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EP1766288B1 - Procede pour faire fonctionner un generateur de vapeur en continu - Google Patents

Procede pour faire fonctionner un generateur de vapeur en continu Download PDF

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Publication number
EP1766288B1
EP1766288B1 EP05766740A EP05766740A EP1766288B1 EP 1766288 B1 EP1766288 B1 EP 1766288B1 EP 05766740 A EP05766740 A EP 05766740A EP 05766740 A EP05766740 A EP 05766740A EP 1766288 B1 EP1766288 B1 EP 1766288B1
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EP
European Patent Office
Prior art keywords
preheater
feed water
density
feedwater
mass flow
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 - Lifetime
Application number
EP05766740A
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German (de)
English (en)
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EP1766288A1 (fr
Inventor
Axel Butterlin
Rudolf Kral
Frank Thomas
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Siemens AG
Original Assignee
Siemens AG
Siemens Corp
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Priority to EP05766740A priority Critical patent/EP1766288B1/fr
Priority to PL05766740T priority patent/PL1766288T3/pl
Publication of EP1766288A1 publication Critical patent/EP1766288A1/fr
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Publication of EP1766288B1 publication Critical patent/EP1766288B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • F22B35/00—Control systems for steam boilers
    • F22B35/06—Control systems for steam boilers for steam boilers of forced-flow type
    • F22B35/10—Control systems for steam boilers for steam boilers of forced-flow type of once-through type

