EP2564118B1 - Procédé et dispositif destinés au contrôle de la température de la vapeur dans une chaudière - Google Patents

Procédé et dispositif destinés au contrôle de la température de la vapeur dans une chaudière Download PDF

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Publication number
EP2564118B1
EP2564118B1 EP11718698.1A EP11718698A EP2564118B1 EP 2564118 B1 EP2564118 B1 EP 2564118B1 EP 11718698 A EP11718698 A EP 11718698A EP 2564118 B1 EP2564118 B1 EP 2564118B1
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EP
European Patent Office
Prior art keywords
steam
boiler
heat
heat exchanger
sootblowers
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.)
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EP11718698.1A
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German (de)
English (en)
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EP2564118A2 (fr
Inventor
Karlheinz Hertweck
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Siemens AG
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Siemens AG
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28GCLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
    • F28G15/00Details
    • F28G15/003Control arrangements
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B35/00Control systems for steam boilers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B37/00Component parts or details of steam boilers
    • F22B37/02Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
    • F22B37/56Boiler cleaning control devices, e.g. for ascertaining proper duration of boiler blow-down
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28GCLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
    • F28G1/00Non-rotary, e.g. reciprocated, appliances
    • F28G1/16Non-rotary, e.g. reciprocated, appliances using jets of fluid for removing debris
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28GCLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
    • F28G9/00Cleaning by flushing or washing, e.g. with chemical solvents
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10TTECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00Fluid handling
    • Y10T137/0318Processes
    • Y10T137/0402Cleaning, repairing, or assembling
    • Y10T137/0419Fluid cleaning or flushing

