CN112082151B - Multi-pollutant collaborative removing and burning device and method for circulating fluidized bed boiler - Google Patents

Multi-pollutant collaborative removing and burning device and method for circulating fluidized bed boiler Download PDF

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CN112082151B
CN112082151B CN202010902637.5A CN202010902637A CN112082151B CN 112082151 B CN112082151 B CN 112082151B CN 202010902637 A CN202010902637 A CN 202010902637A CN 112082151 B CN112082151 B CN 112082151B
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chamber
pyrolysis
semicoke
communicated
reburning
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CN112082151A (en
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宋国良
包绍麟
杨召
吕清刚
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Institute of Engineering Thermophysics of CAS
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Institute of Engineering Thermophysics of CAS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/24—Devices for removal of material from the bed
    • F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • 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
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Abstract

The invention discloses a multi-pollutant collaborative removing combustion device of a circulating fluidized bed boiler, which comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the device also comprises a second coal feeder, a pyrolysis chamber, a semicoke activation chamber, a second cyclone separator and an active coke desulfurization and demercuration reaction tower; the invention also discloses a method for cooperatively removing and burning multiple pollutants in the circulating fluidized bed boiler, which realizes the SO of multiple gaseous pollutants through secondary desulfurization, secondary denitration and primary demercuration reaction 2 Low-cost and high-efficiency combined removal of NOx and heavy metal Hg. The invention has the advantages that: the process flow is simple; the multi-pollutant removal efficiency is high, and no secondary pollution is caused; no extra heat source is needed, energy conservation is realized, and the investment and operation cost is greatly reduced.

Description

Multi-pollutant collaborative removing and burning device and method for circulating fluidized bed boiler
Technical Field
The invention belongs to the technical field of clean and efficient combustion of coal, and particularly relates to a device and a method for removing and combusting multiple pollutants in a circulating fluidized bed boiler in a coordinated manner.
Background
China has rich coal resources, and NOx and SO discharged by coal-fired flue gas 2 And Hg bring great harm to human health and ecological environment. The electricity production is the largest main body of coal consumption, and the coal burning amount accounts for 51 percent of the coal consumption. Therefore, the NOx and SO of the coal-fired power plant 2 And the control of various pollutants such as Hg and the like, has become the most urgent task in the field of atmospheric pollution control in China.
The Circulating Fluidized Bed (CFB) combustion technology is a clean combustion technology with high efficiency and low pollution, and is widely popularized and applied at home and abroad. With the promulgation and implementation of the national emission Standard of atmospheric pollutants for thermal power plants (GB 13223-2011), NOx and SO are required 2 Respectively reach 100mg/m with Hg 3 、100mg/m 3 、0.03mg/m 3 Of (2)New emission standard for NOx and SO 2 Even strictly reaches 50mg/m 3 And 35mg/m 3 This makes circulating fluidized bed boilers even more challenging.
Existing control of NOx and SO 2 And Hg are the most mature methods for the three contaminants: the standard emission of NOx is realized by adopting a method of combining selective non-catalytic reduction (SNCR) and selective non-catalytic reduction (SCR); SO realization through first-stage wet desulphurization (WFGD) or second-stage wet desulphurization of tail flue 2 Discharging after reaching the standard; activated carbon was used to inject demercuration (ACI). At present, a one-by-one treatment method is used for multiple pollutants at home and abroad, namely different pollutants are removed by adding different purification devices to form series connection of removal processes, but the grading treatment mode has the defects of large floor area, large consumption of reducing agents and absorbing agents, extremely high capital investment and operating cost and the like.
Although the integrated processes of simultaneous desulfurization and denitrification, such as high-energy radiation chemical process, activated carbon process, flue gas circulating fluidized bed process, plasma process, etc., have been available, they have not been widely used due to their huge investment and operation costs, and other gaseous pollutants and solid particles still need to be realized by connecting other process devices in series. For example, chinese patent CN201610077738.7 discloses an ultra-low emission synergistic removal system for industrial coal-fired boiler flue gas pollutants, which realizes the combined action of an SCR denitration device, an electrostatic precipitator, a three-phase turbulence barrel high-efficiency desulfurization and dust removal tower and an efficiency-improving wet-type electrostatic precipitation and demisting device SO as to realize the NOx and SO in the industrial coal-fired boiler flue gas 2 And ultra-low emission of dust pollutants. The tail flue equipment of the system is complex, and the investment, operation and maintenance costs are high. Chinese patent CN201810113587.5 discloses a system and a method for combined desulfurization and denitration of powdery active coke, wherein NOx and SO in flue gas are removed through the powdery active coke and ammonia gas 2 And the investment and operation cost is high due to the need of providing additional active coke and ammonia gas raw materials.
In summary, the prior circulating fluidized bed boiler pollutant removal technology has the following defects:
(1) The method for removing multiple pollutants of the circulating fluidized bed mainly adopts a single-item cascade connection treatment mode, namely a denitration method combining SNCR and SCR, a combined desulfurization method of calcium spraying desulfurization in a furnace and tail one-stage wet desulfurization or multistage wet desulfurization, an active coke demercuration method and the like.
