CN118517695A - Waste incineration waste heat boiler system and control method thereof - Google Patents
Waste incineration waste heat boiler system and control method thereof Download PDFInfo
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- CN118517695A CN118517695A CN202410736654.4A CN202410736654A CN118517695A CN 118517695 A CN118517695 A CN 118517695A CN 202410736654 A CN202410736654 A CN 202410736654A CN 118517695 A CN118517695 A CN 118517695A
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- 239000002918 waste heat Substances 0.000 title claims abstract description 60
- 238000004056 waste incineration Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 128
- 239000003546 flue gas Substances 0.000 claims abstract description 128
- 238000002485 combustion reaction Methods 0.000 claims abstract description 40
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 239000002253 acid Substances 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 41
- 239000001301 oxygen Substances 0.000 claims description 41
- 229910052760 oxygen Inorganic materials 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 239000000779 smoke Substances 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 229910052717 sulfur Inorganic materials 0.000 claims description 6
- 239000011593 sulfur Substances 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 3
- 238000012937 correction Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 39
- 238000005260 corrosion Methods 0.000 abstract description 9
- 230000007797 corrosion Effects 0.000 abstract description 9
- 238000013461 design Methods 0.000 abstract description 6
- 238000000605 extraction Methods 0.000 abstract description 6
- 230000009286 beneficial effect Effects 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 230000001276 controlling effect Effects 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000004868 gas analysis Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 206010022000 influenza Diseases 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
-
- 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
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements or dispositions of combustion apparatus
- F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B35/00—Control systems for steam boilers
- F22B35/007—Control systems for waste heat boilers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
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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)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Air Supply (AREA)
Abstract
The invention provides a waste incineration waste heat boiler system and a control method thereof, and by the structural design of the waste incineration waste heat boiler system, flue gas of a waste heat boiler can be effectively utilized to heat primary air, the temperature of mixed primary air is ensured to be above an acid dew point temperature, and the problem of low-temperature corrosion existing in the prior art that the flue gas of the waste heat boiler is utilized to heat the primary air is solved. Meanwhile, the steam extraction amount required by heating the primary air by using the steam extracted from the boiler or the steam turbine in the prior art is saved, the generated energy or the external steam supply amount is increased by the saved steam extraction amount, the recycling rate of the garbage incineration treatment is improved, the manufacturing cost and the equipment occupation space of the air preheater for heating the primary air by the steam are reduced, and the flow resistance of air is reduced. The method ensures the effective and stable combustion of the garbage, is beneficial to creating a local reducing atmosphere in the garbage incineration process, realizes the control of the generation of nitrogen oxides in the combustion process, and reduces the cost of removing the nitrogen oxides by the flue gas.
Description
Technical Field
The invention relates to the technical field of energy environmental protection, in particular to a waste incineration waste heat boiler system and a control method thereof.
Background
With the development of society, more and more garbage is generated, such as household garbage, construction garbage and the like. The way of disposing of the waste includes landfill and incineration. The traditional landfill method can not cope with the challenges of increasing the quantity of urban garbage caused by the process of urban and industrialized China. In order to solve the problem, china is rapidly popularized and applied to garbage incineration and waste heat power generation projects as an alternative scheme. The treatment mode has the remarkable advantages of harmlessness, reduction and recycling. Through high-temperature incineration, the garbage can be effectively treated, so that the pollution to the environment is reduced. In addition, the incineration can convert garbage into energy, such as power generation or heat supply, so that the recycling of resources is realized, and the dependence on the traditional energy is reduced.
However, unlike conventional fossil fuels such as coal, fuel oil and gas, the urban household garbage has complex components, the combustion products of garbage incineration contain a large amount of corrosive acid gases, and the water vapor content, the NOx content and the oxygen concentration in the flue gas are high.
The flue gas characteristics of waste incineration lead to a heating surface arrangement for flue gas heat utilization which is also different from that of a traditional fossil fuel boiler. The tail flue of all coal-fired power plant boilers is provided with an air preheater behind the economizer, the flue gas releases heat to the water supply of the boiler through a heating surface pipe of the economizer and reduces the temperature after entering the economizer, then the flue gas enters the air preheater, the temperature of the flue gas is reduced to about 120 ℃ after the flue gas releases heat to the air through the heating surface pipe of the air preheater, and most of waste heat resources of the flue gas are utilized by the economizer and the air preheater.
However, for the waste incineration waste heat boiler, in order to avoid the problem of low-temperature corrosion caused by dew condensation of acid gas in flue gas on the surface of a low-temperature heating surface, only the economizer is arranged on the final heating surface of a tail flue of the waste heat boiler, and an air preheater is not arranged. The inlet water temperature of the economizer is generally 130 ℃ and is far higher than the normal-temperature air temperature of the inlet of the air preheater, and a certain temperature difference is needed for heat exchange between flue gas and hot water in the economizer, so that the exhaust gas temperature of the outlet of the economizer is far higher than the exhaust gas temperature of the outlet of the air preheater of the coal-fired power plant and is generally 190-250 ℃, and the exhaust gas heat loss of the waste incineration waste heat boiler is far higher than that of the coal-fired power plant boiler.
