WO2014005476A1 - 顺流式锅炉烟气余热回收*** - Google Patents

顺流式锅炉烟气余热回收*** Download PDF

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Publication number
WO2014005476A1
WO2014005476A1 PCT/CN2013/076917 CN2013076917W WO2014005476A1 WO 2014005476 A1 WO2014005476 A1 WO 2014005476A1 CN 2013076917 W CN2013076917 W CN 2013076917W WO 2014005476 A1 WO2014005476 A1 WO 2014005476A1
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WO
WIPO (PCT)
Prior art keywords
heat
heat exchanger
flue gas
temperature
pipeline
Prior art date
Application number
PCT/CN2013/076917
Other languages
English (en)
French (fr)
Inventor
刘兵
Original Assignee
上海伏波环保设备有限公司
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
Priority claimed from CN 201220327646 external-priority patent/CN202692016U/zh
Priority claimed from CN201210234270.XA external-priority patent/CN102734787B/zh
Application filed by 上海伏波环保设备有限公司 filed Critical 上海伏波环保设备有限公司
Priority to JP2015518806A priority Critical patent/JP2015525863A/ja
Publication of WO2014005476A1 publication Critical patent/WO2014005476A1/zh
Priority to US14/578,476 priority patent/US9476583B2/en

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/02—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged in the boiler furnace, fire tubes, or flue ways
    • F22D1/12—Control devices, e.g. for regulating steam temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F22B1/1892—Systems therefor not provided for in F22B1/1807 - F22B1/1861
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/02—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged in the boiler furnace, fire tubes, or flue ways
    • F22D1/04—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged in the boiler furnace, fire tubes, or flue ways the tubes having plain outer surfaces, e.g. in vertical arrangement
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/02—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged in the boiler furnace, fire tubes, or flue ways
    • F22D1/08—Feed-water heaters, i.e. economisers or like preheaters with water tubes arranged in the boiler furnace, fire tubes, or flue ways the tubes having fins, ribs, gills, corrugations, or the like on their outer surfaces, e.g. in vertical arrangement
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
    • F24D12/00—Other central heating systems
    • F24D12/02—Other central heating systems having more than one heat source
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
    • F24H8/00—Fluid heaters characterised by means for extracting latent heat from flue gases by means of condensation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
    • F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F21/00—Constructions of heat-exchange apparatus characterised by the selection of particular materials
    • F28F21/08—Constructions of heat-exchange apparatus characterised by the selection of particular materials of metal
    • F28F21/081—Heat exchange elements made from metals or metal alloys
    • F28F21/082—Heat exchange elements made from metals or metal alloys from steel or ferrous alloys
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
    • F24D2200/00—Heat sources or energy sources
    • F24D2200/16—Waste heat
    • F24D2200/18—Flue gas recuperation
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]

Definitions

  • the invention belongs to the field of energy and environmental protection, and particularly relates to a downstream boiler flue gas waste heat recovery system. Background technique
  • the boiler exhaust gas temperature is usually designed to be high.
  • the new boiler is about 14CTC, and it tends to be as high as 160 °C after running for a period of time.
  • this part of the flue gas must be desulfurized, that is, remove the acid gases such as S02 and S03 in the flue gas; dry and wet according to the absorbent and desulfurization products in the desulfurization process.
  • the state can further divide the desulfurization technology into a wet process, a dry process and a semi-dry (semi-wet) process.
  • the wet method is to desulfurize and treat the desulfurization product in a wet state by using a solution or slurry containing an absorbent.
  • the method has the advantages of fast desulfurization reaction, simple equipment, high desulfurization efficiency, and the like, so whether it is a large-scale power generation boiler or a small-sized industrial boiler. , both occupy a dominant position.
  • the boiler exhaust gas is generally 140 ⁇ 160 °C.
  • the boiler flue gas entering the desulfurization tower will be cooled down during desulfurization, generally falling below 60 °C.
  • the flue gas temperature is reduced from 140 ⁇ 160°C to 60°C, which not only wastes a lot of flue gas waste heat, but also increases the desulfurization operation cost; recovers this part of flue gas waste heat, reduces the flue gas temperature entering the desulfurization tower, and the equipment economy Operation, environmental protection and energy conservation are of great benefit.
  • the usual practice is to recover the part of the flue gas waste heat to heat the boiler feed water.
  • We know that the general flow of water into the boiler is to first remove the salt and soften it, then remove the oxygen, and then pass the economizer to the boiler; the flue gas waste heat heats the boiler's feed water.