(2) The existing integrated technology for desulfurization, denitrification and demercuration of part of coal-fired flue gas, such as a high-energy radiation chemical method, an activated carbon method, a plasma method and the like, has the defects of huge investment and operation cost, large maintenance workload, small flue gas treatment amount, secondary pollution and other factors due to the need of providing additional absorbent, reducing agent and additional energy consumption, is not widely applied, and is still required to be connected with other process devices in series to realize other gaseous pollutants.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide a device and a method for removing and combusting multiple pollutants of a circulating fluidized bed boiler in a coordinated manner.
In order to achieve the above object, the present invention adopts the following technical solutions:
a multi-pollutant collaborative removal combustion device of a circulating fluidized bed boiler comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the boiler comprises a main combustion chamber, a first cyclone separator and a material returning device; the device is characterized by also comprising a second coal feeder, a pyrolysis chamber, a semicoke activation chamber, a second cyclone separator and an active coke desulfurization and demercuration reaction tower; the material returning device is arranged at the solid phase outlet of the first cyclone; the side wall of the upper part of the front wall of the pyrolysis chamber is communicated with the side wall of the feeding vertical pipe of the material returning device; allowing part of the high-temperature circulating ash to enter a pyrolysis chamber from the solid-phase outlet; the second coal feeder is arranged at the top of the pyrolysis chamber and is used for adding secondary fuel; the inlet of the second cyclone separator is connected with the upper outlet of the pyrolysis chamber; the semicoke activation chamber is communicated with the lower part of the rear wall of the pyrolysis chamber; the inlet of the active coke desulfurization and demercuration reaction tower is communicated with the bottom of the semicoke activation chamber, and the outlet of the bottom of the active coke desulfurization and demercuration reaction tower is communicated with the main combustion chamber through a semicoke reburning nozzle.
Preferably, the tail flue comprises a superheater and/or a reheater, an economizer and an air preheater which are arranged from top to bottom; the hot air outlet pipeline of the air preheater is respectively communicated with a primary air pipeline at the bottom of the boiler and a semicoke reburning nozzle of a hearth at the lower part of the main combustion chamber; the inlet of the front wall of the active coke desulfurization and demercuration reaction tower is communicated with the outlet flue of the tail flue dust remover, the outlet of the rear wall is communicated with the inlet flue, and the bottom of the active coke desulfurization and demercuration reaction tower is communicated with the semicoke reburning nozzle of the hearth.
Preferably, a feeding fluidization air chamber and a discharging fluidization air chamber are arranged at the bottom of the pyrolysis chamber, a partition plate is arranged on the inner side of the middle position of the top of the pyrolysis chamber, the pyrolysis chamber is divided into a feeding chamber and a discharging chamber through the partition plate, the feeding chamber is communicated with the discharging chamber through a channel at the lower part of the partition plate, and an activation chamber is arranged at an outlet of the pyrolysis chamber.
Preferably, a gas phase outlet at the top of the second cyclone separator is respectively communicated with the pyrolysis gas nozzle, the feeding fluidization air chamber and the returning fluidization air chamber, and a solid phase outlet at the bottom of the second cyclone separator is communicated with a feeding hole at the top of the semicoke activation chamber; the side wall of the semicoke activation chamber is communicated with a superheater arranged on the tail flue.
Preferably, the main combustion chamber is provided with a primary oxidation desulfurization zone and a semicoke reburning primary denitration zone from bottom to top; the connection part of the first cyclone separator and the tail flue is sequentially provided with a pyrolysis gas reburning secondary denitration area and a burnout area; and a gas phase outlet of the second cyclone separator is communicated with the pyrolysis gas reburning secondary denitration area through a pyrolysis gas nozzle.
Preferably, the semicoke reburning primary denitration area is provided with at least one semicoke reburning nozzle; the pyrolysis gas reburning secondary denitration area is provided with at least one pyrolysis gas nozzle; the burnout zone is provided with at least one burnout air nozzle; and the side wall of the bottom of the primary oxidation desulfurization area is provided with a limestone nozzle.
Preferably, the pyrolysis gas nozzles can be arranged at the middle lower part of the main combustion chamber and positioned at the lower part of the semicoke reburning nozzles; the over-fire air nozzles are arranged on the vertical or horizontal flue of the outlet of the first cyclone separator.
Preferably, the main combustion chamber is provided with a primary oxidation desulfurization zone and a pyrolysis gas reburning primary denitration zone from bottom to top; a semicoke reburning secondary denitration area and a burnout area are sequentially arranged at the joint of the first cyclone separator and the tail flue; and an outlet of the heating surface of the tail flue is provided with an active coke secondary desulfurization and demercuration area.
Preferably, the pyrolysis gas reburning primary denitration area is provided with at least one pyrolysis gas spout; the semicoke reburning secondary denitration area is provided with at least one semicoke reburning nozzle; the burnout zone is provided with at least one burnout air nozzle.