As the air coefficient in the garbage incineration process is generally higher than that of the coal-fired power station boiler, the volume of smoke discharged by garbage incineration and the smoke discharging heat loss of the waste heat boiler are further increased. Because the water content of the garbage is high and the heat value is low, the primary air temperature of garbage incineration needs to be increased in order to realize stable combustion of the garbage. Because the tail flue cannot be provided with the air preheater, the waste incineration exhaust heat boiler generally adopts the extraction steam of the boiler steam drum and the first-stage extraction steam of the steam turbine as heat sources for heating primary air to heat the primary air to more than 200 ℃, and the primary air heating mode consumes precious steam resources, so that the generated energy of a waste combustion power plant or external heat supply is reduced. The existing garbage incineration system adopts an air preheater as heat exchange equipment for heating primary air by steam, and needs larger heat exchange area for heating the normal-temperature primary air to a set temperature value, thereby not only increasing occupied space, but also needing larger initial investment; in addition, the primary air flows through the air preheater to overcome larger resistance, so that the power consumption and the operation and maintenance cost of the primary air fan are increased.
In addition, compared with a coal-fired boiler, the air coefficient in the garbage incineration process is larger, the nitrogen content of garbage is generally higher than that of coal, so that the concentration of NOx in flue gas generated by garbage incineration is high, and more environmental protection treatment problems are caused.
The problems which are difficult to solve by the existing garbage incineration system are all solved.
Disclosure of Invention
In order to solve the problems caused by that only an economizer is arranged on the final heating surface of the tail flue of the existing waste incineration waste heat boiler and an air preheater is not arranged any more in the background art, the invention provides a waste incineration waste heat boiler system which comprises a primary air flue, a circulating flue, a waste heat boiler flue and a combustion chamber;
The inlet of the circulating flue is connected with a low-temperature circulating flue, and the low-temperature circulating flue is connected with a waste heat boiler flue; the inlet of the circulating flue is also connected with a high-temperature circulating flue, and the high-temperature circulating flue is connected with a waste heat boiler flue;
the inlet of the primary air channel is connected with the primary air fan; the primary air channel is also connected with an air preheater;
the inlet of the steam-water side of the air preheater is also connected with a steam pipeline of the air preheater for heating, and the outlet of the steam-water side of the air preheater is connected with a drain pipeline of the air preheater; the steam pipeline of the air preheater is connected with the steam drum through a saturated steam eduction tube;
The outlet of the primary air channel is connected with the outlet of the circulating flue and is converged in the mixed primary air channel, and the mixed primary air channel is connected with the air chamber at the lower part of the combustion chamber;
The flue inlet of the waste heat boiler is connected with the flue gas outlet of the combustion chamber; an evaporator, a superheater and an economizer are arranged in the waste heat boiler flue, and the economizer is arranged at the last section of the flue gas flow in the waste heat boiler flue; the waste heat boiler flue is provided with a flue outlet; the evaporator is connected with the steam drum through a steam-water circulating pipe; the superheater inlet is connected with a superheated steam pipeline, and the superheated steam pipeline is connected with the steam drum through a saturated steam outlet pipe; the outlet of the economizer is connected with the steam drum through a water supply pipe.
On the basis of the technical scheme, a primary air flowmeter is further arranged in the primary air duct, and a primary air thermometer is arranged in the primary air duct of the air preheater outlet; and a superheated steam flowmeter is arranged in the inlet pipeline of the superheater.
Based on the technical scheme, further, the oxygen concentration range in the mixed primary air duct is 15-18%, and the temperature range in the mixed primary air duct is 130-210 ℃.
On the basis of the technical scheme, a second circulating flue is further arranged, so that the second circulating flue is arranged on the circulating flue and is connected with the combustion chamber through a circulating air port arranged on the upper portion of the fire grate, and a circulating flue baffle is arranged on the second flue.
On the basis of the technical scheme, further, a heating steam regulating valve and a heating steam flowmeter are arranged on the steam pipeline of the air preheater.
On the basis of the technical scheme, a mixed primary air thermometer is further arranged on the mixed primary air duct;
and a smoke circulating fan and a dust remover are arranged on the circulating flue, and a circulating smoke thermometer and a circulating flue baffle are arranged on a communication pipeline between the smoke fan outlet and the mixed primary air flue.
On the basis of the technical scheme, the low-temperature circulating flue is further provided with a low-temperature circulating flue gas flowmeter and a low-temperature circulating flue gas baffle, a connection port of the low-temperature circulating flue and the waste heat boiler flue is positioned at the rear side of the economizer, and a low-temperature flue gas thermometer is arranged at the connection port;
The high-temperature circulating flue is provided with a high-temperature circulating flue gas flowmeter and a high-temperature circulating flue gas baffle, a connecting port of the high-temperature circulating flue gas and the waste heat boiler flue is positioned at the front side of the economizer, and a high-temperature flue gas thermometer is arranged.