Definitions

  • the invention relates to a method for operating a continuous steam generator with a Verdämpferterrorism Structure and a Verdampferbushes Structure flow medium side upstream preheater and a device for adjusting the feedwater mass flow ⁇ in the evaporator.
  • the heating of a number of steam generator tubes which together form the gas-tight surrounding wall of the combustion chamber, leads to complete evaporation of a flow medium in the steam generator tubes in one pass.
  • the flow medium usually water-is fed to a preheater upstream of the evaporator heating surface upstream of the evaporator, usually also referred to as an economizer, and preheated there.
  • the feedwater mass flow is regulated in the evaporator heating surface.
  • the evaporator flow and the heat input into the evaporator heating surface should be changed as synchronously as possible, otherwise an overshoot of the specific enthalpy of the flow medium at the outlet of the evaporator heating surface can not be reliably avoided.
  • Such an undesirable overshoot of the specific enthalpy makes it difficult to regulate the temperature of the live steam emerging from the steam generator and, moreover, leads to high material loads and thus to a reduced service life of the steam generator.
  • feedwater flow control In order to prevent an overshoot of the specific enthalpy and large temperature fluctuations in each operating state of the steam generator, is a feedwater flow control is provided, which provides the necessary feed water setpoints depending on the operating state even during load changes.
  • a continuous steam generator in which the feedwater flow rate is controlled via a pre-calculation of the feedwater quantity.
  • the basis for the calculation method is the heat flow balance of the evaporator heating surface into which the feedwater mass flow should enter, in particular at the inlet of the evaporator heating surface.
  • the measurement of the feedwater mass flow directly at the entrance of the evaporator heating surface proves to be technically complex and not reliably feasible in any operating condition.
  • the feedwater mass flow at the inlet of the preheater is alternatively measured and included in the calculations of the feedwater quantity, which however is not always equal to the feedwater mass flow at the inlet of the evaporator heating surface.
  • the size of the temperature fluctuations depends on the speed of the load change and a fast load change is particularly large. That's why it has been necessary make a limitation of the load cycle speed and thus take a lower efficiency of the steam generator in purchasing.
  • the fast and uncontrollable load changes that occur in the event of malfunctions reduce the life of the steam generator.
  • the invention is therefore based on the object of specifying a method for operating a steam generator of the type mentioned above, which allows a largely synchronous change of the feedwater mass flow through the evaporator and the heat input into the evaporator in any operating condition without great technical effort.
  • the device for adjusting the feed-water mass flow ⁇ is assigned a control device, whose control variable of the feed-water mass flow ⁇ and whose setpoint is guided ms for the feed-water mass flow dependent assigned by one of the steam generator power target value L, the control apparatus of the as a Input variables of the actual value ⁇ E of the feedwater density at the inlet of the preheater is supplied.
  • the invention is based on the consideration that for the synchronous change of feedwater mass flow through and heat input into the evaporator heating a heat flow balancing of the evaporator heating should occur.
  • a measurement of the feedwater mass flow should indeed be provided at the inlet of the evaporator heating surface.
  • the direct measurement of the feedwater mass flow at the entrance of the evaporator heating surface has proven not to be reliably feasible, it is now provided at a location which is suitable upstream of the media, namely at the inlet of the preheater.
  • the possible mass injection and recovery effects in the preheater could distort the measured value, these effects should be appropriately compensated.
  • the additional detection of the density of the flow medium at the outlet of the preheater heating surface is advantageously provided.
  • the desired value ⁇ s for the feedwater mass flow is the expression ⁇ + ⁇ ⁇ ⁇ V , where ⁇ is the actual value of the feedwater mass flow at the inlet of the preheater, ⁇ ⁇ the time change of the mean density of the flow medium in the preheater and V are the volume of the preheater.
  • the setpoint ⁇ s instead of the average density can be used for the calculation ⁇ approximately the density ⁇ E of the flow medium can be used at the inlet of the preheater.
  • the change with time: the density ⁇ E may be equal to the time change of the average density ⁇ are set, so that an additional detection of the density ⁇ A of the flow medium at the outlet of the evaporator heating surface is not required.
  • the signal of the entry density change must be delayed according to the flow time of the system, if instead of the mean density ⁇ approximately the density ⁇ E of the flow medium is used at the inlet of the preheater. Therefore, the actual value ⁇ E of the entry density is advantageously converted by a differentiating element with PT1 behavior customary in control technology into an entry density change delayed with the throughput time of the preheater as the time constant.
  • the calculation of the mean density is ⁇ and its time change ⁇ ⁇ not possible only by the approximate use of entry density. Since in the arithmetic mean ⁇ E and ⁇ A in the calculation of ⁇ In each case, in the case of a transient heat input, but a constant entry density ⁇ E, half the change in the exit density ⁇ A can be used as a measure of the density change in the preheater.
  • the formation of the time derivative of the density signal is performed by a differentiator.
