CN104061580B - Process ammonia desulfuration equipment and the technique thereof of flue gas desulfurization band liquid - Google Patents
Process ammonia desulfuration equipment and the technique thereof of flue gas desulfurization band liquid Download PDFInfo
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Abstract
The invention belongs to process ammonia desulfuration equipment and the technique thereof of flue gas desulfurization band liquid；Including boiler smoke pipeline and ammonia storage tank, flue is connected with the import of venturi by the exhaust gases passes in smoke evaporative device, ammonia storage tank is connected by the import of the spray equipment that circulating pump is arranged with venturi internal upper part, the outlet of venturi is connected with smoke absorption tower import, under upper, it is sequentially provided with spiral board inside smoke absorption tower, spray irrigation device, high efficient gas and liquid separator and demister, smoke absorption tower side wall between high efficient gas and liquid separator and demister is provided with smoke absorption tower import, the gas outlet of smoke absorption top of tower is connected with chimney breast；Have that equipment is simple, easy to maintenance, operational reliability is good, desulphurization cost and the low advantage of by-products recoveries.
Description
Technical field
The invention belongs to technical field of environment protection equipment, be specifically related to a kind of obvious heat of smoke comprehensive utilization, in flue gas
Entrained drip carries out the ammonia desulfuration equipment processing flue gas desulfurization band liquid and the technique thereof removing and recycling.
Background technology
Ammonia flue gas desulfurization technique is the sulfur dioxide utilizing ammonia to absorb in flue gas, and its reaction is solution-air or gas
-gas phase is reacted, and response speed is fast, and absorbent utilization rate is high, and absorption equipment volume is little.But the ammonia process of desulfurization should
When the desulfurization of fire coal boiler fume, existing all kinds of technology generally also exist ammonia consumption height, aerosol is difficult to
The problem such as elimination, absorbing liquid Crystallization Plugging, flue gas entrained drip.Owing to ammonia type flue gas desulfurizing is to absorb with ammonia
Sulfur dioxide in flue gas generates ammonium sulfate, and with air oxidation after concentration, flue gas, through contact absorbing liquid, is made
Becoming entrained drip in flue gas, drop is contained within moisture, ammonium sulfite, ammonium sulfate, ammonia, flue dust etc., sub-
Ammonium sulfate, ammonium sulfate at pipeline, flue, chimney intercrystalline, cause the equipment such as pipeline, flue, chimney,
Facility burn into blocks.Meanwhile, through chimney with in fume emission to air, surrounding enviroment are polluted.These
The existence of problem makes the enforcement of ammonia-process desulfurization technique run into the biggest obstacle.
Summary of the invention
It is an object of the invention to overcome defect of the prior art, and provide a kind of equipment simple, easy to maintenance,
Operational reliability is good, desulphurization cost and by-products recoveries low process flue gas desulfurization band liquid the ammonia process of desulfurization
Device and technique thereof.
The object of the present invention is achieved like this: includes boiler smoke pipeline and ammonia storage tank, and flue passes through
Exhaust gases passes in smoke evaporative device is connected with the import of venturi, and ammonia storage tank passes through circulating pump and venturi
The import of the spray equipment that internal upper part is arranged is connected, and the outlet of venturi is connected with smoke absorption tower import,
By being sequentially provided with spiral board, spray irrigation device under upper inside smoke absorption tower, high efficient gas and liquid separator and
Demister, the smoke absorption tower side wall between high efficient gas and liquid separator and demister is provided with smoke absorption tower and enters
Mouthful, the gas outlet of smoke absorption top of tower is connected with chimney breast, at the bottom of demister bottom and smoke absorption tower
Smoke absorption tower side wall between portion is provided with smoke absorption tower liquid outlet, and smoke absorption tower liquid outlet leads to
Piping is connected with the first ammonia pump and the second ammonia pump respectively, and described first ammonia pump passes through pipeline and spray
The import of flusher is connected, and described second ammonia pump is connected with oxidator by air ejector, oxidator
The liquid outlet of bottom is connected with the ammonium sulfate passage in smoke evaporative device by ammonium sulfate liquor pump, sulfur
Acid ammonium solution passage is connected with the sulfur ammonium passage in smoke evaporative device by centrifuge, described sulfur ammonium passage and
Finished product sulfur ammonium storage tank is connected, and the overfall of described centrifuge is connected with the slurry reflux mouth on oxidator top.
Described smoke evaporative device includes that exhaust gases passes, exhaust gases passes are provided with copper alloy heat exchange fin, and copper closes
The two ends of gold heat exchange fin are connected with ammonium sulfate passage and sulfur ammonium passage respectively.