The invention also provides a control method of the waste incineration waste heat boiler system, which is used for controlling the primary air flow in the mixed primary air duct so as to ensure that:
V1A＝COE1A×FSTM；
Wherein,
V 1A is the running primary air flow, nm 3/s;V1A is measured and displayed by the primary air flow meter;
F STM is the steam yield of the waste heat boiler, and the unit is kg/s; measured and displayed by a superheated steam flow meter;
COE 1A is the primary air steam coefficient, the unit is Nm 3/kg, and is the ratio of the primary air flow V 1A of the operation of the incinerator to the steam flow F STM of the waste heat boiler, and the range of the steam coefficient is 0.70-1.15 Nm 3/kg.
On the basis of the technical scheme, further, the primary air oxygen volume concentration in the mixed primary air duct is controlled so that:
Wherein:
O mix is the volume concentration of the oxygen of the mixed primary air,%;
V 1A is the running primary air flow, nm 3/h;
v HG is the flow rate of high-temperature circulating flue gas, nm 3/s; measuring by a high-temperature circulating flue gas flowmeter;
V LG is the low-temperature circulating smoke flow, nm 3/s; measured by a low temperature circulating flue gas flowmeter;
O Rec is the volume concentration of oxygen in the circulating flue and ranges from 3% to 10%; measured by an on-line flue gas analysis system in%.
On the basis of the above technical scheme, further, the primary air temperature t aim,1Amix in the mixed primary air duct is controlled so that:
taim,1Amix＝tadp,1Amix+tS,Cor+tyl；
Wherein,
T aim,1Amjx is the temperature of the target mixed primary air, and the temperature is lower than the temperature;
t adp,1Amix is the acid dew point temperature of the mixed primary air, in degrees centigrade, which can be calculated by any of the following formulas:
tadp,1Amix＝18.0×Mar+134.83；
Wherein M ar is the mass percent of the water content of the base received by the garbage in the furnace;
t S,Cor the fuel sulfur content correction factor, in degrees Celsius, can be calculated from the following equation:
tS,Cor＝65.46×Sar-6.42；
S ar is the mass percent of the sulfur content of the received base of the garbage in the furnace;
t yl is the margin, and the value range is 2-15 ℃.
Based on the technical scheme, further, the oxygen concentration range in the mixed primary air duct is 15-18%, and the temperature range in the mixed primary air duct is 130-210 ℃.
The waste incineration waste heat boiler system and the control method provided by the invention have the following beneficial effects:
By the structural design of the waste incineration waste heat boiler system, part of flue gas is extracted to be used as a heat source of primary air, the primary air is heated in a mixed heating mode, and the problems of low-temperature corrosion of a heating surface caused by the fact that the air preheater is used as heat exchange equipment for heating the primary air by utilizing steam in the prior art are solved; if a larger heat exchange area is needed for heating the normal-temperature primary air to the set temperature value, the volume of the air preheater is increased, so that the occupied space is increased, and the problem of larger cost is also solved.
In the preferred technical scheme, the waste incineration waste heat boiler system can also extract two paths of flue gas with different temperatures to mix with primary air through the layout of the structure and the design of the control method, simultaneously realize the control of the temperature target and the oxygen concentration target of the mixed primary air, prevent the problem of low-temperature corrosion of the mixed primary air duct, the air chamber and the fire grate, control the optimal mixed primary air oxygen concentration, effectively reduce the generation control of the combustion process of the waste incineration nitrogen oxides, and reduce the control cost of the nitrogen oxides and the exceeding emission risk.
Other technical effects of the technical scheme provided by the invention will be further described in connection with the embodiments of the invention.
Drawings
Fig. 1 is a schematic diagram of a process flow of the garbage incineration waste heat boiler system.
Reference numerals:
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
The invention provides an embodiment of a waste incineration waste heat boiler system, which is shown in fig. 1, and comprises a primary air duct 100, a circulating flue 200, a waste heat boiler flue 300 and a combustion chamber 400; the inlet of the circulating flue 200 is connected with a low-temperature circulating flue 232, and the low-temperature circulating flue 232 is connected with a waste heat boiler flue 300; the inlet of the circulating flue 200 is also connected with a high-temperature circulating flue 242, and the high-temperature circulating flue 242 is connected with the waste heat boiler flue 300; the inlet of the primary air duct 100 is connected with a primary air fan 140; the primary air duct 100 is also connected with an air preheater 150; the inlet of the steam water side of the air preheater 150 is also connected with an air preheater steam pipeline 160 for heating, and the outlet is connected with an air preheater drain pipeline 130; the air preheater steam line 160 is connected to the drum 320 via a saturated steam exit line 333; the outlet of the primary air duct 100 is connected with the outlet of the circulating flue 200 and is converged into a mixed primary air duct 450, and the mixed primary air duct 450 is connected with an air chamber 440 at the lower part of the combustion chamber 400; the inlet of the waste heat boiler flue 300 is connected with the flue gas outlet of the combustion chamber 400; an evaporator 310, a superheater 330 and an economizer 340 are arranged in the exhaust-heat boiler flue 300, and the economizer 340 is arranged at the last section of the flow of the flue gas in the exhaust-heat boiler flue 300; the waste heat boiler flue 300 is provided with a flue outlet 350; the evaporator 310 is connected with the steam drum 320 through a steam-water circulation pipe 315; the inlet of the superheater 330 is connected with a superheated steam pipeline 336, and the superheated steam pipeline 336 is connected with the steam drum 320 through a saturated steam outlet pipe 333; the outlet of the economizer 340 is connected to the drum 320 through a feed pipe 341.