  • demineralized demineralized water heated to remove oxygen for ordinary industrial boilers, demineralized demineralized water temperature is ambient temperature, about 25 °C, changes with ambient temperature; if this part of demineralized water is used directly to cool boiler flue gas Recycling waste heat from the flue gas will cause the temperature of the heat exchanger wall that is in contact with the flue gas to be too low, causing acid gas condensation in the flue gas. Corrosion heat exchange equipment on the wall of the heat exchanger.
  • the domestic technologies for recovering this part of flue gas waste heat are: mature technologies such as low pressure economizer, heat pipe heat exchanger and phase change heat.
  • the low-pressure economizer technology is mainly used to reduce the exhaust gas temperature in domestic large and medium-sized power plants. It is installed in the flue of the boiler tail and is cooled by the condensate on the water side of the low-pressure heater in the steam turbine regenerative system instead of the high-pressure feed water. Flue gas, its heat exchange conditions are similar to the economizer, but the pressure on the water side is much lower than the pressure of the economizer, so it is called the low pressure economizer.
  • the installation of the low-pressure economizer allows the steam turbine heat exchange system to obtain an external heat, saves a part of the extraction steam, and recovers the heat loss of the exhaust gas well, which improves the thermal efficiency of the whole plant.
  • a heat pipe is a component that relies on its internal working liquid phase change to achieve heat transfer.
  • the heat pipe can be divided into two parts: the evaporation section and the condensation section.
  • the working fluid is heated and vaporized by the heat source to become steam, and the steam flows to the other end along the intermediate channel under the pressure difference.
  • the steam condenses into a liquid after releasing the latent heat to the cold source in the condensation section; when the working medium evaporates in the evaporation section, the gas-liquid interface is concave, forming a plurality of meniscus liquid surfaces, generating capillary pressure, and the liquid working medium is in the capillary capillary pressure Under the action of return flow such as gravity, it returns to the evaporation section, and continues to absorb heat and evaporate. In this way, the evaporation and condensation of the working fluid continuously transfer heat from the hot end to the cold end. Since the heat pipe uses the phase change heat of the working fluid to transfer heat, the heat pipe has a large heat transfer capacity and heat transfer efficiency.
  • the phase change heat exchanger is further extended on the basis of the heat pipe, and the original heat pipe cluster is connected to make the internal medium flow arbitrarily, and the working pressure of the internal medium can be adjusted arbitrarily with the change of the load.
  • the non-condensable gas in the heat pipe cluster can be discharged at any time.
  • the above three heat exchange technologies utilize the wall temperature of the heat exchange device to be higher than the acid dew point temperature of the flue gas, so that the device is not corroded by acid dew, and the temperature difference of heat transfer is considered, so that the temperature range of the flue gas is small. .
  • the temperature drop space has been further improved.
  • the Chinese invention application with the publication number CN1477333A is a composite heat exchange technology.
  • the feed water is preheated by the cold end of the flue gas through the phase change heat device, and then directly exchanged by the hot end of the flue gas through the economizer to thereby achieve The higher the temperature of the heated water, the cold fluid is first heated by the low temperature section of the flue gas, and then flows to the high temperature section of the flue gas for further heating.
  • the flow direction is called the countercurrent type, and the applicable range is low temperature cold source - less boiler feed water, recycling
  • the heat can be fully utilized to the heating water supply; assuming the dew point temperature of the flue gas is 80 ° C, leaving a certain safety margin and heat transfer temperature difference, in order to ensure the normal operation of the equipment, the final exhaust gas temperature is still above 10 CTC;
  • the utility model patent of the publication No. 201844388U is a counterflow type flue gas waste heat recovery device.
  • the feed water first passes through a separate heat pipe heat exchanger located in the low temperature section of the flue, and then flows to the tandem type pipe located in the high temperature section of the flue. Heat exchanger.
  • the counterflow heat exchanger has certain requirements on the inlet water temperature, and the use of the flue gas temperature range is limited, and the cooling temperature is still incomplete.
  • the wall temperature of the heat exchanger is greater than the acid dew point temperature of the flue gas, since no sulfuric acid vapor is precipitated, it can be regarded as a non-corrosive heat exchanger.
  • the above technology and the listed patents are based on this; as the wall temperature decreases, the sulfuric acid starts. Condensation, at the beginning, because the concentration of sulfuric acid is very high, the amount of condensation is not much, so the corrosion rate is not very fast. As the wall temperature decreases, the amount of condensation increases, the corrosion accelerates, and the maximum temperature is 20-3CTC below the dew point temperature, and the temperature decreases again. The reactivity between the metal and the acid is reduced, and the corrosion rate is also reduced.
