CN108975285A - A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization - Google Patents
A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization Download PDFInfo
- Publication number
- CN108975285A CN108975285A CN201810934729.4A CN201810934729A CN108975285A CN 108975285 A CN108975285 A CN 108975285A CN 201810934729 A CN201810934729 A CN 201810934729A CN 108975285 A CN108975285 A CN 108975285A
- Authority
- CN
- China
- Prior art keywords
- gas
- level
- oxidation
- unit
- process gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 287
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 239000001117 sulphuric acid Substances 0.000 title claims abstract description 19
- 235000011149 sulphuric acid Nutrition 0.000 title claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 305
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 148
- 238000001816 cooling Methods 0.000 claims abstract description 90
- 239000002253 acid Substances 0.000 claims abstract description 83
- 238000011084 recovery Methods 0.000 claims abstract description 38
- 239000000428 dust Substances 0.000 claims abstract description 33
- 238000002485 combustion reaction Methods 0.000 claims abstract description 31
- 239000002918 waste heat Substances 0.000 claims abstract description 20
- 150000007513 acids Chemical class 0.000 claims abstract description 16
- 238000005516 engineering process Methods 0.000 claims abstract description 11
- 230000003647 oxidation Effects 0.000 claims description 107
- 239000003054 catalyst Substances 0.000 claims description 40
- 238000009833 condensation Methods 0.000 claims description 32
- 230000005494 condensation Effects 0.000 claims description 32
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 28
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 13
- 229910002026 crystalline silica Inorganic materials 0.000 claims description 13
- 235000012239 silicon dioxide Nutrition 0.000 claims description 13
- 229910021529 ammonia Inorganic materials 0.000 claims description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 10
- 239000003085 diluting agent Substances 0.000 claims description 8
- 239000000446 fuel Substances 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 6
- 239000012717 electrostatic precipitator Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 16
- 239000005864 Sulphur Substances 0.000 abstract description 13
- 238000006477 desulfuration reaction Methods 0.000 abstract description 5
- 230000023556 desulfurization Effects 0.000 abstract description 5
- 239000000498 cooling water Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000001035 drying Methods 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000008246 gaseous mixture Substances 0.000 description 8
- 239000011521 glass Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 239000002699 waste material Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 239000011449 brick Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- VDGJOQCBCPGFFD-UHFFFAOYSA-N oxygen(2-) silicon(4+) titanium(4+) Chemical compound [Si+4].[O-2].[O-2].[Ti+4] VDGJOQCBCPGFFD-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a kind of wet process sulphuric acid plant and wet desulphurization method, which includes being sequentially connected logical technique combustion unit, waste heat recovery unit, process gas dust removing units, denitration unit, level-one SO2Aoxidize cooling unit, primary acids processing unit, second level SO2Oxidation unit, second level acid processing unit and tail gas treating unit.The present invention is in such a way that two-stage converts condensed in two stages, so that the rate of recovery of sulphur is up to 99.9% or more in process gas；Using advanced control of acid fog technology, without drying, wet process is catalyzed relieving haperacidity, SO during guarantee3And H2O, which is directly condensed, generates sulfuric acid, while having achieved the purpose that gas desulfurization and purification, and tail gas can directly meet discharge standard；Process unit recycles a large amount of mesohigh steam simultaneously, and low energy consumption, and heat recovery efficiency is high, and cooling-water consumption is low, and operating cost also accordingly substantially reduces.It can be combined with SCR denitration process in the process, realize the desulfurization and denitrification integral of refinery processes gas.
Description
Technical field
The present invention relates to the wet process gas sulphur-containing exhaust gas/waste acidity recovery Sulphuric acid technical fields of industry, more particularly to one kind
Wet process sulphuric acid plant and a kind of method of wet desulphurization.