Preferably, a primary air flowmeter 110 is disposed in the primary air duct 100, and a primary air thermometer 105 is disposed in the primary air duct 100 at the outlet of the air preheater 150; a superheated steam flow meter 338 is disposed within the inlet conduit of the superheater 330.
Preferably, the oxygen concentration in the primary mixing air duct 450 ranges from 15% to 18%, and the temperature in the primary mixing air duct 450 ranges from 130 ℃ to 210 ℃.
In a preferred embodiment, a second circulation flue 413 is further provided, so that the second circulation flue 413 is disposed on the circulation flue 200 and is connected to the combustion chamber 400 through a circulation air port 417 disposed at an upper portion of the fire grate 420, and a circulation flue baffle 415 is disposed on the second flue 413. The circulating flue gas may also enter the combustion chamber 400 through the second circulating flue 413 from the circulating tuyere 417 above the combustion chamber 400.
Preferably, a heating steam adjusting valve 170 and a heating steam flowmeter 180 are disposed on the air preheater steam conduit 160.
Further, a primary air mixing thermometer 460 is disposed on the primary air mixing duct 450;
The circulating flue 200 is provided with a flue gas circulating fan 210 and a dust remover 220, and a circulating flue gas thermometer 203 and a circulating flue gas baffle 206 are arranged on a communication pipeline between the outlet of the flue gas fan 210 and the mixed primary air flue 450.
More preferably, the low-temperature circulating flue 232 is provided with a low-temperature circulating flue flowmeter 231 and a low-temperature circulating flue baffle 233, and a connection port of the low-temperature circulating flue 232 and the waste heat boiler flue 300 is positioned at the rear side of the economizer 340, and a low-temperature flue thermometer 234 is arranged at the connection port;
The high-temperature circulating flue 242 is provided with a high-temperature circulating flue gas flowmeter 241 and a high-temperature circulating flue gas baffle 243, and a high-temperature flue gas thermometer 244 is provided at the front side of the economizer 340 where the connection port between the high-temperature circulating flue 242 and the waste heat boiler flue 300 is located.
Preferably, a flue gas circulation system purge door 120 is further disposed between the primary air duct 100 and the circulation flue 200.
Preferably, the tail end of the exhaust-heat boiler flue 300 is further provided with an online flue gas analysis system 355.
Other optional structures in the embodiment of the waste incineration exhaust heat boiler system are shown in fig. 1, and in addition, other optional instruments or equipment can be added by a person skilled in the art on the basis of the innovative technical scheme of the invention.
With reference to fig. 1, the working flow of the garbage incineration waste heat boiler system provided by the invention is as follows:
Household garbage from the garbage pool enters the fire grate 420 at the lower part of the combustion chamber 400 through the garbage feeder 430. The hot flue gas of the circulating flue 200 is mixed with the primary air from the primary air duct 100 in the mixed primary air duct, the mixed primary air is mixed and heated, the heated mixed primary air enters the combustion chamber 400 from the lower part of the fire grate 420 through the air chamber 440, and is incompletely combusted with the garbage on the upper part of the fire grate, so that a local reducing atmosphere is formed, nitrogen element in the garbage generates nitrogen under the condition of lacking enough free oxygen atoms, and the generation concentration of nitrogen oxides is reduced. Wherein, the local reducing atmosphere controls the oxygen concentration in the primary air duct 450 to be 15-18%, and the temperature in the primary air duct 450 to be 130-210 ℃ and the oxygen concentration are formed under the cooperation of the two conditions.
Because the household garbage is different from the fire coal, most combustible matters in the household garbage enter the combustion chamber and are released into the combustion chamber in a volatile manner, and the local reducing atmosphere is favorable for reducing the generation of nitrogen oxides. As the household garbage moves backward on the grate 420 and gradually completes combustion, the residue after combustion is discharged out of the combustion chamber through a slag discharge port arranged at the tail of the grate.
In order to achieve that the lower part of the combustion chamber 400 is in a reducing atmosphere, the volatile matters released from the household garbage do not achieve complete combustion, and these volatile matters flow toward the upper part of the combustion chamber 400 along with the combustion products. The secondary air entering the combustion chamber 400 from the upper portion of the grate 420 through the secondary air duct 410 provides a sufficient amount of oxygen as the burn-up air, which is further mixed with the volatile components of the unburned ashes in the combustion products for combustion, wherein the carbon element is fully oxidized and converted into carbon dioxide, the hydrogen element is fully oxidized and converted into water, and the heat energy is fully released.
The combustion products (i.e., flue gas) completely combusted and sufficiently released heat energy enter the exhaust-heat boiler stack 300 from the outlet of the upper portion of the combustion chamber 400, exchange heat with the evaporator 310, the superheater 330 and the economizer 340 disposed in the exhaust-heat boiler stack 300 as the flue gas moves toward the stack outlet 350, and gradually heat the boiler feed water entering the economizer into superheated steam. After the heat release, the temperature of the flue gas at the outlet of the economizer 340 is reduced to about 180 ℃ to 250 ℃. Unlike conventional coal-fired boilers, the waste incineration flue gas has strong pollution adhesion and corrosiveness, so that the waste incineration exhaust-heat boiler gradually increases the exhaust gas temperature at the outlet of the economizer 340 along with the extension of the operation time. In the technical scheme of the invention, in order to avoid the problem of low-temperature corrosion, the outlet of the economizer is not provided with an air preheater, so that the cost and the equipment space are greatly saved.
