CN212915058U - Low temperature removes integration of bed and adsorbs SOx/NOx control system - Google Patents

Low temperature removes integration of bed and adsorbs SOx/NOx control system Download PDF

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CN212915058U
CN212915058U CN202020832863.6U CN202020832863U CN212915058U CN 212915058 U CN212915058 U CN 212915058U CN 202020832863 U CN202020832863 U CN 202020832863U CN 212915058 U CN212915058 U CN 212915058U
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flue gas
low
communicated
inlet
moving bed
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汪世清
郜时旺
王绍民
蒋敏华
肖平
黄斌
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Huaneng Clean Energy Research Institute
China Huaneng Group Co Ltd
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Huaneng Clean Energy Research Institute
China Huaneng Group Co Ltd
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    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
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    • B01D2253/102—Carbon
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
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    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01D53/34—Chemical or biological purification of waste gases
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    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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    • B01D53/83—Solid phase processes with moving reactants
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    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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Abstract

The utility model discloses a low temperature removes bed integration and adsorbs SOx/NOx control system contains SO2The NOx flue gas input pipeline is communicated with an inlet of a flue gas waste heat recoverer through a flue gas induced draft fan, an outlet of the flue gas waste heat recoverer is communicated with an inlet of a flue gas cooling system, an outlet of the flue gas cooling system is communicated with a flue gas inlet of a low-temperature moving bed adsorption tower, a porous adsorbent outlet at the bottom of the low-temperature moving bed adsorption tower is communicated with an inlet of a desorption tower, a porous adsorbent outlet of the desorption tower is communicated with a porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower, and the low-temperature moving bedThe gas outlet of the cold energy recoverer is communicated with the inlet of the cold energy recoverer; the flue gas cooling system adopts the syllogic cooling structure that sprays, and the device can satisfy the requirement of ultra-clean emission, and desorption temperature is lower, and the adsorbent loss is less simultaneously.