The structure of described high efficient gas and liquid separator includes top circuit and lower support beam, the center of top circuit
Position is provided with center connecting plate, is provided with some deflection plates between described center connecting plate and smoke absorption tower
Formula removes mist deflector；Lower support beam includes annular brace beam, sets between annular brace beam and smoke absorption tower
Having reinforcement, described reinforcement is four, and the top of described top circuit is provided with that high-density wear-resistant PP is spherical to be filled out
The bed of material.
Described baffle plate type is except mist deflector is by the upper strata deflector of horizontally set and longitudinally disposed lower floor's baffling
Plate is constituted, and the knuckle in the middle part of lower floor's deflection plate is 30～45 degree, and described upper strata deflector and lower floor deflection plate are
Integrative-structure.
Described some baffle plate types are 30～40cm except the spacing between mist deflector, high-density wear-resistant PP ball
A diameter of the 45 of shape filler～55cm.
The material of described top circuit and lower support beam is 316L rustless steel.
Described some baffle plate types are 35cm except the spacing between mist deflector；Described high-density wear-resistant
A diameter of 50cm of PP Ball-type packing.
The technique of a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid, comprises the steps:
One, boiler smoke is sent in the exhaust gases passes in smoke evaporative device by boiler smoke pipeline, its cigarette
Temperature is 120 DEG C～160 DEG C, and the exhaust gases passes in smoke evaporative device passes through copper alloy heat exchange fin and sulfur
Acid ammonium solution passage and sulfur ammonium passage carry out heat exchange, and the flue-gas temperature after heat exchange is 55～75 DEG C；
Two, during the ammonia in ammonia storage tank enters the spray equipment of venturi internal upper part by circulating pump；
Three, it it is 55～75 DEG C by temperature in the ammonia sprayed by spray equipment in above-mentioned steps two and step one
Flue gas in venturi, carry out one-level gas liquid reaction, generate ammonium sulfite solution, its SOxResponse rate be 90～
98%；
Four, the ammonium sulfite solution in step 3 is made to enter in smoke absorption tower by smoke absorption tower import,
And by after demister, isolate ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters flue gas
The bottom on absorption tower, and respectively enter the first ammonia pump and the second ammonia pump by smoke absorption tower liquid outlet,
The ammonium sulfite solution entering the first ammonia pump is entered in smoke absorption tower by spray irrigation device, makes sulfurous
In the ammonia reacted the most completely in acid ammonium solution and step 4, isolated flue gas carries out two grades of gas liquid reactions, two grades
Ammonium sulfite is generated after gas liquid reaction；
Five, in described step 4, ammonium sulfite after two grades of gas liquid reactions, by demister, is again separate out two
Secondary liquid phase part and secondary gas phase portion, secondary gas phase portion is entered by high efficient gas and liquid separator and spiral board
In chimney breast, entering air eventually through chimney, now the temperature of secondary gas phase portion is 45～60 DEG C,
The smoke content of secondary gas phase portion is less than or equal to 25mg/Nm3, the droplet content of secondary gas phase portion is less than
In 60mg/Nm3；
Six, the bottom of the entrance of the secondary liquid phase part in above-mentioned steps five smoke absorption tower separates with step 4
The ammonium sulfite solution gone out mixes, and becomes liquid phase part after mixing；
Seven, in above-mentioned steps six, mixed liquid phase part enters the first ammonia pump and the second liquefied ammonia by pipeline
In pump；
Eight, above-mentioned steps 7 enters the first mixed liquid phase part of ammonia pump fill again by spray irrigation
Put in entrance smoke absorption tower, recycle；
Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, reach 1.08～
After 1.14, this mixed liquid phase part enters in oxidator through the second ammonia pump by air ejector, when
Mixed liquid phase part is by being oxidized to ammonium sulfate with air contact during air ejector；
Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator enters smoke evaporative by ammonium sulfate liquor pump
In ammonium sulfate passage in device；
11, above-mentioned steps 10 enters the ammonium sulfate in ammonium sulfate passage by step one
Copper alloy heat exchange fin carries out heat exchange concentration, and the solid content volume ratio of the ammonium sulfate after heat exchange concentration is
25～55%；
12, making the ammonium sulfate entrance centrifuge after heat exchange concentration in above-mentioned steps 11, centrifuge divides
The sulfur crystalline ammonium body separated out enters in sulfur ammonium passage, and isolated serosity enters oxidation by slurry reflux mouth 17
Device recycles；
13, the sulfur crystalline ammonium body entering in sulfur ammonium passage in above-mentioned steps 12 is made to close with the copper in step one
Gold heat exchange fin carries out heat exchange and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank.
