amount of chemical components in them, characterized in that, in order to simultaneously control the operation of two or more coli. The number of absorbers with different absorbing capacity in the optimal mode, the flow rates in each absorber are regulated depending on the flow rates in all absorbers and on the concentration of components determined in the feed gas, solvent, and exhaust gas of each absorber, taking into account the cost parameters of the process.
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    同族专利:
    公开号 | 公开日
    NL7505050A|1975-11-05|
    NO751307L|1975-11-04|
    GB1481751A|1977-08-03|
    US3917931A|1975-11-04|
    SU715010A3|1980-02-05|
    BE828233A|1975-10-22|
    CA1049636A|1979-02-27|
    DK193475A|1975-11-04|
    引用文献:
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    US3703068A|1971-03-26|1972-11-21|Union Carbide Corp|Control system for selective adsorption process|
    US3760168A|1971-05-24|1973-09-18|Universal Oil Prod Co|Reaction zone control|
    BE795592A|1972-02-24|1973-08-16|Texaco Development Corp|ALCOHYLATION INSTALLATION AND PROCESS|
    US3781533A|1972-04-07|1973-12-25|Exxon Research Engineering Co|Constraint control system for optimizing performance of process units|
    US3778603A|1972-05-26|1973-12-11|Texaco Inc|Means and method for achieving an optimum operating condition for an alkylation unit|
    US3838256A|1973-12-03|1974-09-24|Exxon Research Engineering Co|Constraint control for processes with equipment limitations|US4021211A|1975-02-26|1977-05-03|Klaus Turek|Process and apparatus for separation of solvents from an air stream laden with solvent vapors|
    AT350515B|1975-08-26|1979-06-11|Veitscher Magnesitwerke Ag|CONTROL SYSTEM FOR ABSORPTION COLUMNS|
    DE2656689C2|1976-12-15|1982-11-04|Daimler-Benz Ag, 7000 Stuttgart|Process for the wet cleaning of exhaust air containing organic carbon compounds with biological liquid regeneration|
    US4772298A|1982-11-24|1988-09-20|Phillips Petroleum Company|Control of a H2 S absorber|
    FR2575306B1|1984-12-21|1987-02-13|Elf Aquitaine|METHOD FOR REGULATING THE AMINE LOAD ON A NATURAL GAS PURIFICATION COLUMN|
    US5154734A|1991-07-12|1992-10-13|Calvert Environmental, Inc.|Pollution control system and method of using same|
    US5682309A|1995-04-28|1997-10-28|Exxon Chemical Patents Inc.|Feedback method for controlling non-linear processes|
    RU2630558C2|2015-12-14|2017-09-11|Открытое акционерное общество "Севернефтегазпром"|Determination method of absorber carry-over during process of gas dehydration|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US461061A|US3917931A|1974-05-03|1974-05-03|Means and method for controlling an absorber system|
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