  • the wall temperature is lower than the dew point temperature of the flue gas, a large amount of water vapor is precipitated, and the corrosion is extremely increased; therefore, there are two for the flue gas heat exchanger.
  • the wall temperature is 20 ⁇ 30°C below the acid dew point; 2.
  • the wall temperature is below the water dew point.
  • the technical problem to be solved by the invention is to provide a flue gas waste heat recovery system of a downstream boiler, wherein the total flow direction of the flue gas heating water is downstream, the first heat exchanger first heats the cold water, and the preheated cold water goes to the second.
  • the heat exchanger is heated, so that the cold water is first heated by the high temperature section of the flue gas, and then further heated with the low temperature section of the flue gas.
  • the total flow is downstream, which can well control the wall temperature of the two-stage heat exchanger, and can The temperature of the smoke is lower.
  • a downstream boiler flue gas waste heat recovery system comprising first and second heat exchangers, wherein the first heat exchanger is disposed on a high temperature side of the flue, comprising an endothermic section, and an exothermic section, the endothermic The section and the heat release section are connected to the circulation loop through the first pipeline, the heat absorption section is disposed in the flue; the second heat exchanger is disposed on the low temperature side of the flue, and the second heat exchanger includes the second tube The inlet header and the outlet header of the road; the first and second heat exchangers are connected by a third pipeline, and the heat release section of the first heat exchanger is placed in the third pipeline, and the medium to be heated flows in The third conduit then enters the second heat exchanger through the inlet header of the second heat exchanger and exits through the outlet header of the second heat exchanger.
  • the third pipeline includes a first branch, a second branch for flow regulation, and the first branch and the second branch are connected in parallel, and the heat release section of the first heat exchanger is placed in the Said in the first branch.
  • the second branch of the third pipeline is provided with a regulating valve, and the opening of the regulating valve is controlled by the control device.
  • a first measuring line connecting the heat absorbing section and the heat releasing section of the first heat exchanger is provided with a temperature measuring point, and the temperature measuring point sends a temperature signal to the control device.
  • the invention mainly comprises a two-stage heat exchanger, which is a first heat exchanger and a second heat exchanger, respectively, wherein the first heat exchanger is located on a high temperature side of the flue, and the flue gas first exchanges heat with the second heat exchanger
  • the low temperature side is located in the flue
  • the first heat exchanger of the invention is divided into two parts: an endothermic section and an exothermic section; the endothermic section is installed in the flue behind the boiler dust collector to absorb the residual heat flowing through the flue gas;
  • the heat absorption section and the heat release section are connected by a pipeline to a closed loop system, and a circulation pump is connected to the connection pipeline; the medium in the pipeline is forced circulation water;
  • the heating medium ie the low temperature feed water to be heated
  • a bypass ie, the second branch
  • a regulating valve is connected to the bypass to adjust the flow of the bypass feed water.
  • the heated feed water and the bypassed feed water are collected and heated to the second heat exchanger;
  • the second heat exchanger of the present invention is an economizer type heat exchanger, which is divided into an inlet and outlet header and a tube bundle; an exothermic section of the first heat exchanger and an inlet of the second branch pipeline and the second heat exchanger
  • the header is connected, and then connected to the second heat exchanger tube bundle, and the heated water supply pipe directly exchanges heat with the flue gas outside the tube
  • the second heat exchanger material of the invention may be corrosion-resistant steel according to the specific implementation case, or For ordinary carbon steel.
  • the control system of the present invention mainly comprises a control device and a temperature measuring point installed at the outlet end of the forced circulation pump, and the temperature signal measured by the temperature measuring point is transmitted to the control device, and the control device controls the opening degree of the regulating valve according to the obtained temperature signal. Realize the flow of feed water to regulate the bypass.
  • FIG. 1 is a system schematic diagram of a flue gas waste heat recovery system of a downstream boiler according to the present invention.
  • FIG. 1 it is a system schematic diagram of a flue gas waste heat recovery system of a downstream boiler according to the present invention.
  • the first heat exchanger is disposed on the high temperature side of the flue 8 and includes the heat absorption section 7 and the heat release section.