The supply of cold primary air from the lower portion of the grate 420 is not conducive to the stable combustion of household garbage. According to the invention, the low-temperature circulating flue 232 is arranged at the flue at the rear end of the economizer, the high-temperature circulating flue 242 is arranged at the flue at the front end of the economizer, and the low-temperature flue gas and the high-temperature flue gas are led out from the waste heat boiler flue 300 through the two flues to serve as heat sources of primary air, and the primary air is heated in a mode of being mixed with the primary air. The temperature of the low-temperature flue gas and the high-temperature flue gas is higher than that of the primary air, and the oxygen concentration of the low-temperature flue gas and the high-temperature flue gas is lower than that of the primary air. Therefore, the mixture of the flue gas and the primary air after mixing is called a mixed primary air, the temperature of the mixed primary air is higher than that of the primary air, and the oxygen content of the mixed primary air is lower than that of the primary air.
Some preferred operating principles of embodiments of the present invention are as follows:
1. different from the existing dividing wall type heating mode, the flue gas and the primary air are mixed to heat the primary air, the area where the flue gas temperature, the air temperature and the pipe wall temperature at the outlet of the air preheater are the lowest does not exist, and the problem of low-temperature corrosion of a heating surface at the lowest temperature does not exist.
2. The acid dew point temperature of the flue gas is related to the concentration of the acid gas and the concentration of the water vapor in the flue gas, and the higher the concentration, the higher the acid dew point temperature, i.e., the higher the dew point temperature of the acid gas. According to the invention, through creative design, the flue gas is mixed with the primary air, although the temperature of the mixed primary air is reduced compared with the temperature of the flue gas before mixing, the risk of dew formation of the acid gas is increased; however, the concentration of the acid gas and the water vapor mixed with the primary air is also remarkably reduced, and the risk of condensation of the acid gas is reduced.
3. The flue gas and the primary air are mixed to heat the primary air, and although the factors of increasing and reducing the dew formation risk of the acid gas of the mixed primary air exist at the same time, the invention further takes measures to ensure that the mixed primary air does not generate the dew formation of the acid gas. The specific design concept is to take into consideration that the temperature change of the flue gas at the outlet of the economizer is larger in the operation process of the waste incineration waste heat boiler, and in order to ensure that the temperature of the mixed primary air is higher than the acid dew point temperature of the flue gas, two different-temperature flue gas is extracted from the flue at the outlet position of the flue gas of the economizer and the flue at the inlet end of the flue gas of the economizer for mixing, so that the adjusting range of the temperature of the mixed primary air is increased, the temperature of the mixed primary air is ensured to be higher than the acid dew point temperature of the flue gas, and the corrosion of the mixed primary air flue, the air chamber and the fire grate caused by the dew formation of the acid gas of the mixed primary air is avoided.
In addition, existing garbage incineration processes produce large amounts of atmospheric pollutant nitrogen oxides. In order to realize standard emission of nitrogen oxides in flue gas, the prior art needs to perform denitration treatment, including SNCR denitration treatment and SCR denitration treatment, on the waste incineration flue gas, so that initial investment cost and operation cost of environmental protection facilities are necessarily increased. According to the invention, through the creative design of the system structure, part of the flue gas is extracted to be mixed with the primary air, so that the temperature of the mixed primary air is increased, the primary air is heated, the problem of low-temperature corrosion caused by acid gas condensation of the mixed primary air is avoided, the oxygen concentration of the mixed primary air is reduced, the ratio of the circulating flue gas amount to the primary air amount is adjusted, and the oxygen concentration of the mixed primary air can be effectively adjusted. Reducing the oxygen concentration of the mixed primary air is beneficial to creating a local reducing atmosphere in a garbage incineration area at the upper part of the fire grate, and reducing nitrogen oxides generated by immediate incineration into nitrogen. Therefore, the technical scheme of the invention reduces the generation of nitrogen oxides in the garbage incineration process, and reduces the pressure and cost of flue gas denitration.
According to the waste incineration waste heat boiler system provided by the embodiment of the invention, on one hand, the generation concentration of nitrogen oxides is reduced, and on the other hand, the problems of strong pollution and corrosiveness of waste incineration flue gas can be solved without using an air preheater, and meanwhile, the problems of space occupation and high cost caused by adopting the air preheater in the prior art are avoided.
Example 2
The invention also provides a control method embodiment of the garbage incineration waste heat boiler system, which specifically comprises the following control scheme:
1. controlling the primary air flow in the mixed primary air duct so that:
V1A＝COE1A×FSTM；
Wherein,
V 1A is the operational primary air flow, nm 3/s;V1A is measured and displayed by primary air flow meter 110;
f STM is the steam yield of the waste heat boiler, and the unit is kg/s; measured and displayed by superheated steam flow meter 338;
COE 1A is the primary air steam coefficient, the unit is Nm 3/kg, and is the ratio of the primary air flow V 1A of the operation of the incinerator to the steam flow F STM of the waste heat boiler, and the range of the steam coefficient is 0.70-1.15 Nm 3/kg.