Description

Low temperature removes integration of bed and adsorbs SOx/NOx control system
Technical Field
The utility model belongs to the technical field of flue gas integration SOx/NOx control, a low temperature removes bed integration and adsorbs SOx/NOx control system is related to.
Background
The current mainstream desulfurization and denitrification technologies are SCR denitration and FGD desulfurization. SCR denitration is the reduction of NOx to N by a catalyst and a reducing agent2Discharging, desulfurizing by limestone-gypsum method by adding SO2And reacting with limestone slurry to generate insoluble calcium sulfate (gypsum) for removal. Although the traditional SCR denitration and FGD desulfurization technologies are widely applied, a plurality of problems exist. For example, FGD desulfurization uses a large amount of limestone as a desulfurizing agent, the large amount of mining of limestone causes serious mountain destruction, and the large amount of desulfurization wastewater generated by FGD desulfurization also brings treatment problems to power plants. The SCR denitration catalyst only has higher activity in a specific temperature interval, and when the operation load of a power plant is adjusted, the change of the flue gas temperature can seriously affect the SCR denitration efficiency. In addition, SCR denitration has secondary pollution problems such as ammonia escape, solid waste of catalyst and the like.
In addition to SCR denitration and FGD desulfurization techniques, activated coke adsorption integrated desulfurization and denitration techniques are also industrially used in japan and germany. The technique is characterized in that SO is adsorbed by utilizing the porous adsorption characteristic of active coke2Adsorbing and removing, and regenerating to obtain high-concentration SO2To prepare sulfuric acid, sulfur or sulfate and other by-products. The activated coke method cannot adsorb NOx because NO is a difficult-to-adsorb gas. NOx removal still requires ammonia injection reduction to N2Activated coke as a selective reduction catalystAn oxidizing agent. The denitration rate of the activated coke is not high, and generally only has the denitration efficiency of 70-80%, so that the requirement of ultra-clean emission cannot be met. In addition, the active coke dry method desulfurization principle is based on H2SO4Chemical adsorption, high regeneration temperature, active coke participating in regeneration reaction and large loss.
The conventional activated coke (charcoal) dry desulfurization and denitrification process is shown in the attached figure 1.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome above-mentioned prior art's shortcoming, provide a low temperature removes bed integration and adsorbs SOx/NOx control system, the device can satisfy the requirement that the ultra-clean discharged, and desorption temperature is lower, and the adsorbent loss is less simultaneously.
In order to achieve the above object, the integrated adsorption desulfurization and denitrification system of the low-temperature moving bed comprises a catalyst containing SO2The system comprises a NOx flue gas input pipeline, a flue gas induced draft fan, a flue gas waste heat recoverer, a flue gas cooling system, a cold energy recoverer, a low-temperature moving bed adsorption tower and a desorption tower;
containing SO2The NOx flue gas input pipeline is communicated with an inlet of a flue gas waste heat recoverer through a flue gas induced draft fan, an outlet of the flue gas waste heat recoverer is communicated with an inlet of a flue gas cooling system, an outlet of the flue gas cooling system is communicated with a flue gas inlet of a low-temperature moving bed adsorption tower, a porous adsorbent outlet at the bottom of the low-temperature moving bed adsorption tower is communicated with an inlet of a desorption tower, a porous adsorbent outlet of the desorption tower is communicated with a porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower, and a gas outlet of the low-temperature moving bed adsorption tower is communicated with an;
the flue gas cooling system adopts a three-section type spray cooling structure.
The porous adsorbent outlet of the desorption tower is communicated with the porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower through a chain bucket lifting device.
The porous adsorbent is active coke or molecular sieve.
When the device works, the high-temperature flue gas after dust removal is sent into a flue gas waste heat recoverer through a flue gas induced draft fan, and the temperature of the flue gas is reduced to 7 ℃ through the flue gas waste heat recovererThe temperature is below 0 ℃, wherein the recovered heat is used for supplying hot water and steam or for refrigeration, the flue gas after waste heat recovery enters a flue gas cooling system, and is cooled to a temperature region below room temperature by a spray cooling or indirect heat exchange mode, wherein the temperature region above the room temperature is cooled and the heat is taken away by cooling water, and the temperature region below the room temperature is cooled by a refrigeration mode; the cooled flue gas enters a low-temperature moving bed adsorption tower, contacts with a porous adsorbent filled in the low-temperature moving bed adsorption tower, and removes SO in the flue gas in a physical adsorption mode2And NOx, the flue gas output by the low-temperature moving bed adsorption tower enters a cold quantity recoverer to recover cold quantity, the porous adsorbent saturated in adsorption is discharged from the bottom of the low-temperature moving bed adsorption tower in a self-weight blanking mode, enters a desorption tower, and is regenerated in the desorption tower in a heating or vacuumizing mode to desorb SO2And a NOx gas; and feeding the desorbed porous adsorbent to the top of the low-temperature moving bed adsorption tower for reuse.
The utility model discloses following beneficial effect has:
low temperature remove bed integration and adsorb SOx/NOx control system when concrete operation, cool down to the flue gas through flue gas waste heat recoverer and flue gas cooling system, adopt low temperature to remove the bed adsorption tower and carry out SO2And NOx adsorption: adsorption temperature is-100 deg.C-room temperature, adsorption is carried out after cooling and dehumidification, SO2Mainly adopts physical adsorption, has low desorption temperature, low adsorbent loss and low adsorbent replenishment amount, and simultaneously has low SO content at low temperature2The adsorption capacity of NOx and the adsorption agent is large, the filling amount of the adsorbent is small, the adsorption equipment is small, in addition, the NOx is removed in a low-temperature oxidation adsorption mode, NH does not need to be sprayed3And (3) carrying out catalytic reduction, finally separating out a large amount of acidic condensate water in the flue gas cooling process, neutralizing the acidic condensate water, and then supplying the acidic condensate water for power plants, so that the water consumption of the power plants is reduced, and the acidic condensate water can be widely applied to integrated desulfurization and denitrification of flue gas of the power plants, sintering flue gas of steel works, coke oven flue gas and the like.
Drawings
FIG. 1 is a schematic diagram of a prior art structure;
fig. 2 is a schematic structural diagram of the present invention.