Definitions

  • the invention relates to a method for controlling the temperature of steam in a boiler and to a corresponding device.
  • a fossil-fired steam generator or boiler of a power plant usually consists of a combustion chamber, an evaporator chamber and a system of heat exchangers that connect to the evaporator chamber.
  • boiler structures e.g. Drum kettle or Benson kettle.
  • the evaporator chamber consists of a tube arrangement which is in direct thermal contact with the combustion chamber.
  • the feedwater pumped from a feedwater pre-heater is evaporated to the saturated steam temperature.
  • the steam is passed through the system of heat exchangers, most of which are likewise tubular, in which the steam temperatures are brought to the inlet temperatures required by the turbines.
  • the system is composed of heat exchangers from at least one superheater, reheater, economizer and air preheater.
  • the Rußblasen therefore takes place in a conventional manner always against the background to eliminate the pollution of the boiler as globally as possible.
  • soot is blown cyclically, whereby the order of the sootblowers is adjusted manually according to the thermal state of the boiler or is blown correspondingly frequently, so that no uncontrollable thermal conditions arise.
  • sootblowing time is calculated according to economic criteria and contamination analyzes.
  • the Siemens system SPPA-P3000 "cost-effective soot blowing" also works according to these Criteria. However, just the pollution and the resulting heat loss are difficult to detect.
  • sootblowers are combined into groups of a maximum of four sootblowers. Each group is responsible for an area with similar deposit characteristics. Further, each sootblower receives a weighting factor corresponding to a percentage of the total number of sootblower cycles in which the sootblower is operating. Each sootblower cycle begins with the group of sootblowers located furthest upstream and continues in the direction of the flow of the combustion gases. The main criterion after which sootblowing is carried out is to operate the boiler at or at least near maximum efficiency. A child Criterion represents the lowest possible use of Rußblasedampf.
  • Displacements of the heat transfer can be partially compensated by an injection control of existing between the heat exchangers steam coolers. In principle, however, only water can be cooled by injection of water into the live steam and only a limited injection quantity can be used. Of particular note is the negative influence of the reheater injection on the heat requirement and the maximum possible output of the steam turbine generator process. Heat demand changes by 0.2% per change by 1% reheater injection rate.
  • the heat balance within the boiler can also be influenced by the combustion itself.
  • the live steam injection can only be kept in the control range with selective level firing, which is not always possible. Hardly, however, in this way, the reheater injection rate is sufficient to control.
  • thermal controllability of the boiler is more stable and optimal under the specification Thermal conditions of the boiler alone by the firing and selective injection cooling designed to be very complex and complex.
  • thermal imbalances can always occur. Additional problems occur due to the contamination in the boiler area, which always influences the heat transfer at the heat exchanger tubes and negatively superimposed on the control process.
  • a method and apparatus for improving steam temperature control is known.
  • a system for analyzing the effect of operating sootblowers in a heat transfer area of a power plant is provided. This system determines a steam temperature affecting sequence and calculates a feedforward control signal to be applied to a heat transfer region steam temperature control system.
  • the basic idea of the invention is to use the pollution, which up to now has been an unpredictable factor in the heat balance and severely limited the thermal controllability of the boiler, in a positive sense by adjusting it by means of sootblower devices on the heat exchanger surfaces inside the boiler and through this adjustment of the heat transfer at these surfaces, the steam temperatures are controlled.
  • the carbon black blowing takes place quasi-continuously and incrementally.
  • the thermal properties of quasi-continuous incremental carbon black bubbles can be controlled by changing the operating times of individual sootblowers or individual sootblower groups. Since the sootblower devices already in each Accordingly, no additional instrumentation or machine device for steam temperature control is required. This can save costs.
  • the adjustment of the pollution in the present invention always under ensuring a balanced overall heat balance within the boiler.
  • This advantageously optimizes the entire process engineering process. This is achieved, for example, by cleaning evaporator surfaces and superheater surfaces in such a way that the heat output to evaporator and superheater is distributed in such a way that, taking into account the limited capacity of the steam coolers, on the one hand the steam setpoint temperatures are always reached and, on the other hand, the permissible limit values are not exceeded , Multi-stranded boiler areas should be cleaned in such a way that temperature differences of the steam after division in the heat exchangers at the location of the subsequent consolidation are avoided. Basically, a minimum cleaning of the individual boiler areas should always be guaranteed and as clean recognized boiler areas should not be cleaned unnecessarily. Only in this way can a high efficiency of the whole process be guaranteed.
  • the pollution of individual heat exchangers is determined by recording a current heat transfer coefficient at the considered areas on the basis of a current heat balance.
  • the degree of contamination is determined by comparison with previously recorded in the clean state heat transfer coefficients, taking into account the influence of the relative boiler load by a region-wise linear regression.
  • the advantage of this embodiment is that here the states "dirty” or "clean” are detected for the first time.
  • the heat transfer coefficient plays a decisive role in a considered area.
  • the heat transfer coefficient is determined from the heat balance of steam and flue gas.
  • the sootblowing advantageously becomes part of the thermal boiler control and supports it. Sootblowing takes place completely automatically taking into account stable and optimal boiler thermal conditions. Even incorrectly dimensioned heat exchangers can be corrected by the controllable contamination according to the invention. So-called thermal imbalances of the boiler indentations are automatically compensated. Cleaning-related temperature fluctuations are minimized. The thermal conditions with renewed relative cleanliness are automatically recorded and stored as a measure of the future contamination.
