CN212790372U - Low temperature fixed bed integration adsorbs SOx/NOx control system - Google Patents
Low temperature fixed bed integration adsorbs SOx/NOx control system Download PDFInfo
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- CN212790372U CN212790372U CN202020832946.5U CN202020832946U CN212790372U CN 212790372 U CN212790372 U CN 212790372U CN 202020832946 U CN202020832946 U CN 202020832946U CN 212790372 U CN212790372 U CN 212790372U
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Abstract
The utility model discloses a low temperature fixed bed integration adsorbs SOx/NOx control system, including containing SO2The system comprises a NOx flue gas input pipeline, a booster fan, a flue gas waste heat recoverer, a cooling system, a flue gas switching device, a cold energy recoverer, a flue gas output pipeline and a plurality of fixed bed adsorption towers; containing SO2The outlet of the NOx flue gas input pipeline is communicated with the inlet of a booster fan, the outlet of the booster fan is communicated with the inlet of a flue gas waste heat recoverer, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a cooling system, and the outlet of the cooling system is communicated with the inlet of a flue gas switching deviceThe outlet of the flue gas switching device is respectively communicated with the inlet of each fixed bed adsorption tower, the outlet of each fixed bed adsorption tower is communicated with the inlet of a cold energy recoverer, and the outlet of the cold energy recoverer is communicated with a flue gas output pipeline.
Description
Technical Field
The utility model belongs to the technical field of flue gas integration SOx/NOx control, a low temperature fixed bed integration 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 N2Active coke asA selective reduction catalyst. 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 fixed bed integration adsorption desulfurization deNOx systems, this system can satisfy the requirement that the flue gas ultra-clean discharged, and regeneration is the loss less.
In order to achieve the above object, the integrated adsorption desulfurization and denitrification system of the low-temperature fixed bed comprises a catalyst containing SO2The system comprises a NOx flue gas input pipeline, a booster fan, a flue gas waste heat recoverer, a cooling system, a flue gas switching device, a cold energy recoverer, a flue gas output pipeline and a plurality of fixed bed adsorption towers;
containing SO2And the outlet of the NOx flue gas input pipeline is communicated with the inlet of a booster fan, the outlet of the booster fan is communicated with the inlet of a flue gas waste heat recoverer, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a cooling system, the outlet of the cooling system is communicated with the inlet of a flue gas switching device, the outlet of the flue gas switching device is respectively communicated with the inlets of the fixed bed adsorption towers, the outlet of each fixed bed adsorption tower is communicated with the inlet of a cold energy recoverer, and the outlet of the cold energy recoverer is communicated with a flue gas output pipeline.
The cooling system is a three-section spraying cooling structure.
The number of the fixed bed adsorption towers is two.
And a porous adsorption material is filled in the fixed bed adsorption tower, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve.
The device also comprises a blowing air pipeline, wherein the blowing air pipeline is communicated with a reverse blowing air inlet of the fixed bed adsorption tower.
During operation, the smoke passes throughContaining SO2And the NOx flue gas input pipeline enters the booster fan, is pressurized by the booster fan and then is sent into the flue gas waste heat recoverer for cooling, then is sent into any fixed bed adsorption tower through the flue gas switching device, is subjected to desulfurization and denitrification treatment through the fixed bed adsorption tower, and the flue gas output by the fixed bed adsorption tower enters the cold energy recoverer for recovering cold energy and is finally discharged through the flue gas output pipeline.
During adsorption, after the fixed bed adsorption tower is saturated in adsorption, the flue gas is input into any other fixed bed adsorption tower through the flue gas switching device, and the saturated fixed bed adsorption tower is regenerated.