Background technique
With the variation of environment and the shortage of the energy, sulphur from now on is become using high-effect and high benefit sulfur recovery technology
The inexorable trend of recovery process development, and there is realistic meaning.The sulfur recovery method of current acid gas mainly has wet desulphurization
And dry desulfurization.It is dry method sulfur recovery that domestic petroleum petrochemical industry is widely used at present, main using traditional Crouse
(Claus) technique.Traditional Crouse (Claus) process flow is long, and equipment is more, cannot handle sour gas and spent acid simultaneously, acid
Property process gas need dehydrate after just can be carried out processing.Therefore it needs the efficient and succinct wet process sulphur-containing exhaust gas of one kind and gives up
The recovery process of acid.
Summary of the invention
In view of the defects and deficiencies of the prior art, the present invention intends to provide a kind of process flow is short, compact layout,
Production cost is low, sulphur high conversion rate, tail gas can direct emission wet process sulphuric acid plant；It additionally provides one kind and can be achieved at the same time and contain
The wet desulphurization method of sulphur exhaust gas and spent acid.
To achieve the above object, the present invention provides following schemes:
The present invention provides a kind of wet process sulphuric acid plant, including being sequentially connected logical technique combustion unit, waste heat recycling list
Member, process gas dust removing units, denitration unit, level-one SO2Aoxidize cooling unit, primary acids processing unit, second level SO2Oxidation unit,
Second level acid processing unit and tail gas treating unit, the level-one SO2Aoxidizing cooling unit includes level-one SO2Oxidation reactor and
From top to bottom it is successively set on the level-one SO2The first SO in oxidation reactor2Cooler between layer of oxidation catalyst, first,
2nd SO2Cooler between layer of oxidation catalyst, secondary process hot-air heater and second, the level-one SO2Oxidation reactor into
Port is connected with the gas outlet of the out of stock unit, and the primary acids processing unit includes first-stage condenser and with described one
The the first control of acid fog device and the first cooling blower that grade condenser is connected, the level-one SO2The gas outlet of oxidation reactor with
The air inlet of the first-stage condenser is connected, the second level SO2Oxidation unit includes that process gas mixer, level-one process gas add
Hot device and second level SO2Oxidation reactor, the air inlet of the process gas mixer gas outlet with the first-stage condenser respectively
With the second level SO2The air inlet pipeline of oxidation reactor is connected, the air inlet of the level-one technique hot-air heater respectively with institute
State process gas mixer and the second level SO2The gas outlet of oxidation reactor is connected, and the level-one technique hot-air heater goes out
Port and the second level SO2The air inlet of oxidation reactor is connected, the gas outlet of the level-one technique hot-air heater with it is described
Second level SO2Cooler between pipeline between the air inlet of oxidation reactor passes through described second, the second level SO2Oxidation reaction
The 3rd SO is provided in device2Layer of oxidation catalyst, the second level acid processing unit include secondary condenser, the second control of acid fog
Device, the second cooling blower and sulfuric acid storage tank, the gas outlet of the level-one technique hot-air heater also with the secondary condenser into
Port is connected, and the secondary condenser is connected with the second control of acid fog device and second cooling blower respectively, institute
It states first-stage condenser and the secondary condenser is connected with the sulfuric acid storage tank, the gas outlet of the secondary condenser and institute
Tail gas treating unit is stated to be connected.
Preferably, the technique combustion unit includes process gas burning boiler, and the waste heat recovery unit includes waste heat
Boiler and air preheater are recycled, the process gas dust removing units include electrostatic precipitator, and the denitration unit includes that liquefied ammonia steams
Send out device, ammonia/sky mixer, diluent air, ammonia-spraying grid, Benitration reactor and denitrating catalyst, the tail gas treating unit packet
Include cleaning technology Gas Cooler and demister.
Preferably, the technique combustion unit further includes stair oxidation blower, one end of the stair oxidation blower with
The process gas burning boiler is connected, the other end of the stair oxidation blower respectively with the first-stage condenser and described two
The gas outlet of grade condenser is connected.