  • the heat absorption section 7, the heat release section 3 is connected into a circulation loop through the first pipeline 11, the heat absorption section 7 is disposed in the flue 8; the second heat exchanger is disposed in the flue 8 low temperature a second heat exchanger comprising an inlet header 5 and an outlet header 4 of the second conduit 12; the first and second heat exchangers are connected by a third conduit 13, the third conduit 13 includes a first branch 14 and a second branch 15, wherein the first branch 14 is provided with a heat release section 3 of the first heat exchanger, and a heating medium flows through the first branch 14 After the two branches 15 merge, they enter the second heat exchanger through the inlet header 5 of the second heat exchanger and then flow out through the outlet header 4 of the second heat exchanger.
  • the second branch 15 of the third line 13 is provided with a regulating valve 2, the opening degree of the regulating valve 2 is controlled by the control device 1, and the heat absorbing section 7 of the first heat exchanger is connected
  • a temperature measuring point 9 is provided on the first line 11 between the heat releasing sections 3, and the temperature measuring point 9 delivers a temperature signal to the control unit 1.
  • the first line 11 of the first heat exchanger flows forced circulation water, and the first line 11 is provided with a circulation pump 10.
  • the boiler low temperature feed water flows through the first branch 14 and the second branch 15 of the third pipeline 13.
  • the material of the tube bundle 6 of the second heat exchanger contacting the flue gas is corrosion-resistant steel or ordinary carbon steel.
  • the invention is divided into a first heat exchanger and a second heat exchanger; Heat is used to recover waste heat from the flue gas; the purpose of the first heat exchanger is to initially heat the low temperature feed water of the boiler, and the heated low temperature feed water and the bypass (ie the second branch 15) are concentrated, and then enter the second economizer type.
  • the heat exchanger exchanges heat with the flue gas, recovers the residual heat of the flue gas, and reduces the temperature of the flue gas entering the desulfurization equipment.
  • the method of the invention is divided into two heat exchangers, wherein the first heat exchanger preheats the desalted feed water at 40 ° C; the first heat exchanger is divided into two parts: the heat absorption section 7 and the heat release section 3, and the heat absorption Section 7 absorbs the waste heat of the flue gas, transfers it to the forced circulation water flowing through, and the circulating water transfers the heat to the 40 °C desalting feed water in the heat release section 3, and controls the opening degree of the bypass regulating valve 2 to control Bypassing the flow of desalting feed water, indirectly controlling the first heat exchanger The heat transfer amount of the hot section 3, thereby controlling the temperature of the forced circulation water in the closed loop of the first heat exchanger exothermic section 3 and the endothermic section, and achieving the first heat exchanger endothermic section 7 from acid dew corrosion Purpose; As with the above various techniques, the maximum energy-saving space of the first heat exchanger is about 10 ° C, and the exhaust gas temperature is about 11 CTC;
  • the temperature of the demineralized water after mixing can be controlled at about 45 ° C. If the water dew point temperature of the flue gas is 42 ° C, The large bypass flow can be adjusted to reduce the heat exchange amount of the first heat exchanger exothermic section 3. At this time, the exhaust heat temperature of the first heat exchanger heat absorption section 7 is higher than (or equal to) 110 °C.
  • the temperature of the demineralized water after being mixed by the first heat exchanger is about 45 ° C of the water dew point of the flue gas, and then enters the second economizer heat exchanger to directly exchange heat with the flue gas (should be guaranteed to pass the second
  • the temperature of the flowing medium of the heat exchanger inlet header 5 entering the second heat exchanger is the water dew point temperature of the flue gas.
  • the temperature of the demineralized water is about +5 °C; therefore, the wall temperature of the second heat exchanger is about 50 °C, which is higher than the water dew point temperature of the flue gas, assuming that the flue gas drops to 70 ° C, the total heat absorption.
  • the temperature of the demineralized water can be increased to 20 ° C, so the outlet temperature of the demineralized water is 65 ° C; thus the wall temperature of the second heat exchanger on the side in contact with the flue gas is 50 to 70 ° C, although the flue gas is avoided.
  • Acid dew corrosion near the water dew point however, the wall temperature of the second heat exchanger may fall in a severely corroded area of 20 ⁇ 30 ° C below the acid dew point.