The utility model discloses following beneficial effect has:
low temperature fixed bed integration adsorb SOx/NOx control system when concrete operation, through the SO of fixed bed adsorption tower in to the flue gas2Adsorb with NOx and handle, adsorption temperature is lower, simultaneously at the during operation, adopts one to use one mode of preparing, when the fixed bed adsorption tower is saturated, then switches to other fixed bed adsorption towers through flue gas auto-change over device, regenerates the fixed bed adsorption tower of saturation simultaneously to satisfy the requirement of the super clean emission of flue gas, and regeneration is that the loss is less, in addition, the utility model discloses a flue gas waste heat recoverer and cooling system cool off the flue gas, make the flue gas temperature reduce to adsorption temperature-100 deg.C room temperature. The utility model discloses well NOx need not spout into NH through the adsorbed mode desorption of low temperature oxidation3Carrying out catalytic reduction, and meanwhile, carrying out SO treatment on the SO by a fixed adsorption tower at low temperature2The NOx and NOx adsorption capacity is large, the loading amount of the adsorbent is small, the adsorption equipment is small, the investment cost is low, continuous supplement is not needed, and only the adsorbent needs to be supplemented or replaced periodically. In addition, acidic condensate water separated out in the flue gas cooling process can be used by power plants after neutralization treatment, so that the water consumption of the power plants is reduced, and the method can be widely applied to integrated desulfurization and denitrification of flue gas of the power plants, sintering flue gas of steel plants, 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 booster fan, 2 is a flue gas waste heat recoverer, 3 is a cooling system, 4 is a flue gas switching device, 5 is a fixed bed adsorption tower, and 6 is a cold energy 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 fixed bed comprises a catalyst containing SO2The system comprises a NOx flue gas input pipeline, a booster fan 1, a flue gas waste heat recoverer 2, a cooling system 3, a flue gas switching device 4, a cold energy recoverer 6, a flue gas output pipeline and a plurality of fixed bed adsorption towers 5; containing SO2The outlet of the NOx flue gas input pipeline is communicated with the inlet of the booster fan 1, the outlet of the booster fan 1 is communicated with the inlet of the flue gas waste heat recoverer 2, the outlet of the flue gas waste heat recoverer 2 is communicated with the inlet of the cooling system 3, the outlet of the cooling system 3 is communicated with the inlet of the flue gas switching device 4, the outlet of the flue gas switching device 4 is respectively communicated with the inlets of the fixed bed adsorption towers 5, the outlet of each fixed bed adsorption tower 5 is communicated with the inlet of the cold energy recoverer 6, and the outlet of the cold energy recoverer 6 is communicated with the flue gas output pipeline.
The cooling system 3 is of a three-section spraying cooling structure; the number of the fixed bed adsorption towers 5 is two; a porous adsorption material is filled in the fixed bed adsorption tower 5, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve; the utility model discloses still including sweeping the wind pipeline, wherein, sweeping the wind pipeline and being linked together with fixed bed adsorption tower 5's reverse blowing wind entry.
When the device works, the dedusted high-temperature flue gas is introduced into a flue gas waste heat recoverer 2 through a booster fan 1, the temperature of the flue gas is reduced to below 70 ℃, and the recovered heat is used for supplying hot water and steam or for refrigeration; the flue gas after waste heat recovery enters a cooling system 3, and is cooled to a temperature area below room temperature by a spray cooling or indirect heat exchange mode, the temperature area above the room temperature is cooled, heat is taken away by cooling water, and the temperature area below the room temperature is cooled by a refrigeration mode; the cooled flue gas enters a first solid through a flue gas switching device 4In the fixed bed adsorption tower 5, SO in the flue gas is adsorbed and removed at low temperature by contacting with the filled porous adsorption material2And NOx; when the first fixed bed adsorption tower 5 is saturated in adsorption, SO2Or when NOx starts to penetrate, the flue gas is switched to a second fixed bed adsorption tower 5 through a flue gas switching device 4 for SO2Or NOx adsorption while SO is being performed on the adsorbent in the first fixed-bed adsorption tower 5 by heating or vacuum-pumping2And NOx desorption and adsorption material regeneration. When the second fixed bed adsorption tower 5 is saturated in adsorption, SO2Or when the NOx starts to penetrate, the flue gas is switched to the first fixed bed adsorption tower 5 after the desorption is finished through the flue gas switching device 4, and the adsorption and desorption operations are carried out between the two fixed bed adsorption towers 5 in a circulating mode.
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 samples were used in the 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 booster fan 1, and the temperature of the flue gas is reduced from 120 ℃ to 70 ℃; the flue gas with the temperature of 70 ℃ enters a cooling system 3, the temperature is reduced to-20 ℃ in a spray cooling mode, the cooling system 3 adopts a three-section spray cooling mode, wherein the first section is sprayed and cooled to 35 ℃, the second section is sprayed and cooled to 5 ℃ through chilled water, the third section is sprayed and cooled to-20 ℃ through a low-temperature calcium chloride solution, the first section is sprayed and cooled by cooling water, and the second section is sprayed and cooled by a water chiller; the third section of spraying circulation liquid (calcium chloride solution) is cooled by a low-temperature refrigerating unit, the low-temperature flue gas cooled to minus 20 ℃ by the cooling system 3 enters a first fixed bed adsorption tower 5 through a flue gas switching device 4, and SO in the flue gas subjected to desulfurization and denitrification2And NOx content is less than 1mg/Nm3Then the cold energy is recovered by a cold energy recoverer 6 and discharged.