The ammonia desulfuration equipment processing flue gas desulfurization band liquid made according to such scheme, by arranging smoke evaporative
Device overcomes traditional view and thinks that flue gas is difficult to pass thermal property, utilizes flue gas on the one hand to carry out doctor solution
Evaporation, cooling, on the other hand utilize flue gas to be dried finished product sulfur ammonium, decrease the use of exsiccator,
Thus reduce operating cost further；It is greatly saved tradition ammonia desulfurizing process and produces ammonium sulfate
The a large amount of steam (general consumption vapour 1.5～2.0t/t sulfur ammonium) consumed during post processing, are ensureing normal desulfurization efficiency
Under premise, not only save investment but also greatly reduce operating cost, and do not use exsiccator, thus enter one
Step reduces the cost of operation；Additionally by arranging high efficient gas and liquid separator, it is possible to meet boiler load 40%
The scope of-200%, wide accommodation, increase spherical except mist filler simultaneously, utilize the thrust of flue gas to promote ball
Body rotation and revolution, increase gas-liquid and the spherical contact area except mist filler and time of contact, be sufficiently separated cigarette
Gas and the drop carried secretly, overcome the problem that tradition demister can not well remove cigarette gas carrying liquid；This
By the present invention in that outward with venturi, making absorption spray section sectional area relatively small, gas-to-liquid contact is abundant, it is possible to
Make absorbing liquid fully absorb the hazardous medium in flue gas, reach to remove the purpose of hazardous medium；And due to gas-liquid
Contact is fully, it is possible to making gas obtain washing, purifying further, smoke absorption tower absorbs two grades of sprays of spray section
Drench, it is possible to well utilize the ammonia reacted the most completely and imonium liquid, on the one hand reduce the tradition ammonia process of desulfurization
The ammonia consumption of technique, has saved cost, the most more thoroughly absorbs the hazardous medium in flue gas；Have
Equipment is simple, easy to maintenance, operational reliability is good, desulphurization cost and the low advantage of by-products recoveries.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention；
Fig. 2 is the top view of high efficient gas and liquid separator of the present invention；
Fig. 3 is the A-A view of Fig. 2；
Fig. 4 is the lower support girder construction schematic diagram bottom high efficient gas and liquid separator of the present invention.
Detailed description of the invention
As shown in Figure 1,2,3, 4, the present invention includes boiler smoke pipeline 1 and ammonia storage tank 2, flue
1 is connected with the import of venturi 6 by the exhaust gases passes 3 in smoke evaporative device, and ammonia storage tank 2 is by circulation
Pump 10 is connected with the import of the spray equipment 5 that venturi 6 internal upper part is arranged, the outlet of venturi 6 and flue gas
Absorption tower import 18 is connected, and smoke absorption tower 16 is internal is sequentially provided with spiral board 15, spray under upper
Flusher 4, high efficient gas and liquid separator and demister 14, between high efficient gas and liquid separator and demister 14
Smoke absorption tower 16 sidewall is provided with smoke absorption tower import 18, the gas outlet at smoke absorption tower 16 top
Be connected with chimney breast 19, bottom demister 14 bottom and smoke absorption tower 16 between smoke absorption tower 16
Sidewall is provided with smoke absorption tower liquid outlet 20, smoke absorption tower liquid outlet 20 by pipeline respectively with the
One ammonia pump 11 is connected with the second ammonia pump 12, and described first ammonia pump 11 is filled with spray irrigation by pipeline
Putting the import of 4 to be connected, described second ammonia pump 12 is connected with oxidator 8 by air ejector 7, aoxidizes
The liquid outlet of device 8 bottom is by ammonium sulfate liquor pump 13 and the ammonium sulfate passage 21 in smoke evaporative device
Being connected, ammonium sulfate passage 21 is connected with the sulfur ammonium passage 22 in smoke evaporative device by centrifuge 9,
Described sulfur ammonium passage 22 is connected with finished product sulfur ammonium storage tank 23, the overfall of described centrifuge 9 and oxidator 8
The slurry reflux mouth 17 on top is connected.Described smoke evaporative device includes exhaust gases passes 3, on exhaust gases passes 3
Be provided with copper alloy heat exchange fin 24, the two ends of copper alloy heat exchange fin 24 respectively with ammonium sulfate passage 21
It is connected with sulfur ammonium passage 22.The structure of described high efficient gas and liquid separator includes top circuit and lower support beam,
The center of top circuit is provided with center connecting plate 25, described center connecting plate 25 and smoke absorption tower
Some baffle plate types it are provided with except mist deflector 26 between 16；Lower support beam includes annular brace beam 27, ring
Being provided with reinforcement 28 between shape support beam 27 and smoke absorption tower 16, described reinforcement 28 is four, described
The top of top circuit is provided with high-density wear-resistant PP Ball-type packing layer 29.Described baffle plate type removes mist deflector
26 are made up of upper strata deflector 30 and longitudinally disposed lower floor's deflection plate 31 of horizontally set, lower floor's deflection plate
Knuckle in the middle part of in the of 31 is 30～45 degree, and described upper strata deflector 30 is structure as a whole with lower floor deflection plate 31.