Preferably, the gas outlet of the level-one technique hot-air heater and the second level SO2The air inlet of oxidation reactor it
Between pipeline on be provided with auxiliary burner, the auxiliary burner is close to the second level SO2Oxidation reactor；
Secondary process gas oxidation fan is provided between the process gas mixer and the level-one technique hot-air heater；
The air preheater is connected with the burning boiler.
Preferably, the gas outlet of the first-stage condenser is connected with the air inlet of the secondary condenser.
It preferably, further include a drum, cooler, the secondary process gas add the drum between described first respectively
Hot device is connected with the heat recovery boiler.
The present invention also provides a kind of method that described device by adopting the above technical scheme carries out wet desulphurization, including it is following
Step:
(1) process gas and fuel are passed through the technique combustion unit and carry out combustion oxidation, obtained containing SO2Technique
Gas；The process gas contains sour gas and acid solution, H in the sour gas2The volume content of S is 3~60%；
(2) contain SO for what the step (1) obtained2Process gas by waste heat recovery unit carry out it is cooling after, obtain
Cooling technique gas enter back into process gas dust removing units and be dusted processing, obtain except dust and gas；
(3) denitration process is carried out except dust and gas is passed through the denitration unit by what the step (2) obtained, obtains denitration gas；
(4) the denitration gas that the step (3) obtains is passed through level-one SO2Oxidation cooling unit carries out oxidation cooling, obtains
Containing SO3Process gas；
(5) step (4) is obtained containing SO3Process gas and crystalline silica nuclei to be passed through primary acids processing unit mixed
It closes, carries out condensation process, the sulfuric acid and remaining process gas that separation condensation generates；
(6) the remaining process gas that the step (5) obtains is passed through second level SO2After oxidation unit is aoxidized, it will aoxidize
Product is passed into second level acid processing unit and carries out condensation process, obtains the sulfuric acid that condensation generates, and residual gas is passed through vent gas treatment
Unit carries out vent gas treatment.
Preferably, the temperature of combustion oxidation is 1000~1200 DEG C in the step (1).
Preferably, the mode of the oxidation cooling in the step (4) includes: that the denitration gas and air are passed through level-one
SO2After oxidation reactor mixing, the first SO is flowed through2Layer of oxidation catalyst is in the first SO2It is described de- under the action of oxidation catalyst
Part SO in niter air2It is oxidized to SO3, cooler is cooled to 410~430 DEG C between mixed gas enters first after then aoxidizing；
Pass through the 2nd SO2Layer of oxidation catalyst is in the 2nd SO2Under the action of oxidation catalyst, part SO in gas after the cooling2Oxygen
Turn to SO3, the mixed gas of the second oxidation sequentially enter cooler between secondary process hot-air heater and second be cooled to 280~
300℃。
Preferably, the temperature of the remaining process gas in the step (5) is 145~165 DEG C；
The temperature of residual gas is 85~105 DEG C in the step (6).
The present invention achieve compared with the existing technology it is following the utility model has the advantages that
Process gas and fuel are passed through the technique combustion unit and carry out combustion oxidation by the present invention, are obtained containing SO2's
Process gas；The process gas contains sour gas and acid solution, H in the sour gas2The volume content of S is 3~60%；So
Contain SO for obtained afterwards2Process gas by waste heat recovery unit carry out it is cooling after, obtained cooling technique gas enters back into
Process gas dust removing units are dusted processing, obtain except dust and gas；Denitration process then is carried out except dust and gas is passed through the denitration unit,
Obtain denitration gas；Denitration gas is passed through level-one SO again2Oxidation cooling unit carries out oxidation cooling, obtains containing SO3Process gas, with
Crystalline silica nuclei is passed through the mixing of primary acids processing unit, carries out condensation process, the sulfuric acid and remaining technique that separation condensation generates
Gas；Obtained remaining process gas is passed through secondary oxidation unit and carries out after aoxidizing cooling, carries out at condensation in second level acid processing unit
Reason, obtains the sulfuric acid that condensation generates, and residual gas is passed through tail gas treating unit and carries out vent gas treatment.