  • sootblowers of a subgroup of sootblowers are subject to the criterion of the maximum operating time between a cleaning and the next cleaning, whereby a predefinable minimum cycle is ensured for each subgroup. Repeated cleaning of still clean areas is prevented by monitoring the average operating time and taking into account the current soiling.
  • the exhaust gas loss of the boiler can be influenced by the modification of the sootblower cycles. The current exhaust gas loss is automatically detected with renewed relative cleanliness of the relevant heat exchanger and stored as a measure of a future increase in the exhaust gas loss.
  • FIG. 1 represents in a greatly simplified form a steam generator.
  • the combustion chamber BR of the boiler K is a fossil solid fuel, for example, this is coal dust, burned.
  • the resulting flue gas RG is passed through the flue gas duct RGK for flue gas cleaning RGR.
  • the evaporation of supplied feedwater SPW takes place in the tube systems of the evaporator chamber and the heat exchanger.
  • the system is constructed such that the feed water from the feedwater tank 1 is fed to the feedwater preheat 2 (ECO). From there, the water-vapor mixture passes into the drum 3 and is supplied via the downpipes 4, the manifolds 5 and the risers 6 to the superheater (7 or Ü) and then to the turbine 8.
  • the superheater Ü can also include a reheater ZÜ.
  • the steam temperature is controlled and regulated by means of the sootblower device a certain contamination of the heat exchanger surfaces is set within the boiler.
  • FIG. 2 serves to clarify the determination of the degree of contamination or heat exchanger losses. Shown is simply a pipe section, wherein steam D flows through the interior of the pipe with a certain mass flow mD and pressure pD. At the inlet opening of the pipe, the temperature becomes TDe and at the outlet opening of the pipe, the temperature TD is measured. The pipe is surrounded by flue gas RG with the mass flow mRG and pressure pRG. Again, temperatures TRGein and TRGaus at the points of inlet and outlet openings of the tube can be determined.
  • the heat absorption of the heat exchanger tube is thus determined by the water / steam side variables flow, pressure and inlet / outlet temperature. On the flue gas side, the measurement of the mass flow and the inlet and outlet side temperatures is helpful, whereby missing temperatures and missing flue gas mass flow can also be calculated on the balance sheet.
  • the heat output of the heat exchanger is redetermined for the clean state after a suitably short mean Rußblasezyklus and adapted the boiler model used accordingly. Changes in the heat transfer behavior caused by permanent deposit formation or by changes in coal quality or operating conditions are automatically compensated in this way.
  • the heat absorbed during the further operation of the plant is then always determined up-to-date. This value is compared with the initial value of the clean state.
  • the example shows the flue gas temperature T as a function of the time t.
  • the flue gas temperature is inversely proportional to the steam temperature.
  • a conventional soot bubble cycle is shown during a travel time t R.
  • a travel time t R is defined as the operating time between a cleaning and the next cleaning for a sootblower or a subset of sootblowers.
  • a sootblowing process R which here consists of 6 Rußbläsern R1 to R6, the flue gas temperature drops sharply, and then increases continuously with increasing pollution of the pipes again.
  • Rnext the sootblowing process
  • sootblowers At low levels, the quasi-continuous operation of the sootblowers according to the invention is achieved. Is always a single sootblower of the totality of sootblowers of the plant in operation, can also be spoken of a continuous operation, which does not correspond to the invention.
  • the sootblower control is integrated into the temperature control of the boiler. There is always an automatic activation of individual Rußbläser under consideration process conditions.
  • the invention allows a very delicate control of steam temperatures in both time and place within the boiler and in the heat exchanger area. By sootblower optimization thermal imbalances within the heat exchanger system can be compensated. In Fig. 4 sketched two strands ST1 and ST2 a heat exchanger, for example, the reheater shown.
  • Fig. 5 For example, an embodiment of a control of a sootblower device is shown in a block diagram.
  • the total system of sootblowers RBGS is connected to individual sootblower groups RBG1 to RBGN and controls them according to the sootblowing algorithm according to the invention.
  • all units are connected to a monitoring logic module, which in turn hangs on a software which comprises an optimization program OP according to one of the claims.
  • individual sootblowers or subgroups of sootblowers RBG1 to RBGN are formed, which as a whole purify individually identifiable heat exchangers and are subdivided so that a single purge will only slightly change the total heat transfer of the heat exchanger.
  • the pollution of the individual heat exchanger is controlled so that in stationary operation of the boiler, the heat absorption of the individual areas in the fine range can be controlled.
  • Control variables of the method according to the invention are the times at which the individual sootblowers or subgroups are activated. From this it is possible to determine both the travel times of the individual sootblowers and the average of the sootblower groups which are assigned to a specific heat exchanger.
  • Input variables of the method are the sensor data of the temperatures of the water vapor and flue gas (see Fig. 2 ), their mass flows, injection rates of cooling water in live steam and superheated steam. From these variables, heat balances, heat transfer coefficients and thus the contamination of the individual boiler areas are determined.
  • the pollution on the other hand, Steam temperatures, thermal imbalances and also injection rates of live steam and the reheater steam detected.
  • By recording the travel time of the individual sootblowers specific subgroups are selectively selected for the next cleaning cycle and the soot blast time is determined.
  • soot bubbles always balance thermal imbalances.
  • For the evaporator area especially the control of the injection rate of live steam plays a major role. Care should be taken to ensure that the injection valve position of the live steam in the superheater is within the control range and that the setpoint temperature of the steam is reached. In the reheater area, the injection rate of live steam should go to zero.