Described some baffle plate types are 30～40cm except the spacing between mist deflector 26, high-density wear-resistant PP ball
A diameter of the 45 of shape filler～55cm.The material of described top circuit and lower support beam is 316L rustless steel.
Described some baffle plate types are 35cm except the spacing between mist deflector 26；Described high-density wear-resistant
A diameter of 50cm of PP Ball-type packing.
The technique of a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid, comprises the steps:
One, boiler smoke is sent in the exhaust gases passes 3 in smoke evaporative device by boiler smoke pipeline 1,
Its flue-gas temperature is 120～160 DEG C, and the exhaust gases passes 3 in smoke evaporative device is by copper alloy heat exchange fin
24 carry out heat exchange with ammonium sulfate passage 21 and sulfur ammonium passage 22, and the flue-gas temperature after heat exchange is 55～75
℃；
Two, during the ammonia in ammonia storage tank 2 enters the spray equipment 5 of venturi 6 internal upper part by circulating pump 10；
Three, it is 55～75 by the ammonia that sprayed by spray equipment 5 in above-mentioned steps two with temperature in step one
DEG C flue gas in venturi 6, carry out one-level gas liquid reaction, generate ammonium sulfite solution, its SOxResponse rate is
90～98%；
Four, the ammonium sulfite solution in step 3 is made to enter smoke absorption tower 16 by smoke absorption tower import 18
In, and by, after demister 14, isolating ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters
Enter the bottom of smoke absorption tower 16, and respectively enter the first ammonia pump by smoke absorption tower liquid outlet 20
11 and second ammonia pump 12, enter the ammonium sulfite solution of the first ammonia pump 11 by spray irrigation device 4
Entering in smoke absorption tower 16, the ammonia reacted the most completely in making ammonium sulfite solution is isolated with step 4
Flue gas carries out two grades of gas liquid reactions, generates ammonium sulfite after two grades of gas liquid reactions；
Five, in described step 4, ammonium sulfite after two grades of gas liquid reactions, by demister 14, is again separate out
Secondary liquid phase part and secondary gas phase portion, secondary gas phase portion passes through high efficient gas and liquid separator and spiral board 15
Enter in chimney breast 19, enter air eventually through chimney, now the temperature of secondary gas phase portion be 45～
60 DEG C, the smoke content of secondary gas phase portion is less than or equal to 25mg/Nm3, the droplet content of secondary gas phase portion
Less than or equal to 60mg/Nm3；
Six, the bottom of the entrance of the secondary liquid phase part in above-mentioned steps five smoke absorption tower 16 and step 4 are divided
The ammonium sulfite solution separated out mixes, and becomes liquid phase part after mixing；
Seven, in above-mentioned steps six, mixed liquid phase part enters the first ammonia pump 11 and the second liquid by pipeline
In ammonia pump 12；
Eight, above-mentioned steps 7 enters the first mixed liquid phase part of ammonia pump 11 again by spray irrigation
Device 4 enters in smoke absorption tower 16, recycles；
Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, reach 1.08～
After 1.14, this mixed liquid phase part enters oxidator 8 through the second ammonia pump 12 by air ejector 7
In, it is oxidized to ammonium sulfate when mixed liquid phase part is by air ejector 7 with air contact；
Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator 8 enters flue gas by ammonium sulfate liquor pump 13
In ammonium sulfate passage 21 in vaporising device；
11, above-mentioned steps 10 enters the ammonium sulfate in ammonium sulfate passage 21 by step one
Copper alloy heat exchange fin 24 carry out heat exchange concentration, the solid content volume ratio of the ammonium sulfate after heat exchange concentration
It is 25～55%；
12, the ammonium sulfate entrance centrifuge 9 after heat exchange concentration, centrifuge 9 in above-mentioned steps 11 are made
Isolated sulfur crystalline ammonium body enters in sulfur ammonium passage 22, and isolated serosity is entered by slurry reflux mouth 17
Enter in oxidator 8 and recycle；
13, the sulfur crystalline ammonium body entering in sulfur ammonium passage 22 in above-mentioned steps 12 is made to close with the copper in step one
Gold heat exchange fin 24 carries out heat exchange and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank 23.