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  • Mechanical Engineering (AREA)
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Abstract

一种顺流式锅炉烟气余热回收***，包括第一、第二换热器，所述第一换热器设于烟道高温侧，包括吸热段、和放热段，所述吸热段、放热段通过第一管路连接成循环回路，所述吸热段设于烟道中；所述第二换热器设于烟道低温侧，所述第二换热器包括第二管路的进口集管、出口集管；所述第一、第二换热器通过第三管路连接，所述第一换热器的放热段置于第三管路内，待加热介质流入所述第三管路中再通过第二换热器的进口集管进入第二换热器并且通过所述第二换热器的出口集管流出，该余热回收***可以把烟温降地更低，大大提高了锅炉烟气余热节能回收的空间，降低了进入脱硫除尘设备的锅炉烟气温度，节省脱硫设备运行成本。

Description

顺流式锅炉烟气余热回收***
技术领域
本发明属于能源环保领域， 具体说涉及一种顺流式锅炉烟气余热回收***。 背景技术
我国目前绝大多数锅炉的燃料还是以煤为主，其中含有 S元素， 经燃烧后使得 锅炉排放的烟气中含有酸性气体， 烟温高时它们会以气态的形式流经锅炉各受热 面。当烟温低于某一温度时，它们会与烟气中的水蒸气结合成硫酸而腐蚀换热设备。 低温腐蚀通常出现在锅炉空气预热器的冷端以及给水温度低的省煤器中。当受热面 的温度低于烟气的露点时， 烟气中的水蒸气和煤燃烧后所生成的三氧化硫（只是硫 的燃料产物的很少一部分）结合成的硫酸会凝结在受热面上， 严重腐蚀受热面。 为 避免锅炉尾部受热面的酸露腐蚀，通常锅炉排烟温度设计较高，新锅炉 14CTC左右， 运行一段时间后往往会高达 160°C。
为了达到国家环保规定的排放标准， 降低酸雨形成危害， 这一部分的烟气必须 经过脱硫处理， 即去除烟气中的 S02、 S03等酸性气体； 按吸收剂及脱硫产物在脱 硫过程中的干湿状态又可将脱硫技术分为湿法、 干法和半干（半湿）法。 湿法技术 是用含有吸收剂的溶液或浆液在湿状态下脱硫和处理脱硫产物，该法具有脱硫反应 速度快、 设备简单、 脱硫效率高等优点， 因此无论是大型发电锅炉， 还是中小型工 业锅炉， 都占有主导地位。
根据前述所知， 锅炉的排烟一般 140~160°C， 为提高脱硫效率及保护脱硫塔自 身设备， 脱硫时会对进入脱硫塔的锅炉烟气进行降温处理， 一般降至 60°C以下， 烟气温度从 140~160°C降至 60°C， 不光浪费了大量的烟气余热， 而且提高脱硫运行 成本； 回收这部分烟气余热、 降低进入脱硫塔的烟气温度， 与之设备经济运行， 环 保节能都大有裨益。
通常的做法是回收这部分烟气余热加热锅炉的给水，我们知道进锅炉的水一般 流程为先除盐软化， 再除氧， 然后再经过省煤器至锅炉； 烟气余热加热锅炉的给水 即是指加热去除氧的除盐软化水； 对于普通工业锅炉来说， 除盐软化水温度为环境 温度， 25°C左右， 随环境温度变化而变化； 若直接拿这部分除盐水冷却锅炉烟气回 收烟气余热， 会使与烟气接触的换热器壁面温度过低， 造成烟气中的酸性气体结露 于换热器壁面腐蚀换热设备。 国内对于回收这部分烟气余热的技术主要为： 有低压 省煤器、 热管换热器及相变换热器等成熟技术。
低压省煤器技术在降低排烟温度上主要对象是国内大中型电厂的锅炉，它安装 在锅炉尾部烟道中，利用汽轮机回热***中的低压加热器水侧的凝结水而非高压给 水来冷却烟气， 其换热条件类似于省煤器， 但水侧的压力远远低于省煤器的压力， 故称其低压省煤器。低压省煤器的安装使得汽轮机换热***得到一份外来热量， 节 省了一部分抽汽气， 很好的回收排烟热损失， 提高了全厂的热效率。
热管是依靠自身内部工作液体相变来实现传热的元件。 热管可分为蒸发段、 冷 凝段两个部分， 当热源在蒸发段对其供热时， 工质自热源吸热汽化变为蒸汽， 蒸汽 在压差的作用下沿中间通道高速流向另一端，蒸汽在冷凝段向冷源放出潜热后冷凝 成液体； 工质在蒸发段蒸发时， 其气液交界面下凹， 形成许多弯月形液面， 产生毛 细压力， 液态工质在管芯毛细压力和重力等的回流动力作用下又返回蒸发段， 继续 吸热蒸发， 如此循环往复， 工质的蒸发和冷凝便把热量不断地从热端传递到冷端。 由于热管是利用工质的相变换热来传递热量，因此热管具有很大的传热能力和传热 效率。