  • the density signal is advantageously PT1-delayed with a relatively small time constant of about one second.
  • a correction circuit is preferably provided which compensates for the reaction of the DT1 element, which differentiates and delays the density signal at the outlet of the preheater, in this case.
  • the inlet density signal to a deadtime element with a time constant of the cycle time of the preheater is switched on, according to a thermal time constant of the preheater PT1-delayed and the signal thus generated the outlet density signal is switched negative.
  • this correction circuit ensures correct consideration of the density changes: In the event of an abrupt change in the temperature of the inflowing medium, the change in the outlet density ⁇ A is not taken into account as described. If, however, the entry density ⁇ E remains constant, but the heat input in the preheater changes and thus the outlet density ⁇ A , then no correction takes place at the outlet of the preheater and the effect of the change in the heat supply is fully taken into account in the calculation of the setpoint value ⁇ s for the feedwater mass flow ,
  • both the dead time and the thermal time constant of the preheater is adjusted reciprocally to the load of the steam generator.
  • the feedwater flow control is switched on and off depending on the operating state of the steam generator.
  • FIG. 1 schematically shows a device 1 for forming the set value Ms. for the feedwater mass flow of a continuous steam generator.
  • the continuous steam generator has a designated as economizer preheater 2 for feed water, which is located in a throttle cable, not shown.
  • the preheater 2 is on the flow medium side, a feedwater pump 3 upstream and a Verdampferlik Structure 4 downstream.
  • a measuring device 5 for measuring the feedwater mass flow ⁇ is arranged through the feedwater line.
  • a drive motor on the feedwater pump 3 is assigned a controller 6, at the input of which the control deviation ⁇ of the feedwater mass flow ⁇ measured by the measuring device 5 is located as a controlled variable.
  • the regulator 6 is associated with the device 1 for forming the set value ⁇ s for the feedwater mass flow .
  • This device is designed for a particularly needs-based determination of the setpoint ⁇ s . It is considered that the detection of the actual value of the feedwater mass flow ⁇ not immediately before the evaporator 4, but already before the preheater 2 takes place. This could be due to unit of mass or -aus Grandeungs binen in the preheater 2 inaccuracies in the measured value determination for the feed-water mass flow ⁇ result. To compensate for this, a correction of this measured value is provided taking into account the density ⁇ E of the feedwater at the inlet of the preheater 2.
  • the device 1 has among other things as input variables, on the one hand, a desired value L output by the setpoint generator for the output of the continuous steam generator and, on the other hand, the actual value ⁇ E of the density of the feedwater at the inlet of the preheater 2 determined from the pressure and temperature measurement of a measuring device 9.
  • the setpoint value L for the output of the continuous steam generator which changes over time in operation and which is given in the (not shown) Brennungsregelnik directly to the fuel control, is also supplied to the input of a first delay element 13 of the device 1.
  • This delay element 13 outputs a first signal or a delayed first power value L1.
  • This first power value L1 is supplied to the inputs of function generator units 10 and 11 of the function generator of the feedwater flow control 1.
  • ⁇ (L1) for the feedwater mass flow
  • ⁇ h (L1) for the difference of the specific enthalpy h IA at the outlet of the evaporator 4 and the specific heat h IE on The entry of this evaporator heating surface 4.
  • the values ⁇ and ⁇ h as functions of L1 are determined from values for ⁇ and Ah, which were measured during steady-state operation of the continuous steam generator, and stored in the function generator units 10 and 11 respectively.
  • the output quantities ⁇ (L1) and ⁇ h (L1) are multiplied together in a multiplication element 14 of the function generator of the device 1.
  • the recovered product value Q ⁇ (L1) corresponds the heat flow in the Verdampferloom Chemistry 4 at the power value L1 and is, if necessary, after correction by a determined in a differentiating element 14a from the enthalpy of entry characteristic for injection or Aus shallungs freee in the evaporator power factor input as a counter in a divider 15.
  • the difference between a desired value h SA (L2) of the specific enthalpy at the outlet of the evaporator heating surface 4 and the actual value h IE of the specific enthalpy at the inlet of the evaporator heating surface 4 formed by a summing element 19 is determined by means of the measuring device 9 is measured, entered.
  • the setpoint h SA (L2) is taken from a third function generator unit 12 of the function generator of the device 1.
  • the input value of the function generator unit 12 is produced at the output of a second delay element 16 whose input quantity is the first power value L1 at the output of the first delay element 13. Accordingly, the input value of the third function encoder unit 12 is a second power value L2 delayed from the first power value L1.
  • the values h SA (L2) as a function of L2 are determined from values for h SA , which were measured during stationary operation of the continuous steam generator, and stored in the third function generator unit 12.
  • a differentiating element 17 At the output of the second delay element 16 is the input of a differentiating element 17, the output of which is negatively connected to a summing element 18.
  • This summing element 18 corrects the value for the heat flow Q ⁇ (L1) into the evaporator heating surface 4 to the output signal of the differentiating member 17th