The present invention is ammonia desulfuration equipment and the technique thereof processing flue gas desulfurization band liquid, in conjunction with specific embodiment pair
The present invention is further described.Specific embodiment is as follows:
Embodiment one
The technique of a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid, comprises the steps:
One, boiler smoke is sent in the exhaust gases passes 3 in smoke evaporative device by boiler smoke pipeline 1,
Its flue-gas temperature is 120 DEG C, exhaust gases passes in smoke evaporative device 3 by copper alloy heat exchange fin 24 with
Ammonium sulfate passage 21 and sulfur ammonium passage 22 carry out heat exchange, and the flue-gas temperature after heat exchange is 55 DEG C；
Two, during the ammonia in ammonia storage tank 2 enters the spray equipment 5 of venturi 6 internal upper part by circulating pump 10；
Three, it is 55 DEG C by the ammonia that sprayed by spray equipment 5 in above-mentioned steps two with temperature in step one
Flue gas carries out one-level gas liquid reaction in venturi 6, generates ammonium sulfite solution, its SOxResponse rate is 90%；
Four, the ammonium sulfite solution in step 3 is made to enter smoke absorption tower 16 by smoke absorption tower import 18
In, and by, after demister 14, isolating ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters
Enter the bottom of smoke absorption tower 16, and respectively enter the first ammonia pump by smoke absorption tower liquid outlet 20
11 and second ammonia pump 12, enter the ammonium sulfite solution of the first ammonia pump 11 by spray irrigation device 4
Entering in smoke absorption tower 16, the ammonia reacted the most completely in making ammonium sulfite solution is isolated with step 4
Flue gas carries out two grades of gas liquid reactions, generates ammonium sulfite after two grades of gas liquid reactions；
Five, in described step 4, ammonium sulfite after two grades of gas liquid reactions, by demister 14, is again separate out
Secondary liquid phase part and secondary gas phase portion, secondary gas phase portion passes through high efficient gas and liquid separator and spiral board 15
Entering in chimney breast 19, enter air eventually through chimney, now the temperature of secondary gas phase portion is 45
DEG C, the smoke content of secondary gas phase portion is 15mg/Nm3, the droplet content of secondary gas phase portion is 30mg/Nm3；
Six, the bottom of the entrance of the secondary liquid phase part in above-mentioned steps five smoke absorption tower 16 and step 4 are divided
The ammonium sulfite solution separated out mixes, and becomes liquid phase part after mixing；
Seven, in above-mentioned steps six, mixed liquid phase part enters the first ammonia pump 11 and the second liquid by pipeline
In ammonia pump 12；
Eight, above-mentioned steps 7 enters the first mixed liquid phase part of ammonia pump 11 again by spray irrigation
Device 4 enters in smoke absorption tower 16, recycles；
Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, reaches 1.08
After, this mixed liquid phase part enters in oxidator 8 through the second ammonia pump 12 by air ejector 7,
It is oxidized to ammonium sulfate with air contact when mixed liquid phase part is by air ejector 7；
Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator 8 enters flue gas by ammonium sulfate liquor pump 13
In ammonium sulfate passage 21 in vaporising device；
11, above-mentioned steps 10 enters the ammonium sulfate in ammonium sulfate passage 21 by step one
Copper alloy heat exchange fin 24 carry out heat exchange concentration, the solid content volume ratio of the ammonium sulfate after heat exchange concentration
It is 25%；
12, the ammonium sulfate entrance centrifuge 9 after heat exchange concentration, centrifuge 9 in above-mentioned steps 11 are made
Isolated sulfur crystalline ammonium body enters in sulfur ammonium passage 22, and isolated serosity is entered by slurry reflux mouth 17
Enter in oxidator 8 and recycle；
13, sulfur crystalline ammonium body and the copper in step one entering in sulfur ammonium passage 22 in above-mentioned steps 12 is made
Alloy heat exchange fin 24 carries out heat exchange and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank 23.