A combustion method for removing multiple pollutants in a circulating fluidized bed boiler in a coordinated manner is characterized by comprising the following steps:
step one, adding primary fuel, primary air and a desulfurizer into a primary oxidation area at the bottom of a main combustion chamber for combustion, adding limestone into the bottom of the main combustion chamber through a material returning device, and adding SO generated in the combustion process at the bottom of the main combustion chamber 2 Performing primary desulfurization reaction, wherein combustion products of the main combustion chamber pass through a first cyclone separator, and part of high-temperature circulating ash discharged from a lower solid-phase outlet enters a pyrolysis chamber;
adding the secondary fuel into a pyrolysis chamber, carrying out low-temperature pyrolysis to generate a pyrolysis product, carrying out gas-solid separation on the pyrolysis product through a second cyclone separator, feeding the separated fine coke powder solid-phase product and the coarse coke powder discharged from the bottom of the pyrolysis chamber into a semicoke activation chamber, carrying out activation reaction on the fine coke powder solid-phase product and the coarse coke powder in the semicoke activation chamber through superheated steam from a superheater to generate active coke, and feeding the active coke into an active coke desulfurization and demercuration reaction tower to carry out demercuration and secondary desulfurization;
step three, the active coke is inactivated in the step two, and then is conveyed by primary hot air to enter the semicoke reburning primary denitration zone at the middle lower part of the main combustion chamber and NOx generated in the primary oxidation zone at the bottom of the main combustion chamber is subjected to primary denitration reduction, so that most of the NOx is reduced into nitrogen;
step four, part of the gas-phase reduction product separated by the second cyclone separator in the step two enters an outlet of the main combustion chamber to carry out second-stage denitration reduction on NOx in the flue gas, and all the NOx which is not reduced in the step three is reduced into nitrogen; the other part enters the bottom of the pyrolysis chamber to provide fluidized wind;
and step five, fully burning out the unburned carbon residue particles and the CO gas under the action of reburning air in the second-stage denitration reduction in the step four.
Preferably, the excess air coefficient of the primary oxidation desulfurization zone is 1.10-1.15; the reaction temperature of the primary oxidation desulfurization zone is 850-900 ℃; the excess air coefficient of the semicoke reburning primary denitration area is 0.9-1.0, and the reaction temperature is 950-1000 ℃; the excess air coefficient of the secondary denitration zone of the reburning of the pyrolysis gas is 1.0-1.08, and the reaction temperature is 1000-1100 ℃; the excess air coefficient of the burnout zone is 1.1-1.15, and the reaction temperature is 900-950 ℃; the reaction temperature of the pyrolysis chamber is 550-650 ℃; the reaction temperature of the active coke secondary desulfurization and demercuration area is 120-160 ℃; the outlet reburning amount of the first cyclone separator accounts for 8-15% of the total input heat.
Preferably, the primary fuel and the secondary fuel are one or more of bituminous coal, lignite, anthracite, biomass or carbon-based fuel.
The invention has the advantages that:
(1) The invention realizes that a large amount of cheap reducing agents and adsorbents generated in the coal thermochemical conversion process are subjected to secondary desulfurization, secondary denitration and primary demercuration reaction in one reaction device to obtain a plurality of gaseous pollutants SO 2 The NOx and the heavy metal Hg are removed in a low-cost and high-efficiency combined mode, the process flow is simple, and the investment and the operating cost can be greatly reduced.
(2) The pyrolysis product is introduced into a secondary denitration zone of pyrolysis gas, and is used as a strong reduction reactant of NOx in combustion flue gas; the second process provides heat source for reduction reaction through reaction heat release, and ensures the temperature of the reduction reaction; the pyrolysis phenolic wastewater and tar in the third pyrolysis gas are subjected to complete decomposition reaction in a high-temperature area, and the problem of secondary pollution discharge is avoided. The problem of the complicated tar dust separation of afterbody after the low temperature pyrolysis and tar precipitate the jam pipeline is solved, the discharge problem of phenol-containing waste water has also been solved simultaneously, realizes zero wastewater discharge, fully guarantees the steady operation of system. In addition, dust produced in the pyrolysis process and inactivated semicoke discharged from the desulfurization and demercuration reaction tower are fed into the main combustion chamber for efficient combustion, so that the utilization of solid waste resources is realized, the energy utilization efficiency of the system is greatly improved, and near zero emission of the system is realized. Meanwhile, the pyrolysis gas reducing agent provided by the pyrolysis chamber can solve the problems of starting debugging of the main combustion chamber and high NOx emission under low load, and can realize full-load full-flow ultralow emission.
(3) The primary fuel and the secondary fuel can be the same fuel or different fuels, so that the fuel applicability and the adjustment flexibility of the system are improved.
(4) According to the invention, the high-temperature circulating ash heat carrier is used as a heat source for the low-temperature pyrolysis reaction of coal, and no additional heat source is needed, so that energy conservation is realized; cheap pyrolysis gas and semicoke with strong reducibility generated in the low-temperature pyrolysis process are respectively used as reducing agents of a primary denitration area and a secondary denitration area of a main combustion chamber to carry out secondary efficient denitration reduction on NOx in flue gas, and compared with a conventional combustion method, the reduction area and the reduction reaction time are both greatly improved, the reaction temperature is improved, the oxygen concentration is reduced, the denitration strength and the denitration efficiency are greatly improved through the technical measures, and the denitration efficiency of a system after secondary denitration can reach more than 90%; the semicoke generated in the pyrolysis process is activated by superheated steam generated by a combustion system, the activated semicoke is used as a desulfurization and demercuration adsorbent, the desulfurization efficiency of the system after secondary desulfurization can reach more than 99 percent, and the demercuration efficiency can reach more than 90 percent; multi-pollutant SO 2 And the reducing agent and the adsorbent required by NOx and Hg removal are all generated by the system, so that additional supply is not required, and the investment and operation cost is greatly reduced.