Wherein, 1 is a flue gas induced draft fan, 2 is a flue gas waste heat recoverer, 3 is a flue gas cooling system, 4 is a low-temperature moving bed adsorption tower, 5 is a desorption tower, and 6 is a cold recoverer.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings:
referring to fig. 2, the integrated adsorption desulfurization and denitrification system of the low-temperature moving bed comprises a catalyst containing SO2A NOx flue gas input pipeline, a flue gas induced draft fan 1, a flue gas waste heat recoverer 2, a flue gas cooling system 3, a low-temperature moving bed adsorption tower 4 and a desorption tower 5; containing SO2An NOx flue gas input pipeline is communicated with an inlet of a flue gas waste heat recoverer 2 through a flue gas induced draft fan 1, an outlet of the flue gas waste heat recoverer 2 is communicated with an inlet of a flue gas cooling system 3, an outlet of the flue gas cooling system 3 is communicated with a flue gas inlet of a low-temperature moving bed adsorption tower 4, a porous adsorbent outlet at the bottom of the low-temperature moving bed adsorption tower 4 is communicated with an inlet of a desorption tower 5, a porous adsorbent outlet of the desorption tower 5 is communicated with a porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower 4, and a gas outlet of the low-temperature moving bed adsorption tower 4 is communicated with an inlet of; the flue gas cooling system 3 adopts a three-section type spray cooling structure.
A porous adsorbent outlet of the desorption tower 5 is communicated with a porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower 4 through a chain bucket lifting device; the porous adsorbent is active coke or molecular sieve.
When the device works, the dedusted high-temperature flue gas is sent into a flue gas waste heat recoverer 2 through a flue gas induced draft fan 1, the temperature of the flue gas is reduced to be below 70 ℃ through the flue gas waste heat recoverer 2, wherein the recovered heat is used for supplying hot water and steam or for refrigeration, the flue gas after waste heat recovery enters a flue gas cooling system 3, and is cooled to a temperature region below room temperature through a spraying cooling or indirect heat exchange mode, wherein the temperature region above the room temperature is cooled and the heat is taken away through cooling water, and the temperature region below the room temperature is cooled in a refrigeration mode; the cooled flue gas enters the adsorption tower 4 of the low-temperature moving bed and is communicated withThe SO in the flue gas is removed in a physical adsorption mode by contacting with a porous adsorbent filled in a low-temperature moving bed adsorption tower 42And NOx, the flue gas output by the low-temperature moving bed adsorption tower 4 enters a cold energy recoverer to recover cold energy, the porous adsorbent saturated in adsorption is discharged from the bottom of the low-temperature moving bed adsorption tower 4 in a self-weight blanking mode, enters a desorption tower 5, and is regenerated in the desorption tower 5 in a heating or vacuumizing mode to desorb SO2And a NOx gas; the porous adsorbent after the desorption is sent to the top of the low-temperature moving bed adsorption tower 4 for repeated use, if a heating desorption mode is adopted, the desorption tower 5 is provided with a cooling section, and the adsorption material after the desorption is cooled by the cooling section and then sent to the top of the low-temperature moving bed adsorption tower 4.
Flue gas of 600MW coal-fired unit (flue gas flow 200 ten thousand standard square/hour, SO)2Content 3000mg/Nm3NOx content 500mg/Nm3) After dust removal, the mixture was introduced into the apparatuses described in examples and comparative examples.
Examples
As shown in the attached figure 2, the flue gas enters a flue gas waste heat recoverer 2 after being pressurized by a flue gas induced draft fan 1, and the temperature of the flue gas is reduced to 70 ℃ from 120 ℃; the flue gas with the temperature of 70 ℃ enters a flue gas cooling system 3 and is cooled to-20 ℃ in a spray cooling mode. The flue gas cooling system 3 adopts a three-section spray cooling mode: the first section is cooled to 35 ℃ by spraying, the second section is cooled to 5 ℃ by spraying chilled water, the third section is cooled to-20 ℃ by spraying low-temperature calcium chloride solution, the first section of spraying circulating liquid is cooled by cooling water, and the second section of spraying circulating liquid is cooled by a water chiller; the third section of spray circulation liquid (calcium chloride solution) is cooled by a low-temperature refrigerating unit. The low-temperature flue gas cooled to-20 ℃ by the flue gas cooling system 3 enters the low-temperature moving bed adsorption tower 4, in the embodiment, the low-temperature moving bed adsorption tower adopts a cross flow mode, the flue gas horizontally passes through the adsorption bed layer, and the active coke adsorbent vertically flows through the low-temperature moving bed adsorption tower 4 from top to bottom. After the flue gas flows through the low-temperature moving bed adsorption tower 4, SO2Or the NOx content is reduced to 1mg/Nm3Then, the cold is recovered by the cold recovery device 6 and discharged. Suction deviceThe saturated active coke is discharged from the bottom of the low-temperature moving bed adsorption tower 4 and enters the desorption tower 5 through the mode of self-weight blanking. The desorption tower 5 is divided into an upper section and a lower section, the upper section is a heating desorption section, and the active coke with saturated adsorption is desorbed to absorb high-concentration SO under the blowing of hot air at 200 DEG C2And NOx, the lower section is a cooling section, and the temperature of the active coke is reduced to room temperature through cold air purging. The regenerated active coke desorbed by the desorption tower 5 is discharged from the bottom of the desorption tower 5 and is lifted to the top of the low-temperature moving bed adsorption tower 4 through a bucket chain lifting device to be fed, so that closed circulation and continuous operation are formed.
Comparative examples
As shown in the attached figure 1, the flue gas (120 ℃) after dust removal is introduced into an adsorption tower through a fan, the adsorption tower consists of an upper section and a lower section, the lower section is a desulfurization section, and the upper section is a denitration section. The flue gas enters the lower section to be adsorbed and desulfurized, SO2With H in the flue gas2O and O2Reaction to produce H2SO4Is adsorbed by active coke (carbon). Spraying NH into the flue gas after adsorption and desulfurization3Enters the upper section of an adsorption tower, and NOx is catalyzed by NH under the catalytic action of activated coke (carbon)3Reduction to N2And (4) carrying out denitration. The adsorption tower adopts a moving bed mode to adsorb SO2The activated coke (carbon) enters a regeneration tower to be regenerated in a heating way, and SO is desorbed2And the regenerated active coke (carbon) is lifted to the top of the adsorption tower through a chain bucket to be fed and recycled after the working procedures of cooling, screening, ash removal and the like. Because a large amount of active coke (charcoal) is consumed in the regeneration process, fresh active coke (charcoal) needs to be supplemented to maintain the continuous operation of the system.
The main technical parameters of the examples and comparative examples are shown in table 1.
TABLE 1
Figure BDA0002496803620000061
Figure BDA0002496803620000071