Embodiment two
The technique of a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid, comprises the steps:
One, boiler smoke is sent in the exhaust gases passes 3 in smoke evaporative device by boiler smoke pipeline 1,
Its flue-gas temperature is 160 DEG C, exhaust gases passes in smoke evaporative device 3 by copper alloy heat exchange fin 24 with
Ammonium sulfate passage 21 and sulfur ammonium passage 22 carry out heat exchange, and the flue-gas temperature after heat exchange is 75 DEG C；
Two, during the ammonia in ammonia storage tank 2 enters the spray equipment 5 of venturi 6 internal upper part by circulating pump 10；
Three, it is 75 DEG C by the ammonia that sprayed by spray equipment 5 in above-mentioned steps two with temperature in step one
Flue gas carries out one-level gas liquid reaction in venturi 6, generates ammonium sulfite solution, its SOxResponse rate is 98%；
Four, the ammonium sulfite solution in step 3 is made to enter smoke absorption tower 16 by smoke absorption tower import 18
In, and by, after demister 14, isolating ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters
Enter the bottom of smoke absorption tower 16, and respectively enter the first ammonia pump by smoke absorption tower liquid outlet 20
11 and second ammonia pump 12, enter the ammonium sulfite solution of the first ammonia pump 11 by spray irrigation device 4
Entering in smoke absorption tower 16, the ammonia reacted the most completely in making ammonium sulfite solution is isolated with step 4
Flue gas carries out two grades of gas liquid reactions, generates ammonium sulfite after two grades of gas liquid reactions；
Five, in described step 4, ammonium sulfite after two grades of gas liquid reactions, by demister 14, is again separate out
Secondary liquid phase part and secondary gas phase portion, secondary gas phase portion passes through high efficient gas and liquid separator and spiral board 15
Entering in chimney breast 19, enter air eventually through chimney, now the temperature of secondary gas phase portion is 60
DEG C, the smoke content of secondary gas phase portion is equal to 25mg/Nm3, the droplet content of secondary gas phase portion is equal to
60mg/Nm3；
Six, the bottom of the entrance of the secondary liquid phase part in above-mentioned steps five smoke absorption tower 16 and step 4 are divided
The ammonium sulfite solution separated out mixes, and becomes liquid phase part after mixing；
Seven, in above-mentioned steps six, mixed liquid phase part enters the first ammonia pump 11 and the second liquid by pipeline
In ammonia pump 12；
Eight, above-mentioned steps 7 enters the first mixed liquid phase part of ammonia pump 11 again by spray irrigation
Device 4 enters in smoke absorption tower 16, recycles；
Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, reaches 1.14
After, this mixed liquid phase part enters in oxidator 8 through the second ammonia pump 12 by air ejector 7,
It is oxidized to ammonium sulfate with air contact when mixed liquid phase part is by air ejector 7；
Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator 8 enters flue gas by ammonium sulfate liquor pump 13
In ammonium sulfate passage 21 in vaporising device；
11, above-mentioned steps 10 enters the ammonium sulfate in ammonium sulfate passage 21 by step one
Copper alloy heat exchange fin 24 carry out heat exchange concentration, the solid content volume ratio of the ammonium sulfate after heat exchange concentration
It is 55%；
12, the ammonium sulfate entrance centrifuge 9 after heat exchange concentration, centrifuge 9 in above-mentioned steps 11 are made
Isolated sulfur crystalline ammonium body enters in sulfur ammonium passage 22, and isolated serosity is entered by slurry reflux mouth 17
Enter in oxidator 8 and recycle；
13, sulfur crystalline ammonium body and the copper in step one entering in sulfur ammonium passage 22 in above-mentioned steps 12 is made
Alloy heat exchange fin 24 carries out heat exchange and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank 23.
Embodiment three
The technique of a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid, comprises the steps:
One, boiler smoke is sent in the exhaust gases passes 3 in smoke evaporative device by boiler smoke pipeline 1,
Its flue-gas temperature is 140 DEG C, exhaust gases passes in smoke evaporative device 3 by copper alloy heat exchange fin 24 with
Ammonium sulfate passage 21 and sulfur ammonium passage 22 carry out heat exchange, and the flue-gas temperature after heat exchange is 65 DEG C；
Two, during the ammonia in ammonia storage tank 2 enters the spray equipment 5 of venturi 6 internal upper part by circulating pump 10；
Three, it is 65 DEG C by the ammonia that sprayed by spray equipment 5 in above-mentioned steps two with temperature in step one
Flue gas carries out one-level gas liquid reaction in venturi 6, generates ammonium sulfite solution, its SOxResponse rate is 94%；
Four, the ammonium sulfite solution in step 3 is made to enter smoke absorption tower 16 by smoke absorption tower import 18
In, and by, after demister 14, isolating ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters
Enter the bottom of smoke absorption tower 16, and respectively enter the first ammonia pump by smoke absorption tower liquid outlet 20
11 and second ammonia pump 12, enter the ammonium sulfite solution of the first ammonia pump 11 by spray irrigation device 4
Entering in smoke absorption tower 16, the ammonia reacted the most completely in making ammonium sulfite solution is isolated with step 4
Flue gas carries out two grades of gas liquid reactions, generates ammonium sulfite after two grades of gas liquid reactions；
Five, in described step 4, ammonium sulfite after two grades of gas liquid reactions, by demister 14, is again separate out
Secondary liquid phase part and secondary gas phase portion, secondary gas phase portion passes through high efficient gas and liquid separator and spiral board 15
Entering in chimney breast 19, enter air eventually through chimney, now the temperature of secondary gas phase portion is 52.5
DEG C, the smoke content of secondary gas phase portion is equal to 20mg/Nm3, the droplet content of secondary gas phase portion is equal to
50mg/Nm3；
Six, the bottom of the entrance of the secondary liquid phase part in above-mentioned steps five smoke absorption tower 16 and step 4 are divided
The ammonium sulfite solution separated out mixes, and becomes liquid phase part after mixing；
Seven, in above-mentioned steps six, mixed liquid phase part enters the first ammonia pump 11 and the second liquid by pipeline
In ammonia pump 12；
Eight, above-mentioned steps 7 enters the first mixed liquid phase part of ammonia pump 11 again by spray irrigation
Device 4 enters in smoke absorption tower 16, recycles；
Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, reaches 1.11
After, this mixed liquid phase part enters in oxidator 8 through the second ammonia pump 12 by air ejector 7,
It is oxidized to ammonium sulfate with air contact when mixed liquid phase part is by air ejector 7；
Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator 8 enters flue gas by ammonium sulfate liquor pump 13
In ammonium sulfate passage 21 in vaporising device；
11, above-mentioned steps 10 enters the ammonium sulfate in ammonium sulfate passage 21 by step one
Copper alloy heat exchange fin 24 carry out heat exchange concentration, the solid content volume ratio of the ammonium sulfate after heat exchange concentration
It is 40%；
12, the ammonium sulfate entrance centrifuge 9 after heat exchange concentration, centrifuge 9 in above-mentioned steps 11 are made
Isolated sulfur crystalline ammonium body enters in sulfur ammonium passage 22, and isolated serosity is entered by slurry reflux mouth 17
Enter in oxidator 8 and recycle；
13, sulfur crystalline ammonium body and the copper in step one entering in sulfur ammonium passage 22 in above-mentioned steps 12 is made
Alloy heat exchange fin 24 carries out heat exchange and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank 23.