Drawings
FIG. 1 is a schematic structural diagram of a multi-pollutant co-removal combustion apparatus 1 according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a multi-pollutant co-removal combustion apparatus for a circulating fluidized bed boiler according to an embodiment 2 of the present invention.
The meanings indicated in the figures are: 1-a main combustion chamber; 2-a first cyclone separator; 3-a material returning device; 4-a first coal feeder; 5-a second coal feeder; 6-a pyrolysis chamber; 7-a semicoke activation chamber; 8-a second cyclone separator; 9-a superheater; 10-an economizer; 11-an air preheater; 12-active coke desulfurization and demercuration reaction tower; a-a primary oxidation desulfurization zone; b, reburning the semicoke in a first-stage denitration area; b' -reburning the pyrolysis gas into a first-stage denitration zone; c, reburning the pyrolysis gas to a secondary denitration area; a C' -semicoke reburning secondary denitration area; d-a burnout zone; e-active coke secondary desulfurization and demercuration area; PA-primary hot air; TA-overfire air; PG-pyrolysis gas; EG-flue gas; SW-superheated steam; ASC-activated coke; DSC-reburn semicoke; CC-limestone.
Detailed Description
The present invention will be further described in detail with reference to the drawings and specific examples.
Example 1
As shown in fig. 1, a combustion apparatus for removing multiple pollutants in a circulating fluidized bed boiler comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the device also comprises a second coal feeder, a pyrolysis chamber, a semicoke activation chamber, a second cyclone separator and an active coke desulfurization and demercuration reaction tower;
the boiler includes: the device comprises a main combustion chamber 1, a first cyclone separator 2 and a material returning device 3; the main combustion chamber 1 is provided with a primary oxidation desulfurization area A and a semicoke reburning primary denitration area B from bottom to top, the rear wall of the primary oxidation desulfurization area A is communicated with the feed opening of the material returning device 3, the front wall is communicated with the discharge opening of the first coal feeder 4, the bottom of the primary oxidation desulfurization area A is communicated with the small hole of the blast cap on the blast distribution plate, and the air inlet at the bottom of the blast cap of the blast distribution plate is communicated with the air chamber; the front wall of the lower part of the semicoke reburning primary denitration area B is communicated with a semicoke reburning nozzle DSC, and the upper part of the semicoke reburning primary denitration area B is communicated with an inlet of the first cyclone separator 2; the gas-phase outlet at the upper part of the first cyclone separator 2 is communicated with the inlet at the lower part of the pyrolysis gas reburning secondary denitration area C; the pyrolysis gas reburning secondary denitration area C is provided with a pyrolysis gas spout; an outlet at the upper part of the secondary denitration zone C for reburning the pyrolysis gas is communicated with an inlet of the burnout zone D, and a TA nozzle of burnout air is arranged at the top of the burnout zone D; wherein the overfire air TA nozzle is arranged on a vertical or horizontal flue at the outlet of the first cyclone separator 2; a feed inlet at the upper part of the material returning device 3 is communicated with a solid phase outlet at the lower part of the first cyclone separator 2, and the upper part of a discharge outlet at the lower part of the material returning device 3 is communicated with a limestone CC nozzle; the limestone CC spout is arranged on the side wall of the first-stage oxidation desulfurization area A at the bottom of the main combustion chamber.
Wherein, the pyrolysis gas PG nozzle can also be arranged at the middle lower part of the main combustion chamber and is positioned at the lower part of the semicoke reburning DSC nozzle.
The tail flue comprises a superheater 9 and/or a reheater, an economizer 10 and an air preheater 11 which are arranged from top to bottom, and a hot air outlet pipeline of the air preheater 11 is respectively communicated with a primary air pipeline at the bottom of the boiler and a semicoke reburning DSC nozzle of a hearth at the lower part of the main combustion chamber 1; the inlet of the front wall of the active coke desulfurization and demercuration reaction tower 12 is communicated with the outlet flue of the tail flue dust remover, the outlet of the rear wall is communicated with the inlet flue, and the bottom of the active coke desulfurization and demercuration reaction tower is communicated with the semicoke reburning DSC nozzle of the hearth.
6 tops of pyrolysis chamber are linked together with 5 discharge gates of second feeder, 6 front wall upper portion lateral walls of pyrolysis chamber are linked together with the lateral wall of 3 feeding risers of returning charge ware, 6 back wall upper portion lateral walls of pyrolysis chamber are linked together with the import of second cyclone 8, 6 back wall lower part lateral walls of pyrolysis chamber are linked together with the lateral wall feed inlet of semicoke activation room 7, 6 bottoms of pyrolysis chamber are equipped with feeding fluidization plenum and returning charge fluidization plenum, 6 top intermediate position inboards of pyrolysis chamber are equipped with a baffle, divide into feed chamber and discharge chamber with the pyrolysis chamber through the baffle, the feed chamber is linked together through the passageway of baffle lower part with the discharge chamber.