  • the measured by the measuring device 9 actual values of temperature and pressure of the feed water at the inlet of the preheater 2 are converted in a computing element 20 in an actual value ⁇ E of the feed water density at the inlet of the preheater 2. This is given to the input of a differentiating element 22 and multiplied by the volume of the preheater.
  • FIG. 2 shows an alternative embodiment of the feedwater flow control, which allows the reliable consideration of Massenein- and -Est Itemss binen in the control of the feedwater mass flow even in the event of a change in the heat input within the preheater 2.
  • the feedwater flow control according to FIG. 1 is to the example according to FIG. 2 added to the consideration of the density ⁇ A of the flow medium at the outlet of the preheater 2.
  • a measuring device 21 for measuring the pressure and the temperature of the flow medium is provided at the outlet of the preheater 2.
  • the computing element 26 determines as an input signal for a downstream summing element 30 from the measurement of temperature and pressure, the actual value for the density ⁇ A of the flow medium at the outlet of the preheater 2.
  • the output of the summing 30 is fed to a differentiator 36, the time derivative multiplied by the volume of the preheater 2 as an output signal.
  • This output signal which represents the change over time of the feedwater mass flow ⁇ ⁇ A at the outlet of the preheater 2, is applied to a summing element 36, which has as a second input variable the change ⁇ ⁇ E of the feedwater mass flow at the inlet of the preheater 2.
  • the summing element 36 has as an output signal calculated from ⁇ M A and ⁇ M E mean change of the feed-water mass flow ⁇ ⁇ basis of unit of mass and -aus arrivedungs binen in the preheater 2.
  • the output of the Dividiergliedes 36 is at the summing element 24 to the output signal of the Dividiergliedes 15 for correcting the Setpoint of the feedwater mass flow switched.
  • the output signal of the computing element 26 In the case of a malfunction, which leads to an abrupt change in temperature of the incoming feedwater to the preheater 2, for example in the event of sudden failure of an upstream preheating section, the output signal of the computing element 26 must still be corrected by the effect of the changed input density. If this is not done, the effect of the density jump at the inlet of the preheater 2 is taken into account twice, namely in the detection of the density of the feedwater at the inlet and at the outlet of the preheater 2. To correct this, the output signal of the differentiator 20 is a deadtime member 28 with the flow time of the feedwater through the preheater 2 as a time constant switched.
  • the signal thus generated is negatively connected to the summing 30 via a delay element 32 with a thermal storage constant of the preheater 2.
  • a delay element 32 with a thermal storage constant of the preheater 2.
  • the feedwater flow control using the device 1 allows in each operating state of the steam generator, a particularly simple determination of the setpoint ⁇ s for the feedwater mass flow through the evaporator 4.
  • a precise vote of this feedwater mass flow on the heat input in the evaporator heating can large fluctuations in the outlet temperature of the live steam and overshoot the specific enthalpy at the outlet of the evaporator 4 are reliably prevented. High material loads due to temperature fluctuations, which lead to a reduced service life of the continuous steam generator, can thus be avoided.
  • the curve II applies in the event that only as in FIG. 1 illustrated the change over time of the density ⁇ E at the inlet of the preheater 2 and thus only the Massenein- and -aus Grandes bine due to the temperature jump at the inlet of the preheater 2 is taken into account in the feedwater flow control. Massenein- and -Est standss bine due to a change in heating in the preheater 2 and thus a change in the heat input into the feed water stay unconsidered. This case corresponds to the feedwater flow control FIG. 1 ,
  • the curve III finally shows the time course of the specific enthalpy with additional consideration of the mass injection and -aus Grandens bine due to a change in heating in the preheater 2, which is the feedwater flow control FIG. 2 equivalent.
  • the summer 24 is off FIG. 2 as a second input variable in addition to the output of the differentiator 15, the calculated from ⁇ ⁇ A and ⁇ ⁇ E mean change in the feedwater mass flow ⁇ ⁇ .
  • the feedwater flow control therefore not only takes into account the density ⁇ E at the inlet of the preheater 2, but additionally the density ⁇ A at its outlet.
  • FIG. 3b shows the course (curves I to III) of the three specific enthalpies in kJ / kg at the outlet of the evaporator 4 depending on the time t for a continuous steam generator in partial load operation (50% of the maximum power) in case of failure of the preheater 2 upstream preheating.
  • the curve III in FIG. 3b shows as in FIG. 3a the time course of the specific enthalpy with additional consideration of the mass injection and -aus Grandens bine due to a change in heating in the preheater 2, which is the feedwater flow control FIG. 2 equivalent.
  • 3c shows the course (curves I to III) of the three specific enthalpies in kJ / kg at the outlet of the evaporator 4 depending on the time t for a continuous steam generator with a load change from full load to part load operation (100% to 50% load).
  • the curve III in 3c shows as in FIG. 3a the time course of the specific enthalpy with additional consideration of the mass injection and -aus Grandens bine due to a change in heating in the preheater 2, which is the feedwater flow control FIG. 2 equivalent.
  • FIGS. 3a . 3b and 3c show that the feedwater flow control 1 off FIG. 1 or 2 to avoid overshoot of the specific enthalpy at the outlet of the evaporator 4 is particularly suitable.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Control Of Steam Boilers And Waste-Gas Boilers (AREA)