Claims (3)

1. A low-temperature moving bed integrated adsorption desulfurization and denitrification system is characterized by comprising a system containing SO2The system comprises a NOx flue gas input pipeline, a flue gas induced draft fan (1), a flue gas waste heat recoverer (2), a flue gas cooling system (3), a low-temperature moving bed adsorption tower (4), a cold energy recoverer (6) and a desorption tower (5);
containing SO2The NOx flue gas input pipeline is communicated with an inlet of a flue gas waste heat recoverer (2) through a flue gas induced draft fan (1), an outlet of the flue gas waste heat recoverer (2) is communicated with an inlet of a flue gas cooling system (3), an outlet of the flue gas cooling system (3) is communicated with a flue gas inlet of a low-temperature moving bed adsorption tower (4), a porous adsorbent outlet at the bottom of the low-temperature moving bed adsorption tower (4) is communicated with an inlet of a desorption tower (5), a porous adsorbent outlet of the desorption tower (5) is communicated with a porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower (4), and a gas outlet of the low-temperature moving bed adsorption tower (4) is communicated with an inlet of a cold energy recoverer (6;
the flue gas cooling system (3) adopts a three-section type spray cooling structure.
2. The integrated adsorption desulfurization and denitrification system for the low-temperature moving bed according to claim 1, wherein the porous adsorbent outlet of the desorption tower (5) is communicated with the porous adsorbent inlet at the top of the low-temperature moving bed adsorption tower (4) through a bucket chain lifting device.
3. The integrated adsorption, desulfurization and denitrification system according to claim 1, wherein the porous adsorbent is activated coke or molecular sieve.
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DE202021101207.2U DE202021101207U1 (en) 2020-05-18 2021-03-10 Integrated adsorption-desulphurisation-denitration system for low-temperature moving bed
JP2021000837U JP3234217U (en) 2020-05-18 2021-03-12 Low temperature moving floor integrated adsorption desulfurization / denitration system

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