2. Controlling the primary air oxygen volume concentration in the mixed primary air duct so that:
Wherein:
O mix is the volume concentration of the oxygen of the mixed primary air,%;
V 1A is the running primary air flow, nm 3/h;
V HG is the flow rate of high-temperature circulating flue gas, nm 3/s; measured by a high temperature circulating flue gas flow meter 241;
V LG is the low-temperature circulating smoke flow, nm 3/s; measured by the low temperature circulating flue gas flow meter 231;
O Rec is the volume concentration of oxygen in the circulating flue and ranges from 3% to 10%; measured in% by an on-line flue gas analysis system 355.
3. The primary air temperature t aim,1Amix in the mixed primary air duct is controlled so that:
taim,1Amix＝tadp,1Amix+tS,Cor+tyl；
Wherein,
T aim,1Amix is the temperature of the target mixed primary air, and the temperature is lower than the temperature;
t adp,1Amix is the acid dew point temperature of the mixed primary air, in degrees centigrade, which can be calculated by either of the following two formulas:
tadp,1Amix＝18.0×Mar+134.83；
Wherein M ar is the mass percent of the water content of the base received by the garbage in the furnace;
t S,Cor the fuel sulfur content correction factor, in degrees Celsius, can be calculated from the following equation:
tS,Cor＝65.46×Sar-6.42；
S ar is the mass percent of the sulfur content of the received base of the garbage in the furnace;
t yl is the margin and the value range is 2-15 ℃.
Preferably, the oxygen concentration in the primary mixing air duct 450 ranges from 15% to 18%, and the temperature in the primary mixing air duct 450 ranges from 130 ℃ to 210 ℃.
In this embodiment, taking a waste incineration exhaust heat boiler system with a steam production of 72 tons/hour as an example, according to the target temperature and the target oxygen concentration requirement of the mixed primary air, the control method of the reference embodiment 2 is implemented by controlling the flow rates of different flue gas oxygen concentrations, different low-temperature flue gas temperatures and different high-temperature flue gas temperatures. The method comprises the following steps:
Example 2.1 control procedure of exhaust gas temperature
The concentration of mixed primary air oxygen is required to be controlled at 16.5%, and the temperature is controlled at 145 ℃; when the oxygen concentration of the flue gas is 5%, and when the temperature of the low-temperature flue gas is increased from 200 ℃ to 235 ℃, and the temperature of the corresponding high-temperature flue gas is increased from 350 ℃ to 385 ℃, the flow rate of the low-temperature circulating flue gas entering the circulating flue gas 200 is increased from 5.05Nm 3/s to 6.84Nm 3/s, and the flow rate of the high-temperature circulating flue gas entering the circulating flue gas 200 is correspondingly decreased from 2.70Nm 3/s to 0.91Nm 3/s. The specific changes are shown in Table 1.
Example 2.2 control procedure of mixing Primary air oxygen concentration
The temperature of the mixed primary air is controlled at 145 ℃; when the oxygen concentration of the flue gas is 5%, the temperature of the low-temperature circulating flue gas is 200 ℃, the temperature of the high-temperature circulating flue gas is 350 ℃, and the mixed primary air oxygen concentration is required to be increased from 15.5% to 17.5%, the flow rate of the low-temperature circulating flue gas entering the circulating flue gas 200 is reduced from 8.71Nm 3/s to 1.97Nm 3/s, and correspondingly, the flow rate of the high-temperature circulating flue gas entering the circulating flue gas 200 is increased from 1.66Nm 3/s to 3.57Nm 3/s. The specific changes are shown in Table 2.
EXAMPLE 2.3 control procedure of Mixed Primary air temperature
When the oxygen concentration of the flue gas is 5%, the temperature of the low-temperature circulating flue gas is 200 ℃, the temperature of the high-temperature circulating flue gas is 350 ℃, when the mixed primary air oxygen concentration is required to be 18%, the temperature of the mixed primary air is controlled to be increased from 120 ℃ to 140 ℃, the flow rate of the low-temperature circulating flue gas entering the circulating flue 200 is reduced from 4.35Nm 3/s to 1.36Nm 3/s, and correspondingly, the flow rate of the high-temperature circulating flue gas entering the circulating flue 200 is increased from 0.22Nm 3/s to 3.21Nm 3/s. The specific changes are shown in Table 3.
Example 2.4 control procedure of flue gas oxygen concentration
The concentration of mixed primary air oxygen is required to be controlled at 17.5%, and the temperature is controlled at 145 ℃; when the temperature of the low-temperature flue gas is 200 ℃, the temperature of the high-temperature flue gas is 350 ℃, the oxygen concentration of the flue gas is increased to 8%, the flow rate of the low-temperature circulating flue gas entering the circulating flue gas 200 is increased from 0.90Nm 3/s to 3.44Nm 3/s, and correspondingly, the flow rate of the high-temperature circulating flue gas entering the circulating flue gas 200 is decreased from 3.88Nm 3/s to 3.15Nm 3/s. The specific changes are shown in Table 4.