The present invention is in such a way that two-stage converts condensed in two stages, so that the rate of recovery of sulphur reaches as high as 99.9% in process gas
More than；The present invention uses advanced control of acid fog technology, and without drying, process flow is short, and wet process is catalyzed relieving haperacidity, during guarantee
SO3And H2O, which is directly condensed, generates sulfuric acid.It can get the industrial concentrated sulfuric acid and steam of commodity grade standard, while having reached gas sweetening
The purpose of purification, tail gas can directly meet discharge standard；And do not need to consume in wet desulfurizing process any chemicals or its
Its additive, also without spent acid and other waste liquid outlets, environmental protection pressure is small.
Wet process sulphuric acid plant equipment of the present invention is few, and compact layout, occupied area is small, and capital cost is low；Using described
Device carries out in process of wet desulphurization, and raw material composition, charging quantity etc., which fluctuate widely, will not influence device normal operation, especially
It is not influenced by the components such as hydro carbons, cyanide, carbide in raw material, and then the present invention adapts to wide scope of material, can locate simultaneously
Managing most sulphur-containing exhaust gas such as sour gas, Waste Sulfuric Acid and spent acid, sour gas allows NH without dehydration in raw material3
With the presence of hydro carbons.The device can recycle a large amount of mesohigh steam simultaneously, and low energy consumption, and heat recovery efficiency is high, cooling-water consumption
Low, operating cost also accordingly substantially reduces.In addition, can be combined with SCR denitration process in the process, refinery processes gas is realized
Desulfurization and denitrification integral.
Detailed description of the invention
It in order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, below will be to institute in embodiment
Attached drawing to be used is needed to be briefly described, it should be apparent that, the accompanying drawings in the following description is only some implementations of the invention
Example, for those of ordinary skill in the art, without any creative labor, can also be according to these attached drawings
Obtain other attached drawings.
Fig. 1 is the overall structure diagram of wet process sulphuric acid plant of the present invention；
Wherein, 1- technique combustion unit, 2- waste heat recovery unit, 3- process gas dust removing units, 4- denitration unit, 5- mono-
Grade SO2Aoxidize cooling unit, 6- primary acids processing unit, 7- second level SO2Oxidation unit, 8- second level acid processing unit, at 9- tail gas
Manage unit, 10- level-one SO2Oxidation reactor, the first SO of 11-2Cooler, 13- second between layer of oxidation catalyst, 12- first
SO2Layer of oxidation catalyst, 14- secondary process hot-air heater, cooler, 16- first-stage condenser, the first acid of 17- between 15- second
Mist controller, 19- process gas mixer, 20- level-one technique hot-air heater, 21- second level SO2Oxidation reactor, the 3rd SO of 22-2Oxygen
It is auxiliary to change catalyst layer, 23- secondary condenser, the second control of acid fog of 24- device, 26- sulfuric acid storage tank, 27- stair oxidation blower, 28-
Combustion-supporting burner, 29- secondary process gas oxidation fan, 30- drum.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
In view of the defects and deficiencies of the prior art, the present invention intends to provide a kind of process flow is short, compact layout,
Production cost is low, sulphur high conversion rate, tail gas can direct emission wet process sulphuric acid plant.
In order to make the foregoing objectives, features and advantages of the present invention clearer and more comprehensible, with reference to the accompanying drawing and specific real
Applying mode, the present invention is described in further detail.