相变换热器在热管的基础上又做了进一步的延伸， 把原先热管簇做了联通， 使 其内部介质可以任意的流动，而且内部介质的工作压力可随负荷的变动而随意的调 整， 可以随时排放热管簇中的不凝气体。
然而上述三种换热技术都是利用换热设备的壁面温度高于烟气的酸露点温度 而使设备不受酸露腐蚀， 考虑的传热温差等因素， 因此降低烟气的温度幅度很小。 近年来随着耐腐蚀材料的广泛应用， 使得温降空间有了进一步的提升。
公开号为 CN1477333A的中国发明申请， 为一种复合式换热技术，给水先经过 相变换热器被烟气冷端预加热， 再经过省煤器被烟气热端直接换热， 从而达到更高 的加热水温度， 这种冷流体先经过被烟气低温段加热， 然后流向烟气高温段进一步 加热的流向称为逆流式， 其适用范围为低温冷源——锅炉给水较少， 回收的热量能 全部利用至加热给水中； 假设烟气露点温度为 80°C， 留有一定安全余量和传热温 差， 为保证设备正常运行， 其最终排烟温度仍在 10CTC以上；
公开号为 201844388U的中国实用新型专利， 为一种逆流式的烟气余热回收装 置， 给水先经过位于烟道低温段的分离式热管换热器， 然后流向位于烟道高温段的 串联式的管式换热器。 然而为保证换热器不受酸露腐蚀的影响，逆流式换热器对进水温度有一定的要 求， 其烟气温度区间利用有限， 降温仍不彻底。
换热器壁面温度大于烟气的酸露点温度时， 由于无硫酸蒸汽析出， 可以近似看 做不腐蚀换热器， 以上技术和所列专利正是基于此； 随着壁面温度的降低， 硫酸开 始凝结， 开始时由于硫酸浓度很高， 凝结的量也不多， 故腐蚀速度不是很快， 随壁 温降低， 凝结量增加， 腐蚀加快， 在露点温度以下 20-3CTC达到最大值， 温度再降 低， 金属与酸液反应活性降低， 腐蚀速度亦随之降低， 当壁面温度低于烟气水露点 温度时， 大量水蒸气析出， 腐蚀极具增大； 因此对于烟气换热器来说有两个腐蚀严 重的区域： 1、 壁温为酸露点以下 20~30°C区域； 2、 壁温为水露点以下区域。
以上技术和所列专利使烟气换热器的壁面温度高于烟气酸露点温度来避免酸 露腐蚀问题，然而正如前述分析，相较于烟气温度 160°C降至 60°C这一可利用空间， 存在降温不彻底的问题， 基于此种情况， 给出本发明所列解决方案。 发明内容
本发明要解决的技术问题是提供一种顺流式锅炉烟气余热回收***，烟气加热 水总的流向为顺流，第一换热器先加热冷水，预加热后的冷水再去第二换热器加热， 这样冷水先经过被烟气高温段加热， 然后与烟气低温段进一步加热， 这一总流程为 顺流， 这样可以很好地控制两级换热器的壁温， 可以把烟温降地更低。
本发明采用以下技术方案：
一种顺流式锅炉烟气余热回收***， 包括第一、 第二换热器， 所述第一换热器 设于烟道高温侧， 包括吸热段、 和放热段， 所述吸热段、 放热段通过第一管路连接 成循环回路， 所述吸热段设于烟道中； 所述第二换热器设于烟道低温侧， 所述第二 换热器包括第二管路的进口集管、 出口集管； 所述第一、第二换热器通过第三管路 连接， 所述第一换热器的放热段置于第三管路内， 待加热介质流入所述第三管路中 再通过第二换热器的进口集管进入第二换热器并且通过所述第二换热器的出口集 管流出。
优选的， 所述第三管路包括第一支路、 用于流量调节的第二支路， 第一支路和 第二支路并联， 所述第一换热器的放热段置于所述第一支路内。
优选的， 所述第三管路的第二支路上设有调节阀， 所述调节阀的开度由控制装 置控制。 优选的，连接所述第一换热器的吸热段和放热段之间的第一管路上设有温度测 点， 该温度测点将温度信号输送至控制装置。
本发明主要包括两级换热器， 分别为第一换热器和第二换热器， 其中第一换热 器位于烟道中的高温侧， 烟气先与之换热， 第二换热器位于烟道中的低温侧； 本发明的其中第一换热器分为吸热段和放热段两个部分；吸热段安装于锅炉除 尘器后的烟道中， 吸收流经烟气的余热； 吸热段与放热段由管路连接为一闭路循环 ***， 连接管路上接有一循环泵； 管线内介质为强制循环水；