Wherein, the top gas phase outlet of the second cyclone separator 8 is respectively communicated with a pyrolysis gas PG nozzle on the side wall of the secondary denitration zone C for reburning pyrolysis gas, a feeding fluidization wind chamber of the pyrolysis chamber 6 and a return fluidization wind chamber air inlet pipe through pipelines, and the bottom solid phase outlet of the second cyclone separator 8 is communicated with a feed inlet on the top of the semicoke activation chamber 7 through a valve; the bottom of the semicoke activation chamber 7 is communicated with a feed inlet at the top of the active coke desulfurization and demercuration reaction tower 12 through a pipeline, and the side wall of the semicoke activation chamber 7 is communicated with an outlet of a superheater through a pipeline.
Based on the combustion device for the collaborative removal of the multiple pollutants of the circulating fluidized bed boiler, the embodiment also relates to a combustion method for the collaborative removal of the multiple pollutants of the circulating fluidized bed boiler, which comprises the following steps:
step one, adding primary fuel and primary air into a primary oxidation desulfurization area A at the bottom of a main combustion chamber 1 for combustion, adding limestone CC into the bottom of the main combustion chamber 1 through a return pipe of a material returning device 3, and mixing with SO generated in the combustion process at the bottom of the main combustion chamber 1 2 Performing primary desulfurization reaction, wherein combustion products of the main combustion chamber 1 pass through the first cyclone separator 2, and part of high-temperature circulating ash discharged from a solid phase outlet at the lower part enters the pyrolysis chamber 6; the reaction mechanism is as follows:
CaCO 3 →CaO+CO 2 (1)
CaO+SO 2 →CaSO 3 (2)
2CaSO 3 +O 2 →2CaSO 4 (3)
the primary fuel is fed from the lower part of the main combustion chamber 1, and the secondary fuel is fed from the top of the pyrolysis chamber 6; the air for fuel combustion is divided into primary air PA, over-fire air TA and return air, wherein the primary air PA is fed from the bottom of the main combustion chamber 1, the over-fire air TA is fed from an outlet over-fire area D of the first cyclone separator 2, and the return air is fed from the bottom of the return feeder 3.
Step two, adding secondary fuel into a pyrolysis chamber 6, pyrolyzing at low temperature to generate pyrolysis products (pyrolysis semicoke, tar and pyrolysis gas), carrying out gas-solid separation on the pyrolysis products through a second cyclone separator 8, feeding the fine coke powder solid-phase product obtained after separation and coarse coke powder discharged from the bottom of the pyrolysis chamber 6 into a semicoke activation chamber 7, carrying out activation reaction through superheated steam SW from a superheater 9 in the semicoke activation chamber 7 to generate active coke ASC, feeding the active coke ASC into an active coke desulfurization and demercuration reaction tower 12 to carry out demercuration and secondary desulfurization, and realizing SO 2 Combined removal with Hg; the reaction mechanism is as follows:
SO 2(gas) +AC→SO 2(ad) (4)
O 2(gas) +AC→O (ad) (5)
H 2 O (gas) +AC→H 2 O (ad) (6)
SO 2(ad) +O (ad) →SO 3(ad) (7)
SO 3(ad) +H 2 O (ad) →H 2 SO 4(ad) (8)
H 2 SO 4(ad) +nH 2 O (ad) →H 2 SO 4 .nH 2 O (ad) (9)
in the formula, (gas) is gas phase, (ad) is adsorption state, and AC is active site of active coke surface.
Preheating the inactivated semicoke from the bottom of the desulfurization and demercuration reaction tower 12 in the second step by hot air from a tail flue air preheater 11, preheating the inactivated semicoke to improve the combustion stability and burnout rate of the inactivated semicoke, conveying the inactivated semicoke into the semicoke reburning primary denitration zone B at the middle lower part of the main combustion chamber 1 through primary hot air, and performing primary denitration reduction on NOx generated by the primary oxidation and desulfurization zone A at the bottom of the main combustion chamber 1 to reduce most of the NOx into nitrogen; the reaction mechanism is as follows:
NO+C()→C(O)+C(N) (10)
C(N)+NO→N 2 +C(O) (11)
wherein C (), C (N) and C (O) represent carbon active sites, a surface carbon-nitrogen component and a surface carbon-oxygen component, respectively.
Step four, in the step two, a part of the gas phase reduction products (pyrolysis gas PG, tar and fine coke powder) separated by the second cyclone separator 8 enters the bottom of the pyrolysis chamber 6 to provide fluidized air for the pyrolysis chamber; the other part of the smoke enters an outlet of the main combustion chamber 1 to carry out secondary denitration reduction on the NOx in the smoke, and the NOx which is not reduced in the third step is reduced into nitrogen; the main reaction mechanism is as follows:
H 2 +NO→HNO+H (12)
HNO+NO→N 2 O+OH (13)
N 2 O+H→N 2 +OH (14)
2CO+2NO→CO 2 +N 2 (15)
CH 4 +3O→CH+3OH (16)
CH+NO→HCN (17)
HCN+OH→NH 2 (18)
NH 2 +NO→N 2 (19)
and step five, fully burning out the unburned carbon residue particles and the CO gas under the action of reburning air in the second-stage denitration reduction in the step four.