Claims (8)

  1. Procédé pour faire fonctionner un générateur de vapeur à passage direct, comprenant une surface ( 4 ) de chauffe d'évaporateur, un préchauffeur ( 2 ) monté en amont du côté du milieu en écoulement de la surface ( 4 ) de chauffe d'évaporateur, un dispositif de réglage du courant Ṁ massique de l'eau d'alimentation et une régulation ( 1 ) du débit de l'eau d'alimentation, qui est associée à ce dispositif, dont la grandeur de réglage est le courant Ṁ massique de l'eau d'alimentation et dont la valeur Ṁs de consigne du courant Ṁ de l'eau d'alimentation est conduite en fonction d'une valeur L de consigne associée à la puissance du générateur de vapeur, caractérisé en ce que l'on envoie la valeur ρE réelle de la densité de l'eau d'alimentation à l'entrée du préchauffeur ( 2 ) à la régulation ( 1 ) du débit de l'eau d'alimentation en tant que l'une des grandeurs d'entrée.
  2. Procédé suivant la revendication 1, dans lequel on envoie la valeur ρA réelle de la densité de l'eau d'alimentation à la sortie du préchauffeur ( 2 ) à la régulation ( 1 ) du débit de l'eau d'alimentation comme autre grandeur d'entrée.
  3. Procédé suivant la revendication 1 ou 2, dans lequel on utilise la grandeur M ˙ + Δ ⁢ ρ ‾ ⋅ V
    Figure imgb0003
    comme valeur Ṁs de consigne du courant massique de l'eau d'alimentation, Ṁ étant la valeur réelle de courant massique de l'eau d'alimentation à l'entrée du préchauffeur ( 2 ), Δρ étant la variation en fonction du temps de la densité moyenne de l'eau d'alimentation dans le préchauffeur ( 2 ) et V étant le volume du préchauffeur ( 2 ).
  4. Procédé suivant l'une des revendications 1 à 3, dans lequel on utilise comme valeur d'approximation de la densité ρ moyenne la densité ρE de l'eau d'alimentation à l'entrée du préchauffeur ( 2 ).
  5. Procédé suivant la revendication 3 ou 4, dans lequel on forme la variation en fonction du temps de la densité Δρ moyenne de l'eau d'alimentation dans le préchauffeur ( 2 ) par un élément de fonction ayant une propriété de différenciation.
  6. Procédé suivant l'une des revendications 2 à 5, dans lequel on applique le signal de densité d'entrée à un élément de temps mort ayant une constante de temps du temps de passage du préchauffeur ( 2 ), on le retarde suivant PT1 conformément à une constante de temps thermique du préchauffeur ( 2 ) et on applique négativement le signal produit au signal de densité de sortie.
  7. Procédé suivant la revendication 1, dans lequel tant le temps mort qu'également la constante de temps thermique du préchauffeur ( 2 ) sont adaptés d'une manière inversement proportionnelle à la charge du générateur de vapeur.
  8. Procédé suivant l'une des revendications 1 à 7, dans lequel la régulation ( 1 ) du débit de l'eau d'alimentation peut être mise en circuit et hors circuit suivant les besoins.
EP05766740A 2004-07-09 2005-07-06 Procede pour faire fonctionner un generateur de vapeur en continu Expired - Lifetime EP1766288B1 (fr)