TABLE 1
TABLE 2
TABLE 3 Table 3
TABLE 4 Table 4
The above examples show that even if the oxygen concentration and the temperature of the flue gas of the waste heat boiler flues fluctuate to a certain extent, the temperature of the mixed primary air and the oxygen concentration can be effectively controlled by controlling the flow of the high-temperature circulating flue gas and the flow of the low-temperature circulating flue gas. The combined control method and the preferable scheme of the waste incineration waste heat boiler system have the following technical effects:
(1) The temperature of the mixed primary air is ensured to be above the acid dew point temperature, the flue gas of the boiler is effectively utilized to heat the primary air, and the problem of low-temperature corrosion existing in the prior art that the flue gas of the waste heat boiler is utilized to heat the primary air is effectively solved. The method saves the extraction quantity required by the prior art for heating the primary air by utilizing the extraction steam of the boiler or the steam turbine, and improves the generated energy of the part of steam or the external steam supply quantity. Improves the recycling rate of the garbage incineration treatment.
(2) Further, the manufacturing cost of the air preheater for heating the primary air by steam is reduced, the occupied space is occupied, and the power consumption of the primary air blower is reduced by the flowing resistance of air.
(3) The mixed primary air entering the combustion chamber from the lower part of the fire grate has controllable oxygen concentration, ensures the effective and stable combustion of the garbage, is beneficial to controlling the local reducing atmosphere in the garbage incineration process, and effectively reduces the generation of nitrogen oxides and the concentration of the nitrogen oxides in combustion products.
In the technical scheme of the invention, if the heat value of the primary air is required to be obtained, the relation between the heat value of the high-temperature circulating smoke and the heat value of the low-temperature circulating smoke and the heat value of the mixed primary air is calculated by the following formula:
Q1A+QHG+QLG＝Q1Amix；
Wherein:
Q 1Amix is the heat value of the mixed primary air, kW;
Q 1A is the heat value of primary air, Q HG is the heat value of high-temperature circulating smoke, Q LG is the heat value of low-temperature circulating smoke, kW
The heat value Q 1A of the primary air is calculated by the following formula
Q1A＝V1A×K1A×t1A；
Wherein: k 1A is the specific heat of the primary air in kJ/(Nm 3 X ℃ C.), is a function of the primary air temperature t 1A, and can be calculated by the following formula:
K1A＝1.2945+6.1408×10-5×t1A；
t 1A is the primary air temperature in degrees centigrade, which can be measured and displayed by the primary air thermometer 105;
Q 1G and Q LG are the heat value of the high-temperature circulating smoke and the heat value of the low-temperature circulating smoke, and can be calculated by the following formulas:
QHG＝VHG×KHG×tHG；
QLG＝VLG×KLG×tLG；
K HG is the specific heat of the high-temperature circulating flue gas, the unit is kJ/(Nm 3 ×) and is a function of the temperature t HG of the high-temperature circulating flue gas, and can be calculated by the following formula:
KHG＝1.373+1.703×10-4×tHG；
t HG is the high temperature circulating flue gas temperature in degrees centigrade, which can be measured and displayed by the high temperature flue gas thermometer 244;
K LG is the specific heat of the low-temperature circulating flue gas, the unit is kJ/(Nm 3 ×) and is a function of the low-temperature circulating flue gas temperature t HG, and can be calculated by the following formula:
KLG＝1.373+1.703×10-4×tLG；
t LG is the low temperature circulating flue gas temperature in degrees celsius, which can be measured and displayed by the low temperature flue gas thermometer 234;
the heating value Q 1Amix of the mixed primary air is calculated by the following formula:
Q1Amix＝V1Amix×K1Amix×t1Amix；
wherein: k 1A mix is the specific heat of the mixed primary air in kJ/(Nm 3 ×) and is a function of the primary air temperature t 1Amix, and can be calculated by the following formula:
K1Amix＝1.325+9.820×10-5×t1Amix；
t 1Amix is the mixed primary air temperature in degrees celsius, which can be measured and displayed by mixed primary air thermometer 460.
Claims (10)
1. A waste incineration exhaust-heat boiler system, characterized in that: comprises a primary air flue (100), a circulating flue (200), a waste heat boiler flue (300) and a combustion chamber (400);
An inlet of the circulating flue (200) is connected with a low-temperature circulating flue (232), and the low-temperature circulating flue (232) is connected with a waste heat boiler flue (300); the inlet of the circulating flue (200) is also connected with a high-temperature circulating flue (242), and the high-temperature circulating flue (242) is connected with a waste heat boiler flue (300);
an inlet of the primary air duct (100) is connected with a primary fan (140); the primary air duct (100) is also connected with an air preheater (150);
The inlet of the steam-water side of the air preheater (150) is also connected with an air preheater steam pipeline (160) for heating, and the outlet is connected with an air preheater drain pipeline (130); the air preheater steam pipeline (160) is connected with the steam drum (320) through a saturated steam eduction tube (333);
The outlet of the primary air flue (100) is connected with the outlet of the circulating flue (200) and is converged into a mixed primary air flue (450), and the mixed primary air flue (450) is connected with an air chamber (440) at the lower part of the combustion chamber (400);
The inlet of the waste heat boiler flue (300) is connected with the flue gas outlet of the combustion chamber (400); an evaporator (310), a superheater (330) and an economizer (340) are arranged in the waste heat boiler flue (300), and the economizer (340) is arranged at the last section of the flow of the flue gas in the waste heat boiler flue (300); the waste heat boiler flue (300) is provided with a flue outlet (350); the evaporator (310) is connected with the steam drum (320) through a steam-water circulating pipe (315); the inlet of the superheater (330) is connected with a superheated steam pipeline (336), and the superheated steam pipeline (336) is connected with the steam drum (320) through a saturated steam eduction pipe (333); the outlet of the economizer (340) is connected with the steam drum (320) through a water supply pipe (341).