Wherein, the excess air coefficient of the first-stage oxidation desulfurization area A of the main combustion chamber 1 is 1.10 to 1.15, and the reaction temperature is 850 to 900 ℃; the excess air coefficient of the semicoke reburning primary denitration area B is 0.9-1.0, and the reaction temperature is 950-1000 ℃; the excess air coefficient of the secondary denitration area C for reburning the pyrolysis gas is 1.0-1.08, and the reaction temperature is 1000-1100 ℃; the excess air coefficient of the burnout zone D is 1.1-1.15, and the reaction temperature is 900-950 ℃; the reaction temperature of the pyrolysis chamber is 550-650 ℃; the reaction temperature of the active coke secondary desulfurization and demercuration zone E is 120-160 ℃; the outlet reburning amount (heat ratio) of the first cyclone separator 2 accounts for 8-15% of the total input heat.
The primary fuel and the secondary fuel can be the same fuel or different fuels, and the fuel can be bituminous coal, lignite, anthracite, biomass or other carbon-based fuels.
Example 2
As shown in fig. 2, a combustion apparatus for removing multiple pollutants in a circulating fluidized bed boiler comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the device also comprises a second coal feeder, a pyrolysis chamber, a semicoke activation chamber, a second cyclone separator and an active coke desulfurization and demercuration reaction tower;
the boiler includes: the device comprises a main combustion chamber 1, a first cyclone separator 2 and a material returning device 3; the main combustion chamber 1 is provided with a primary oxidation desulfurization zone A, a pyrolysis gas reburning primary denitration zone B 'and a semicoke reburning secondary denitration zone C' from bottom to top, the rear wall of the primary oxidation desulfurization zone A is communicated with a material returning port of a material returning device 3, the front wall is communicated with a discharge port of a first coal feeder 4, and the bottom of the primary oxidation desulfurization zone A is provided with an air distribution plate and an air chamber; the front wall of the B 'of the pyrolysis gas reburning primary denitration zone is provided with a pyrolysis gas PG spout, the front wall of the C' of the semicoke reburning secondary denitration zone is provided with a reburning semicoke DSC spout, the PG spout of the pyrolysis gas and the reburning semicoke DSC spout are both arranged on the front wall of the main burning chamber, the reburning semicoke DSC spout is arranged right above the pyrolysis gas spout, and the upper part of the secondary denitration zone is communicated with the inlet of the first cyclone separator 2; an inlet of the first cyclone separator 2 is communicated with an outlet at the upper part of the secondary denitration area, a gas phase outlet at the upper part of the first cyclone separator is communicated with an inlet of the burnout area D, a burnout air nozzle is arranged on the side wall of the burnout area D, and a solid phase outlet at the lower part of the first cyclone separator is communicated with an inlet of a vertical pipe of a material returning device; the upper part of a discharge port at the lower part of the material returning device is communicated with a CC nozzle of limestone;
6 tops of pyrolysis chamber are linked together with 5 discharge gates of second feeder, 6 front wall upper portion lateral walls of pyrolysis chamber are linked together with the lateral wall of 3 feeding risers of returning charge ware, 6 rear wall upper portion lateral walls of pyrolysis chamber are linked together with the import of second cyclone 8, 6 rear wall lower part lateral walls of pyrolysis chamber are linked together with the lateral wall feed inlet of semicoke activation room 7, 6 bottoms of pyrolysis chamber are equipped with feeding fluidization plenum and returning charge fluidization plenum, 6 top intermediate position inboards of pyrolysis chamber are equipped with a baffle, divide into feed chamber and discharge chamber with the pyrolysis chamber through the baffle, the feed chamber is linked together through the passageway of baffle lower part with the discharge chamber. And a gas phase outlet at the top of the second cyclone separator 8 is respectively communicated with a pyrolysis gas PG nozzle on the front wall of the pyrolysis gas reburning primary denitration area, a pyrolysis chamber feeding fluidization air chamber and a return fluidization air chamber air inlet pipe through pipelines, and a solid phase outlet at the bottom of the second cyclone separator is communicated with a feeding hole at the top of the semicoke activation chamber through a valve.
The bottom of the semi-coke activation chamber 7 is communicated with a feed inlet at the top of the active coke desulfurization and demercuration reaction tower through a pipeline, and the side wall of the semi-coke activation chamber is communicated with an outlet of the superheater through a pipeline. The tail flue heating surface comprises a superheater 9 and/or a reheater, an economizer 10, an air preheater 11 and a hot air outlet pipeline of the air preheater 11 which are arranged from top to bottom, wherein the hot air outlet pipeline of the air preheater 11 is respectively communicated with a primary air pipeline at the bottom of a hearth and a semicoke reburning DSC nozzle on the front wall of a main combustion chamber.