Priority Applications (2)

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EP05766740A EP1766288B1 (fr) 2004-07-09 2005-07-06 Procede pour faire fonctionner un generateur de vapeur en continu
PL05766740T PL1766288T3 (pl) 2004-07-09 2005-07-06 Sposób eksploatacji przepływowej wytwornicy pary

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP04016248A EP1614962A1 (fr) 2004-07-09 2004-07-09 Méthode pour l'opération d'une chaudière à vapeur à passage unique
EP05766740A EP1766288B1 (fr) 2004-07-09 2005-07-06 Procede pour faire fonctionner un generateur de vapeur en continu
PCT/EP2005/053227 WO2006005708A1 (fr) 2004-07-09 2005-07-06 Procede pour faire fonctionner un generateur de vapeur en continu

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EP1766288A1 EP1766288A1 (fr) 2007-03-28
EP1766288B1 true EP1766288B1 (fr) 2013-01-23

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EP05766740A Expired - Lifetime EP1766288B1 (fr) 2004-07-09 2005-07-06 Procede pour faire fonctionner un generateur de vapeur en continu

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US (1) US7624708B2 (fr)
EP (2) EP1614962A1 (fr)
JP (1) JP4704427B2 (fr)
CN (1) CN1906441B (fr)
AU (1) AU2005261689B2 (fr)
BR (1) BRPI0506706A (fr)
CA (1) CA2573015A1 (fr)
DK (1) DK1766288T3 (fr)
ES (1) ES2399756T3 (fr)
PL (1) PL1766288T3 (fr)
RU (1) RU2372554C2 (fr)
TW (1) TWI318280B (fr)
UA (1) UA90683C2 (fr)
WO (1) WO2006005708A1 (fr)
ZA (1) ZA200603906B (fr)

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DE102011004277A1 (de) * 2011-02-17 2012-08-23 Siemens Aktiengesellschaft Verfahren zum Betrieb eines direkt beheizten, solarthermischen Dampferzeugers
DE102011004269A1 (de) * 2011-02-17 2012-08-23 Siemens Aktiengesellschaft Verfahren zum Betrieb eines solarthermischen Parabolrinnenkraftwerks
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DE102012206466A1 (de) * 2012-04-19 2013-10-24 Siemens Aktiengesellschaft Verfahren und Vorrichtung zum Betrieb eines solarthermischen Kraftwerks
DE102014222682A1 (de) 2014-11-06 2016-05-12 Siemens Aktiengesellschaft Regelungsverfahren zum Betreiben eines Durchlaufdampferzeugers
EP3647657A1 (fr) * 2018-10-29 2020-05-06 Siemens Aktiengesellschaft Régulation de l'eau d'alimentation pour générateur de vapeur à récupération de chaleur à circulation forcée
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BRPI0506706A (pt) 2007-05-02
RU2372554C2 (ru) 2009-11-10
ZA200603906B (en) 2008-04-30
DK1766288T3 (da) 2013-04-08
ES2399756T3 (es) 2013-04-03
TW200606373A (en) 2006-02-16
CN1906441A (zh) 2007-01-31
PL1766288T3 (pl) 2013-06-28
JP4704427B2 (ja) 2011-06-15
CN1906441B (zh) 2010-06-16
US7624708B2 (en) 2009-12-01
UA90683C2 (ru) 2010-05-25
AU2005261689B2 (en) 2010-02-04
CA2573015A1 (fr) 2006-01-19
JP2008506087A (ja) 2008-02-28
US20080066695A1 (en) 2008-03-20
AU2005261689A1 (en) 2006-01-19
TWI318280B (en) 2009-12-11
RU2007104929A (ru) 2008-08-20
EP1614962A1 (fr) 2006-01-11
WO2006005708A1 (fr) 2006-01-19
EP1766288A1 (fr) 2007-03-28

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