When SO is in the clean flue gas at the outlet of the first fixed bed adsorption tower 52Or NOx content exceeding 1mg/Nm3During the process, the flue gas is switched to a second fixed bed for adsorption through a flue gas switching device 4The tower 5 is used for adsorption desulfurization and denitration. Simultaneously, the hot air with the temperature of 200 ℃ is introduced into the first fixed bed adsorption tower 5 to reversely sweep the bed layer SO as to desorb SO2And NOx, after desorption is finished, introducing cold air to blow and sweep the cooling bed layer; when the second fixed bed adsorption tower 5 is saturated in adsorption, SO in the outlet clean flue gas2Or NOx content exceeding 1mg/Nm3In the meantime, the flue gas is switched to the first fixed bed adsorption tower 5 again by the flue gas switching device 4 to perform the adsorption process, and simultaneously, the desorption and cold blowing operation processes are performed on the second fixed bed adsorption tower 5.
Comparative examples
As shown in the attached figure 1, the flue gas (120 ℃) after dust removal is introduced into a moving bed adsorption tower through a draught fan, the moving bed 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, H formed2SO4Is adsorbed by active coke (carbon). Spraying NH into the flue gas after adsorption and desulfurization3Entering the upper section of a moving bed adsorption tower, and under the catalytic action of activated coke (carbon), NOx is treated by NH3Reduction to N2Denitrating and adsorbing 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 of the moving bed for charging and recycling after working procedures such as 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
| Main technical parameters | Examples | Comparative examples |
| Adsorbent bed type | Fixed bed | Moving bed |
| Adsorption temperature | -20℃ | 120℃ |
| Regeneration temperature | 200℃ | 400℃ |
| SO2Removing mode | Physical adsorption | Chemical adsorption |
| Nox removal mode | Oxidative adsorption | Ammonia injection reduction |
| SO2Efficiency of removal | >99％ | <95％ |
| Nox removal efficiency | >99％ | <80％ |
| Sulfur capacity (mg/g) | 170 | 34 |
| Activated coke loading (t) | 2000 | 8000 |
| Consumption of activated coke (kg/h) | <100 | 1200 |
| Ammonia consumption (kg/h) | 0 | 460 |
Claims (4)
1. A low-temperature fixed bed integrated adsorption desulfurization and denitrification system is characterized by comprising a system containing SO2The system comprises a NOx flue gas input pipeline, a booster fan (1), a flue gas waste heat recoverer (2), a cooling system (3), a flue gas switching device (4), a cold energy recoverer (6), a flue gas output pipeline and a plurality of fixed bed adsorption towers (5);
containing SO2An outlet of the NOx flue gas input pipeline is communicated with an inlet of a booster fan (1), an outlet of the booster fan (1) is communicated with an inlet of a flue gas waste heat recoverer (2), an outlet of the flue gas waste heat recoverer (2) is communicated with an inlet of a cooling system (3), an outlet of the cooling system (3) is communicated with an inlet of a flue gas switching device (4), outlets of the flue gas switching device (4) are respectively communicated with inlets of fixed bed adsorption towers (5), outlets of the fixed bed adsorption towers (5) are communicated with an inlet of a cold energy recoverer (6), and an outlet of the cold energy recoverer (6) is communicated with a flue gas output pipeline;
the cooling system (3) is of a three-section spraying cooling structure.
2. The low-temperature fixed bed integrated adsorption desulfurization and denitrification system according to claim 1, wherein the number of the fixed bed adsorption towers (5) is two.
3. The low-temperature fixed bed integrated adsorption desulfurization and denitrification system according to claim 1, wherein a fixed bed adsorption tower (5) is filled with a porous adsorption material, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve.
4. The integrated adsorption desulfurization and denitrification system of the low-temperature fixed bed according to claim 1, further comprising a purge air pipeline, wherein the purge air pipeline is communicated with a reverse purge air inlet of the fixed bed adsorption tower (5).
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113750741A (en) * | 2021-09-02 | 2021-12-07 | 中国华能集团有限公司 | Flue gas purification system with fluidized bed reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113750741A (en) * | 2021-09-02 | 2021-12-07 | 中国华能集团有限公司 | Flue gas purification system with fluidized bed reactor |
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