2. The waste incineration exhaust heat boiler system according to claim 1, characterized in that: a primary air flowmeter (110) is arranged in the primary air duct (100), and a primary air thermometer (105) is arranged in the primary air duct (100) at the outlet of the air preheater (150); a superheated steam flowmeter (338) is arranged in an inlet pipeline of the superheater (330).
3. The waste incineration exhaust heat boiler system according to claim 1, characterized in that: the oxygen concentration range in the mixed primary air duct (450) is 15-18%, and the temperature range in the mixed primary air duct (450) is 130-210 ℃.
4. The waste incineration exhaust heat boiler system according to claim 1, characterized in that: and a second circulating flue (413) is further arranged, so that the second circulating flue (413) is arranged on the circulating flue (200) and is connected with the combustion chamber (400) through a circulating air port (417) arranged at the upper part of the fire grate (420), and a circulating flue baffle (415) is arranged on the second flue (413).
5. The waste incineration exhaust heat boiler system according to claim 1, characterized in that: a heating steam regulating valve (170) and a heating steam flowmeter (180) are arranged on the air preheater steam pipeline (160);
A mixed primary air thermometer (460) is arranged on the mixed primary air duct (450);
A smoke circulating fan (210) and a dust remover (220) are arranged on the circulating flue (200), and a circulating smoke thermometer (203) and a circulating flue baffle (206) are arranged on a communication pipeline between an outlet of the smoke fan (210) and the mixed primary air flue (450).
6. The waste incineration exhaust heat boiler system according to claim 1, characterized in that: the low-temperature circulating flue (232) is provided with a low-temperature circulating flue gas flowmeter (231) and a low-temperature circulating flue gas baffle (233), a connection port of the low-temperature circulating flue (232) and the waste heat boiler flue (300) is positioned at the rear side of the economizer (340), and a low-temperature flue gas thermometer (234) is arranged at the connection port;
The high-temperature circulating flue (242) is provided with a high-temperature circulating flue gas flowmeter (241) and a high-temperature circulating flue gas baffle (243), a connection port of the high-temperature circulating flue (242) and the waste heat boiler flue (300) is positioned at the front side of the economizer (340), and a high-temperature flue gas thermometer (244) is arranged.
7. The control method of a waste incineration exhaust heat boiler system according to any one of claims 1 to 6, wherein the primary air flow in the mixed primary air duct is controlled such that:
V1A＝COE1A×FSTM；
Wherein,
V 1A is the running primary air flow, nm 3/s;
f STM is the steam yield of the waste heat boiler, and the unit is kg/s;
COE 1A is the primary air steam coefficient, the unit is Nm 3/kg, and is the ratio of the primary air flow V 1A of the operation of the incinerator to the steam quantity F STM of the waste heat boiler, and the range of the steam coefficient is 0.70-1.15 Nm 3/kg.
8. The control method of a waste incineration exhaust heat boiler system according to claim 7, wherein the primary air oxygen volume concentration in the mixed primary air duct is controlled such that:
Wherein:
O mix is the volume concentration of the oxygen of the mixed primary air,%;
V 1A is the running primary air flow, nm 3/h;
V HG is the flow rate of high-temperature circulating flue gas, nm 3/s;
v LG is the low-temperature circulating smoke flow, nm 3/s;
O Rec is the volume concentration of oxygen in the circulating flue, and the range is 3% -10%.
9. The control method of a waste incineration exhaust heat boiler system according to claim 7, characterized in that: the primary air temperature t aim,1Amix in the mixed primary air duct is controlled so that:
taim,1Amix＝tadp,1Amix+tS,Cor+tyl；
Wherein,
T aim,1Amix is the temperature of the target mixed primary air, and the temperature is lower than the temperature;
t adp,1Amix is the acid dew point temperature of the mixed primary air, in degrees celsius, and can be calculated by the following formula:
tadp,1Amix＝18.0×Mar+134.83；
Wherein M ar is the mass percent of the water content of the base received by the garbage in the furnace;
t S,Cor the fuel sulfur content correction factor, in degrees Celsius, can be calculated from the following equation:
tS,Cor＝65.46×Sar-6.42；
Wherein S ar is the mass percent of the sulfur content of the received base of the garbage in the furnace;
t yl is the margin, and the value range is 2-15 ℃.
10. The control method of a waste incineration exhaust heat boiler system according to claim 7: the oxygen concentration range in the primary air mixing duct is 15-18%, and the temperature range in the primary air mixing duct is 130-210 ℃.
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