As shown in Figure 1, the present invention provides a kind of wet process sulphuric acid plant, including be sequentially connected logical technique combustion unit 1,
Waste heat recovery unit 2, process gas dust removing units 3, denitration unit 5, level-one SO2Aoxidize cooling unit 5, primary acids processing unit 6,
Second level SO2Oxidation unit 7, second level acid processing unit 8 and tail gas treating unit 9, the level-one SO2Aoxidizing cooling unit 5 includes one
Grade SO2Oxidation reactor 10 and from top to bottom it is successively set on the level-one SO2The first SO in oxidation reactor 102Oxidation
Cooler 12, the 2nd SO between catalyst layer 11, first2Layer of oxidation catalyst 13, secondary process hot-air heater 14 and second
Between cooler 15, the level-one SO2The air inlet of oxidation reactor 10 is connected with the gas outlet of the out of stock unit, and described one
The sour processing unit 6 of grade include first-stage condenser 16 and the first control of acid fog device 17 being connected with the first-stage condenser 16 and
The first cooling blower being connected with the first-stage condenser 16, the level-one SO2The gas outlet of oxidation reactor and described one
The air inlet of grade condenser 16 is connected, the second level SO2Oxidation unit 7 adds including process gas mixer 19, level-one process gas
Hot device 20 and second level SO2Oxidation reactor 21, the air inlet of the process gas mixer 19 respectively with the first-stage condenser 16
Gas outlet and the second level SO2The air inlet pipeline of oxidation reactor 21 is connected, the level-one technique hot-air heater 20 into
Port respectively with the process gas mixer 19 and the second level SO2The gas outlet of oxidation reactor 21 is connected, the level-one
The gas outlet of technique hot-air heater 20 and the second level SO2The air inlet of oxidation reactor 21 is connected, the level-one process gas
The gas outlet of heater 20 and the second level SO2Pipeline between the air inlet of oxidation reactor 21 is cold between passing through described second
But device 15, the second level SO2The 3rd SO is provided in oxidation reactor 212Layer of oxidation catalyst 22, the second level acid processing unit
8 include secondary condenser 23, the second control of acid fog device 24, the second cooling blower and sulfuric acid storage tank 26, and the level-one process gas adds
The gas outlet of hot device 20 is also connected with the air inlet of the secondary condenser 23, and the secondary condenser 23 is respectively with described
Two acid mist controllers 24 are connected with second cooling blower, the first-stage condenser 16 and the secondary condenser 23 with
The sulfuric acid storage tank 26 is connected, and the gas outlet of the secondary condenser 23 is connected with the tail gas treating unit 9.
Wherein, heretofore described technique combustion unit 1 includes process gas burning boiler, the waste heat recovery unit 2
Including heat recovery boiler and air preheater, the process gas dust removing units 3 include electrostatic precipitator, the denitration unit 4
Including liquid ammonia evaporator, ammonia/sky mixer, diluent air, ammonia-spraying grid, Benitration reactor and denitrating catalyst, the tail gas
Processing unit 9 includes cleaning technology Gas Cooler and demister.
Heretofore described technique combustion unit 1 further includes stair oxidation blower 27, the stair oxidation blower 27
One end is connected with the process gas burning boiler, the other end of the stair oxidation blower 27 respectively with the first-stage condenser
16 are connected with the gas outlet of the secondary condenser 23.
The gas outlet of heretofore described level-one technique hot-air heater 20 and the second level SO2The air inlet of oxidation reactor 21
It is provided with auxiliary burner 28 on pipeline between mouthful, the auxiliary burner 28 is close to the second level SO2Oxidation reactor 21.
Secondary process is provided between heretofore described process gas mixer 19 and the level-one technique hot-air heater 20
Gas oxidation fan 29.
Heretofore described air preheater is connected with the burning boiler.
The gas outlet of heretofore described first-stage condenser 16 is connected with the air inlet of the secondary condenser 23.
It further include a drum 30 in the present invention, the drum 30 cooler 12, the second level between described first respectively
Technique hot-air heater 14 is connected with the heat recovery boiler.