An inlet of a front wall of the active coke desulfurization and demercuration reaction tower 12 is communicated with an outlet flue of a tail flue dust collector, an outlet of a rear wall of the active coke desulfurization and demercuration reaction tower 12 is communicated with an inlet flue of a chimney, and the bottom of the active coke desulfurization and demercuration reaction tower 12 is communicated with a semicoke reburning DSC nozzle of a hearth.
It should be noted that the above-mentioned embodiments do not limit the present invention in any way, and all technical solutions obtained by using equivalent alternatives or equivalent variations fall within the protection scope of the present invention.

Claims (9)

1. A multi-pollutant collaborative removal combustion device of a circulating fluidized bed boiler comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the boiler comprises a main combustion chamber (1), a first cyclone separator (2) and a material returning device (3); the device is characterized by also comprising a second coal feeder (5), a pyrolysis chamber (6), a semicoke activation chamber (7), a second cyclone separator (8) and an active coke desulfurization and demercuration reaction tower (12); the material returning device (3) is arranged at the solid phase outlet of the first cyclone separator (2); the side wall of the upper part of the front wall of the pyrolysis chamber (6) is communicated with the side wall of the feeding vertical pipe of the material returning device (3), so that part of high-temperature circulating ash enters the pyrolysis chamber (6) from the solid-phase outlet; the second coal feeder (5) is arranged at the top of the pyrolysis chamber (6) and is used for adding secondary fuel; the inlet of the second cyclone separator (8) is connected with the upper outlet of the pyrolysis chamber (6); a gas phase outlet at the top of the second cyclone separator (8) is communicated with a pyrolysis gas nozzle; the semicoke activation chamber (7) is communicated with the lower part of the rear wall of the pyrolysis chamber (6); a solid phase outlet at the bottom of the second cyclone separator (8) is communicated with a feed inlet at the top of the semicoke activation chamber (7) through a valve; an inlet of the active coke desulfurization and demercuration reaction tower (12) is communicated with the bottom of the semicoke activation chamber (7), and an outlet at the bottom of the active coke desulfurization and demercuration reaction tower (12) is communicated with the main combustion chamber (1) through a semicoke reburning nozzle; the main combustion chamber (1) is provided with a primary oxidation desulfurization zone and a semicoke reburning primary denitration zone from bottom to top; the connection part of the first cyclone separator (2) and the tail flue is sequentially provided with a pyrolysis gas reburning secondary denitration area and a burnout area; the gas-phase outlet of the second cyclone separator (8) is communicated with the second-stage denitration region of the reburning pyrolysis gas through a pyrolysis gas nozzle; the semicoke reburning primary denitration area is provided with at least one semicoke reburning nozzle; the pyrolysis gas reburning secondary denitration area is provided with at least one pyrolysis gas nozzle; the burnout zone is provided with at least one burnout air nozzle; and the side wall of the bottom of the primary oxidation desulfurization area is provided with a limestone nozzle.
2. The combustion plant according to claim 1, characterized in that the back pass comprises from top to bottom a superheater (9) and/or a reheater, an economizer (10), an air preheater (11); the hot air outlet pipeline of the air preheater (11) is respectively communicated with a primary air pipeline at the bottom of the boiler and a semicoke reburning nozzle of a hearth at the lower part of the main combustion chamber (1); the inlet of the front wall of the active coke desulfurization and demercuration reaction tower (12) is communicated with the outlet flue of the tail flue dust remover, the outlet of the rear wall is communicated with the inlet flue, and the bottom of the active coke desulfurization and demercuration reaction tower is communicated with the semicoke reburning nozzle of the hearth.
3. The combustion device as claimed in claim 1, wherein the bottom of the pyrolysis chamber (6) is provided with a feeding fluidization air chamber and a returning fluidization air chamber, the inner side of the middle position of the top of the pyrolysis chamber (6) is provided with a partition plate, the pyrolysis chamber (6) is divided into a feeding chamber and a discharging chamber through the partition plate, the feeding chamber is communicated with the discharging chamber through a channel at the lower part of the partition plate, and the outlet of the pyrolysis chamber (6) is provided with an activation chamber.
4. The combustion device as claimed in claim 3, wherein the top gas phase outlet of the second cyclone separator (8) is respectively communicated with the pyrolysis gas nozzle, the feeding fluidization air chamber and the returning fluidization air chamber, and the side wall of the semicoke activation chamber (7) is communicated with a superheater outlet pipeline arranged on the tail flue.
5. The combustion apparatus as claimed in claim 1, wherein the pyrolysis gas nozzles are further arranged at the lower middle part of the main combustion chamber and at the lower part of the semicoke reburning nozzles; the over-fire air nozzles are arranged on a vertical or horizontal flue at the outlet of the first cyclone separator (2).