带加热介质（即要加热的低温给水）先去第一换热器的放热段加热， 其中设有 一旁路 （即第二支路）， 旁路上接有一调节阀， 调节旁路给水的流量； 加热后的给 水和旁路来的给水， 汇聚后去第二换热器加热；
本发明的第二换热器为省煤器式的换热器， 分为进出口集管和管束； 第一换热 器放热段及第二支路管路与第二换热器的进口集管相连， 然后连接第二换热器管 束， 要加热的给水走管内与管外的烟气直接换热； 本发明第二换热器材质根据具体 实施的案例可以为耐腐蚀钢， 也可为普通碳钢。
本发明的控制***主要包括一控制装置和安装于强制循环泵出口端的温度测 点， 温度测点测得的温度信号传给控制装置， 控制装置根据所得的温度信号， 控制 调节阀的开度， 实现调节旁路的给水流量。 附图说明
图 1为本发明涉及的顺流式锅炉烟气余热回收***的***原理图。
其巾：
1-控制装置； 2-调节阀； 3-第一换热器放热段； 4-第二换热器出水集管； 5-第二 换热器进水集管； 6-第二换热器管束； 7-第一换热器吸热段； 8-烟道； 9-温度测点； 10-强制循环泵； 11-第一管路； 12-第二管路； 13-第三管路； 14-第一支路； 15-第二 支路
具体实施方式
参见图 1， 为本发明涉及的顺流式锅炉烟气余热回收***的***原理图。 包括 第一、 第二换热器， 所述第一换热器设于烟道 8高温侧， 包括吸热段 7、 和放热段 3， 所述吸热段 7、 放热段 3通过第一管路 11连接成循环回路， 所述吸热段 7设于 烟道 8中； 所述第二换热器设于烟道 8低温侧， 所述第二换热器包括第二管路 12 的进口集管 5、 出口集管 4; 所述第一、 第二换热器通过第三管路 13连接， 所述第 三管路 13包括第一支路 14、 第二支路 15， 所述第一支路 14上设所述第一换热器 的放热段 3， 带加热介质流经所述第一支路 14、 第二支路 15汇合后通过第二换热 器的进口集管 5进入第二换热器再通过第二换热器的出口集管 4流出。所述第三管 路 13的第二支路 15上设有调节阀 2， 所述调节阀 2的开度由控制装置 1控制， 而 在连接所述第一换热器的吸热段 7和放热段 3之间的第一管路 11上设有温度测点 9， 该温度测点 9将温度信号输送至控制装置 1。 所述第一换热器的第一管路 11中 流动强制循环水， 在第一管路 11上设有循环泵 10。 而所述第三管路 13的第一支 路 14、 第二支路 15上都流动着锅炉低温给水。 另外， 所述第二换热器的管束 6与 烟气接触部分的材料为耐腐蚀钢或者普通碳钢。
现对本发明的实施进行阐述； 为了更大程度地降低进入脱硫设备的烟气温度， 回收更多的烟气余热； 本发明分为第一换热器和第二换热器； 分两级换热对烟气进 行余热回收； 第一换热器目的为初步加热锅炉的低温给水， 加热后的低温给水与旁 路 （即第二支路 15) 的给水汇聚， 然后进入第二省煤器式换热器中与烟气换热， 回收烟气余热， 降低进入脱硫设备的烟气温度。
为了方便阐述本发明两个换热器的防腐蚀机理，现以某一具体案例进行分析说 明： 假设某锅炉空预器后的排烟温度为 125°C， 经过除尘器后其温度降为 120°C ; 假设其烟气的酸露点为 90 。C , 水露点温度为 45°C ; 冷凝器出口进低压加热器（或 除氧器）的除盐给水温度为 40°C。锅炉节能改造前， 除尘器后的 12CTC烟气直接进 入脱硫设备中降温脱硫， 然后排放， 造成很大的能量浪费。
技术背景中的种种技术和所列专利， 仅从换热器壁面温度高于酸露点温度出 发， 对烟气进行余热回收， 因此烟气酸露点温度为 90°C时， 加上传热温差等因素， 经此节能改造后， 其排烟温度约 11CTC左右， 节能改造空间只有 10°C， 因此降温节 能投资效益不明显。