Above-described embodiment is only for clearly demonstrating example, and not restriction to embodiment.Right
For the general technical staff of art, other not similar shape can also be made on the basis of the above description
The change of formula or variation.Here without also cannot all of embodiment be given exhaustive, and be thus amplified
Go out obviously changes or changes among still in the invention scope of the claims.
Claims (8)
- null1. the ammonia desulfuration equipment processing flue gas desulfurization band liquid，Including boiler smoke pipeline (1) and ammonia storage tank (2)，It is characterized in that: boiler smoke pipeline (1) is connected with the import of venturi (6) by the exhaust gases passes (3) in smoke evaporative device，Ammonia storage tank (2) is connected by the import of the spray equipment (5) that circulating pump (10) is arranged with venturi (6) internal upper part，The outlet of venturi (6) is connected with smoke absorption tower import (18)，Smoke absorption tower (16) is internal is sequentially provided with spiral board (15) under upper、Spray irrigation device (4)，High efficient gas and liquid separator and demister (14)，Smoke absorption tower (16) sidewall between high efficient gas and liquid separator and demister (14) is provided with smoke absorption tower import (18)，The gas outlet at smoke absorption tower (16) top is connected with chimney breast (19)，Smoke absorption tower (16) sidewall between demister (14) bottom and smoke absorption tower (16) bottom is provided with smoke absorption tower liquid outlet (20)，Smoke absorption tower liquid outlet (20) is connected with the first ammonia pump (11) and the second ammonia pump (12) respectively by pipeline，Described first ammonia pump (11) is connected with the import of spray irrigation device (4) by pipeline，Described second ammonia pump (12) is connected with oxidator (8) by air ejector (7)，The liquid outlet of oxidator (8) bottom is connected with the ammonium sulfate passage (21) in smoke evaporative device by ammonium sulfate liquor pump (13)，Ammonium sulfate passage (21) is connected with sulfur ammonium passage (22) in smoke evaporative device by centrifuge (9)，Described sulfur ammonium passage (22) is connected with finished product sulfur ammonium storage tank (23)，The overfall of described centrifuge (9) is connected with the slurry reflux mouth (17) on oxidator (8) top.
- 2. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 1 according to right, it is characterized in that: described smoke evaporative device includes exhaust gases passes (3), exhaust gases passes (3) is provided with copper alloy heat exchange fin (24), and the two ends of copper alloy heat exchange fin (24) are connected with ammonium sulfate passage (21) and sulfur ammonium passage (22) respectively.
- 3. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 1 according to right, it is characterized in that: the structure of described high efficient gas and liquid separator includes top circuit and lower support beam, the center of top circuit is provided with center connecting plate (25), is provided with some baffle plate types except mist deflector (26) between described center connecting plate (25) and smoke absorption tower (16)；Lower support beam includes annular brace beam (27), reinforcement (28) it is provided with between annular brace beam (27) and smoke absorption tower (16), described reinforcement (28) is four, and the top of described top circuit is provided with high-density wear-resistant PP Ball-type packing layer (29).
- 4. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 3 according to right, it is characterized in that: described baffle plate type is made up of upper strata deflector (30) and longitudinally disposed lower floor's deflection plate (31) of horizontally set except mist deflector (26), the knuckle at lower floor's deflection plate (31) middle part is 30～45 degree, and described upper strata deflector (30) is structure as a whole with lower floor's deflection plate (31).