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

Claims (7)

  1. Dispositif de contrôle de la température de la vapeur dans une chaudière (K) d'une installation (TA) technique, dans laquelle on produit des gaz de fumée et de la vapeur par combustion d'un combustible formant des cendres,
    dans lequel la chaudière (K) a au moins un évaporateur (V) et au moins un échangeur de chaleur (Ü, ZÜ, ECO), caractérisé
    en ce qu'au moyen de dispositifs de ramonage fonctionnant d'une manière quasi continue, on établit incrémentalement un encrassement graduel de surfaces de l'échangeur de chaleur à l'intérieur de la chaudière (K) et
    en ce que, par ce réglage de l'encrassement des surfaces de l'échangeur de chaleur, on régule un transfert de chaleur à ces surfaces de l'échangeur de chaleur, ainsi que des températures de la vapeur qui s'ensuivent dans la chaudière (K).
  2. Dispositif suivant la revendication 1,
    caractérisé
    en ce que l'on forme des groupes partiels de dispositifs de ramonage, qui nettoient des parties de la chaudière (K) identifiables individuellement autant que possible,
    en ce que l'on détecte dans l'installation (TA) technique au moins les paramètres suivants
    - taux d'injection de la vapeur fraîche et de la vapeur de surchauffeur intermédiaire,
    - température d'entrée de la vapeur et des gaz de fumée dans les échangeurs de chaleur
    - température de sortie des échangeurs de chaleur
    - facteurs d'encrassement de divers échangeurs de chaleur
    - temps de fonctionnement entre un nettoyage et le nettoyage venant immédiatement ensuite pour un dispositif de ramonage ou pour un groupe partiel,
    en ce qu'à partir des paramètres détectés et en garantissant un bilan thermique global compensé dans la chaudière, on détermine pour des dispositifs de ramonage individuels ou pour un groupe partiel des dispositifs de ramonage l'instant de ramonage.
  3. Dispositif suivant la revendication 2,
    caractérisé
    en ce que pour le ramonage,
    - on tient compte dans la zone de l'évaporateur et dans la zone du surchauffeur du taux d'injection de la vapeur fraîche et des températures d'entrée et de sortie du surchauffeur,
    - on tient compte, dans la zone du surchauffeur intermédiaire, du taux d'injection de la vapeur du surchauffeur intermédiaire en vue de la minimiser,
    - on tient compte de la perte de gaz perdus dans la zone de l'économiseur.
  4. Dispositif suivant l'une des revendications précédentes,
    caractérisé
    en ce que pour des temps de fonctionnement brefs s'ensuivant depuis un dernier nettoyage de tous les dispositifs de ramonage d'un échangeur de chaleur, on considère celui-ci comme propre.
  5. Dispositif suivant l'une des revendications précédentes,
    caractérisé
    en ce que l'on détermine l'encrassement des divers échangeurs de chaleur en détectant un coefficient (HTC) de transfert de chaleur présent sur les surfaces considérées à l'aide d'un bilan thermique présent,
    en ce que l'on détermine pour divers échangeurs de chaleur le degré de l'encrassement par comparaison à des coefficients de transfert de chaleur enregistrés auparavant dans l'état propre, l'influence de la charge relative de la chaudière étant prise en compte par une régression linéaire par partie.
  6. Dispositif suivant la revendication 5,
    caractérisé
    en ce que l'on détermine le degré d'encrassement par le facteur V d'encrassement au moyen de la formule V = 1-q/q0, dans laquelle q est la puissance calorifique spécifique de la vapeur par différence de température K entre les gaz de fumée et la vapeur et q0 est la puissance de la vapeur spécifique pour un état considéré comme propre.
  7. Dispositif pour effectuer le procédé suivant l'une des revendications 1 à 6.
EP11718698.1A 2010-04-29 2011-04-29 Procédé et dispositif destinés au contrôle de la température de la vapeur dans une chaudière Active EP2564118B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010018717 2010-04-29
PCT/EP2011/056853 WO2011135081A2 (fr) 2010-04-29 2011-04-29 Procédé et dispositif destinés au contrôle de la température de la vapeur dans une chaudière

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EP2564118A2 EP2564118A2 (fr) 2013-03-06
EP2564118B1 true EP2564118B1 (fr) 2016-06-01

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US (1) US20130192541A1 (fr)
EP (1) EP2564118B1 (fr)
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WO (1) WO2011135081A2 (fr)

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DE102011108327A1 (de) * 2011-07-25 2013-01-31 Clyde Bergemann Gmbh Maschinen- Und Apparatebau Verfahren zur Erhöhung des Wirkungsgrades einer Verbrennungsanlage, insbesondere eines Müllverbrennungs- oder Biomassekraftwerkes
FR3021103B1 (fr) * 2014-05-13 2016-05-06 Renault Sa Procede de detection de perte de performance d'un echangeur thermique de circuit de refroidissement
CN105069185A (zh) * 2015-07-14 2015-11-18 东南大学 一种利用烟气压差法建立空预器清洁因子计算模型的方法及应用
CN108303888B (zh) * 2018-02-07 2020-11-03 广东电网有限责任公司电力科学研究院 一种电站锅炉主蒸汽温度减温喷水控制方法及***
CN108506921B (zh) * 2018-04-25 2024-04-30 西安西热节能技术有限公司 一种电站锅炉的中高压工业供汽***及方法
US20210341140A1 (en) * 2020-05-01 2021-11-04 International Paper Company System and methods for controlling operation of a recovery boiler to reduce fouling
CN113378394B (zh) * 2021-06-19 2023-04-18 中国大唐集团科学技术研究院有限公司中南电力试验研究院 一种基于古尔维奇热平衡的智能吹灰算法
CN114111437A (zh) * 2021-10-26 2022-03-01 湖南永杉锂业有限公司 一种换热器结垢处理***及其控制方法

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Also Published As

Publication number Publication date
CN103328887A (zh) 2013-09-25
WO2011135081A2 (fr) 2011-11-03
EP2564118A2 (fr) 2013-03-06
WO2011135081A3 (fr) 2013-11-28
US20130192541A1 (en) 2013-08-01
CN103328887B (zh) 2016-04-20

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