本发明做法为分两个换热器， 其中第一换热器对 40°C除盐给水进行预加热； 第一换热器分为吸热段 7和放热段 3两个部分， 吸热段 7吸收烟气的余热， 把它传 递给流经的强制循环水， 循环水再在放热段 3把热量传递给 40°C除盐给水， 通过 调节旁路调节阀 2的开度来控制旁路除盐给水的流量，间接地控制了第一换热器放 热段 3的传热量，从而控制了第一换热器放热段 3与吸热段 Ί闭路循环中强制循环 水的温度， 达到了第一换热器吸热段 7免受酸露腐蚀的目的； 正如前述的种种技术 一样， 第一换热器最大节能空间为 10°C左右， 其排烟温度约为 11CTC左右；
这样可以把 40°C部分除盐给水加热至某一温度， 通过布置合理的受热面， 可 以把混合后的除盐水温度控制在 45°C左右， 若烟气的水露点温度为 42°C， 可调大 旁路流量， 使第一换热器放热段 3的换热量减少， 此时第一换热器吸热段 7的排烟 温度会高于 （或者等于） 110°C。
由第一换热器过来混合后的除盐水温约为烟气的水露点温度 45 °C， 此时进入 第二省煤器式换热器中直接与烟气换热（应保证通过第二换热器的进口集管 5进入 第二换热器的流动介质温度为烟气的水露点温度）， 我们知道此时省煤器式换热器 与烟气接触侧的壁面温度约为流经除盐水的温度 +5°C左右；因此此时第二换热器的 壁面温度为 50°C左右， 高于烟气的水露点温度， 假设烟气降至 70°C， 总的吸热量 可使除盐水的温升为 20°C， 因此除盐水的出口温度 65°C ; 这样第二换热器的与烟 气接触侧的壁面温度区间为 50~70°C， 虽然避免了烟气水露点附近的酸露腐蚀， 然 而第二换热器部分壁温可能落在酸露点以下 20~30°C区域的严重腐蚀区域， 对于这 部分第二换热器管束 6采用耐腐蚀钢， 或者调整总的节能量， 总之结合锅炉的具体 型号、 烟气的酸露点、 烟气的水露点等因素综合考量， 得出最优节能方案。

Claims

权利要求书
1. 一种顺流式锅炉烟气余热回收***， 其特征是包括第一、 第二换热器， 所述 第一换热器设于烟道（8) 高温侧， 包括吸热段（7)、 和放热段 （3)， 所述吸 热段（7)、放热段（3)通过第一管路（11 )连接成循环回路， 所述吸热段（7) 设于烟道 （8) 中； 所述第二换热器设于烟道 （8 ) 低温侧， 所述第二换热器 包括第二管路 （12) 的进口集管 （5 )、 出口集管 （4); 所述第一、 第二换热 器通过第三管路（ 13)连接，所述第一换热器的放热段（3)置于第三管路（ 13) 内，待加热介质流入所述第三管路（13)中再通过第二换热器的进口集管（5) 进入第二换热器并且通过所述第二换热器的出口集管 （4) 流出。
2. 根据权利要求 1所述的顺流式锅炉烟气余热回收***， 其特征是： 所述第三 管路 （13) 包括第一支路 （14)、 用于流量调节的第二支路 （15 )， 第一支路
( 14)和第二支路（15)并联， 所述第一换热器的放热段（3)置于所述第一 支路 （14) 内。
3. 根据权利要求 2所述的顺流式锅炉烟气余热回收***， 其特征是： 所述第三 管路 （13) 的第二支路 （15)上设有调节阀 （2)， 所述调节阀 （2) 的开度由 控制装置 （1 ) 控制。
4. 根据权利要求 3所述的顺流式锅炉烟气余热回收***， 其特征是： 连接所述 第一换热器的吸热段 （7) 和放热段 （3) 之间的第一管路 （11 ) 上设有温度 测点 （9)， 该温度测点 (9) 将温度信号输送至控制装置 ( Do
5. 根据权利要求 1所述的顺流式锅炉烟气余热回收***， 其特征是： 所述第一 换热器的第一管路 （11 ) 中流动强制循环水。
6. 根据权利要求 1所述的顺流式锅炉烟气余热回收***， 其特征是： 所述待加 热介质为锅炉低温给水。
7. 根据权利要求 1所述的顺流式锅炉烟气余热回收***， 其特征是： 所述第二 换热器的管束 （6) 与烟气接触部分的材料为耐腐蚀钢。
8. 根据权利要求 1或 4所述的顺流式锅炉烟气余热回收***， 其特征是： 所述 第二换热器的管束 （6) 与烟气接触部分的材料为普通碳钢。
PCT/CN2013/076917 2012-07-06 2013-06-07 顺流式锅炉烟气余热回收*** WO2014005476A1 (zh)

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