- 5. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 3 according to right, it is characterized in that: described some baffle plate types are 30～40cm except the spacing between mist deflector (26), a diameter of the 45～55cm of high-density wear-resistant PP Ball-type packing.
- 6. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 3 according to right, it is characterised in that: the material of described top circuit and lower support beam is 316L rustless steel.
- 7. want the ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 5 according to right, it is characterised in that: described some baffle plate types are 35cm except the spacing between mist deflector (26)；A diameter of 50cm of described high-density wear-resistant PP Ball-type packing.
- 8. the technique wanting a kind of ammonia desulfuration equipment processing flue gas desulfurization band liquid described in 1 according to right, it is characterised in that: comprise the steps:One, boiler smoke is sent in the exhaust gases passes (3) in smoke evaporative device by boiler smoke pipeline (1), its flue-gas temperature is 120～160 DEG C, exhaust gases passes (3) in smoke evaporative device carries out heat exchange by copper alloy heat exchange fin (24) with ammonium sulfate passage (21) and sulfur ammonium passage (22), and the flue-gas temperature after heat exchange is 55～75 DEG C；Two, during the ammonia in ammonia storage tank (2) enters the spray equipment (5) of venturi (6) internal upper part by circulating pump (10)；Three, it is that the flue gas of 55～75 DEG C carries out one-level gas liquid reaction in venturi (6) by the ammonia sprayed by spray equipment (5) in above-mentioned steps two and temperature in step one, generates ammonium sulfite solution, its SOxResponse rate is 90～98%；Four, the ammonium sulfite solution in step 3 is made to enter in smoke absorption tower (16) by smoke absorption tower import (18), and by after demister (14), isolate ammonium sulfite solution and flue gas, wherein, ammonium sulfite solution enters the bottom of smoke absorption tower (16), and respectively enter the first ammonia pump (11) and the second ammonia pump (12) by smoke absorption tower liquid outlet (20), the ammonium sulfite solution entering the first ammonia pump (11) enters in smoke absorption tower (16) by spray irrigation device (4), the ammonia reacted the most completely in making ammonium sulfite solution carries out two grades of gas liquid reactions with isolated flue gas in step 4, ammonium sulfite is generated after two grades of gas liquid reactions；Five, in described step 4 ammonium sulfite after two grades of gas liquid reactions by demister (14), it is again separate out secondary liquid phase part and secondary gas phase portion, secondary gas phase portion enters in chimney breast (19) by high efficient gas and liquid separator and spiral board (15), air is entered eventually through chimney, now the temperature of secondary gas phase portion is 45～60 DEG C, and the smoke content of secondary gas phase portion is less than or equal to 25mg/Nm3, the droplet content of secondary gas phase portion is less than or equal to 60mg/Nm3；Six, the bottom ammonium sulfite solution isolated with step 4 of entrance smoke absorption tower of the secondary liquid phase part in above-mentioned steps five (16) mixes, and becomes liquid phase part after mixing；Seven, in above-mentioned steps six, mixed liquid phase part is entered in the first ammonia pump (11) and the second ammonia pump (12) by pipeline；Eight, above-mentioned steps 7 enters the first ammonia pump (11) mixed liquid phase part and enters in smoke absorption tower (16) again by spray irrigation device (4), recycle；Nine, the mixed liquid phase part in above-mentioned steps seven measures proportion through manual sampling, after reaching 1.08～1.14, this mixed liquid phase part enters in oxidator (8) through the second ammonia pump (12) by air ejector (7), is oxidized to ammonium sulfate when mixed liquid phase part is by air ejector (7) with air contact；Ten, in above-mentioned steps nine, the ammonium sulfate in oxidator (8) is entered in the ammonium sulfate passage (21) in smoke evaporative device by ammonium sulfate liquor pump (13)；11, the ammonium sulfate entered in above-mentioned steps ten in ammonium sulfate passage (21) carries out heat exchange concentration by the copper alloy heat exchange fin (24) in step one, and the solid content volume ratio of the ammonium sulfate after heat exchange concentration is 25～55%；12, ammonium sulfate entrance centrifuge (9) after heat exchange concentration in above-mentioned steps 11 is made, centrifuge (9) isolated sulfur crystalline ammonium body enters in sulfur ammonium passage (22), and isolated serosity is entered in oxidator (8) by slurry reflux mouth (17) and recycles；13, the sulfur crystalline ammonium body made in above-mentioned steps 12 in entrance sulfur ammonium passage (22) carries out heat exchange with the copper alloy heat exchange fin (24) in step one and is dried, and dried sulfur crystalline ammonium body enters in finished product sulfur ammonium storage tank (23).
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| CN115286012B (en) * | 2022-07-27 | 2023-10-31 | 南京延长反应技术研究院有限公司 | Reaction system and reaction method for preparing sodium carbonate |
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