6. A multi-pollutant collaborative removal combustion device of a circulating fluidized bed boiler comprises: a boiler and a tail flue; the boiler is communicated with the tail flue; the boiler comprises a main combustion chamber (1), a first cyclone separator (2) and a material returning device (3); the device is characterized by also comprising a second coal feeder (5), a pyrolysis chamber (6), a semicoke activation chamber (7), a second cyclone separator (8) and an active coke desulfurization and demercuration reaction tower (12); the material returning device (3) is arranged at the solid phase outlet of the first cyclone separator (2); the side wall of the upper part of the front wall of the pyrolysis chamber (6) is communicated with the side wall of the feeding vertical pipe of the material returning device (3), so that part of high-temperature circulating ash enters the pyrolysis chamber (6) from the solid phase outlet; the second coal feeder (5) is arranged at the top of the pyrolysis chamber (6) and is used for adding secondary fuel; the inlet of the second cyclone separator (8) is connected with the upper outlet of the pyrolysis chamber (6); a gas phase outlet at the top of the second cyclone separator (8) is communicated with a pyrolysis gas nozzle; the semicoke activation chamber (7) is communicated with the lower part of the rear wall of the pyrolysis chamber (6); a solid phase outlet at the bottom of the second cyclone separator (8) is communicated with a feed inlet at the top of the semicoke activation chamber (7) through a valve; an inlet of the active coke desulfurization and demercuration reaction tower (12) is communicated with the bottom of the semicoke activation chamber (7), and an outlet at the bottom of the active coke desulfurization and demercuration reaction tower (12) is communicated with the main combustion chamber (1) through a semicoke reburning nozzle; the method is characterized in that a primary oxidation desulfurization zone and a pyrolysis gas reburning primary denitration zone are arranged in the main combustion chamber from bottom to top; a semicoke reburning secondary denitration area and a burnout area are sequentially arranged at the joint of the first cyclone separator (2) and the tail flue; an active coke secondary desulfurization and demercuration area is arranged at the outlet of the heating surface of the tail flue; the pyrolysis gas reburning primary denitration area is provided with at least one pyrolysis gas spout; the semicoke reburning secondary denitration area is provided with at least one semicoke reburning nozzle; the burnout zone is provided with at least one burnout air nozzle.
7. A combustion method for removing multiple pollutants in a circulating fluidized bed boiler in a coordinated manner is characterized by comprising the following steps:
step one, adding primary fuel, primary air and a desulfurizer into a primary oxidation area at the bottom of a main combustion chamber (1) for combustion, and adding limestone into the primary oxidation area through a material returning deviceEnters the bottom of the main combustion chamber (1) and is in combustion with SO generated in the bottom of the main combustion chamber (1) 2 Performing primary desulfurization reaction, wherein combustion products in the main combustion chamber (1) pass through the first cyclone separator (2), and part of high-temperature circulating ash discharged from a lower solid-phase outlet enters the pyrolysis chamber (6);
step two, adding secondary fuel into a pyrolysis chamber (6), pyrolyzing at low temperature to generate a pyrolysis product, carrying out gas-solid separation on the pyrolysis product through a second cyclone separator (8), feeding a fine coke powder solid-phase product obtained after separation and coarse coke powder discharged from the bottom of the pyrolysis chamber (6) into a semicoke activation chamber (7), carrying out activation reaction on the semicoke activation chamber (7) through superheated steam from a superheater to generate active coke, and feeding the active coke into an active coke desulfurization and demercuration reaction tower (12) to carry out demercuration and secondary desulfurization;
step three, after the activated coke is inactivated in the step two, the activated coke is conveyed into a semicoke reburning primary denitration area at the middle lower part of the main combustion chamber (1) through primary hot air, NOx generated by a primary oxidation area at the bottom of the main combustion chamber is subjected to primary denitration reduction, and most of the NOx is reduced into nitrogen;
step four, in the step two, part of the gas-phase reduction product separated by the second cyclone separator (8) enters an outlet of the main combustion chamber (1) to carry out second-stage denitration reduction on NOx in the flue gas, and all the NOx which is not reduced in the step three is reduced into nitrogen; the other part enters the bottom of the pyrolysis chamber (6) to provide fluidized wind;
and step five, fully burning out the unburned carbon residue particles and the CO gas under the action of reburning air in the second-stage denitration reduction in the step four.
8. The combustion method as claimed in claim 7, wherein the excess air ratio of the primary oxidative desulfurization zone is 1.10 to 1.15; the reaction temperature of the primary oxidation desulfurization zone is 850-900 ℃; the excess air coefficient of the semicoke reburning primary denitration area is 0.9 to 1.0, and the reaction temperature is 950 to 1000 ℃; the excess air coefficient of the pyrolysis gas reburning secondary denitration area is 1.0 to 1.08, and the reaction temperature is 1000 to 1100 ℃; the excess air coefficient of the burnout zone is 1.1 to 1.15, and the reaction temperature is 900 to 950 ℃; the reaction temperature of the pyrolysis chamber (6) is 550 to 650 ℃; the reaction temperature of the secondary desulfurization and demercuration area of the active coke is 120 to 160 ℃; the outlet reburning quantity of the first cyclone separator (2) accounts for 8 to 15 percent of the total input heat.
9. The combustion method according to claim 7 or 8, wherein the primary fuel and the secondary fuel are one or more of bituminous coal, lignite, anthracite, biomass or carbon-based fuel.
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