The present invention also provides a kind of method that described device by adopting the above technical scheme carries out wet desulphurization, including it is following
Step:
(1) process gas and fuel are passed through the technique combustion unit and carry out combustion oxidation, obtained containing SO2Technique
Gas；The process gas contains sour gas and acid solution, H in the sour gas2The volume content of S is 3~60%；
(2) contain SO for what the step (1) obtained2Process gas by waste heat recovery unit carry out it is cooling after, obtain
Cooling technique gas enter back into process gas dust removing units and be dusted processing, obtain except dust and gas；
(3) denitration process is carried out except dust and gas is passed through the denitration unit by what the step (2) obtained, obtains denitration gas；
(4) the denitration gas that the step (3) obtains is passed through level-one SO2Oxidation cooling unit carries out oxidation cooling, obtains
Containing SO3Process gas；
(5) step (4) is obtained containing SO3Process gas and crystalline silica nuclei to be passed through primary acids processing unit mixed
It closes, carries out condensation process, the sulfuric acid and remaining process gas that separation condensation generates；
(6) the remaining process gas that the step (5) obtains is passed through second level SO2After oxidation unit is aoxidized, in second level
Sour processing unit carries out condensation process, obtains the sulfuric acid that condensation generates, and residual gas is passed through tail gas treating unit and carries out at tail gas
Reason.
Process gas and fuel are passed through technique combustion unit and carry out combustion oxidation by the present invention, are obtained containing SO2Technique
Gas.In the present invention, the process gas contains sour gas and acid solution, H in the sour gas2The volume content of S is 3
~60%, preferably 10~50%, further preferably 15~30%.In the present invention, the sour gas preferably also contains
SO2、CS2With one of COS or a variety of.In the present invention, the component of the acid solution is preferably the acidity containing element sulphur
Solution.The present invention does not have particular/special requirement to the source of the process gas, any to contain aforementioned volume content H2Exhaust gas, the waste liquid of S
Or gas-liquid mixture.
The present invention does not have particular/special requirement to the fuel, any enables to work using well-known to those skilled in the art
Combustion oxidation reaction occurs for skill gas.
In the present invention, the temperature of the combustion oxidation is preferably 1000~1200 DEG C, and further preferably 1100 DEG C.This
Such as H of the invention during combustion oxidation, in process gas2S、CS2SO is oxidized to sulphur-containing substances such as COS2。
After combustion oxidation, the present invention contains SO for described2Process gas by waste heat recovery unit carry out it is cooling after, obtain
Cooling technique gas enter back into process gas dust removing units and be dusted processing, obtain except dust and gas.Preferably, described to contain SO2's
Process gas is cooled to 570~590 DEG C, further preferably 580~585 DEG C through the heat recovery boiler of waste heat recovery unit；So
The air preheater again through the waste heat recovery unit is cooled to 410~420 DEG C, further preferably 415 DEG C afterwards.Present invention warp
Waste heat recovery unit not only realizes the cooling to process gas, also achieves the recycling to heat.
After the cooling, the present invention is passed through process gas dust removing units to process gas after cooling and is dusted processing, is removed
Dust and gas.The present invention through the dust removal process, preferably obtain 380~400 DEG C except dust and gas.
After dust removal process, the present invention carries out denitration process except dust and gas is passed through the denitration unit for described, obtains denitration gas.
The present invention preferably described will remove dust and gas with air, ammonia after denitration unit mixes, and under the action of denitrating catalyst, removing is removed
NO in dust and gasx.In the present invention, the temperature of the air is preferably 300 DEG C or so；The dosage of the air is with Dilution air
The concentration of ammonia is no more than subject to more than 5% afterwards.
The present invention does not have particular/special requirement to the source of denitrating catalyst, using well-known to those skilled in the art.
The denitration unit of the present invention preferably wet process sulphuric acid plant described in preceding solution carries out denitration process, removes in process gas
NOx, obtain denitration gas.
After denitration process, the denitration gas is passed through level-one SO by the present invention2Oxidation cooling unit carries out oxidation cooling, obtains
Containing SO3Process gas.In the present invention, the cooling mode of the oxidation preferably includes: the denitration gas and air are passed through one
Grade SO2After oxidation reactor mixing, the first SO is flowed through2Layer of oxidation catalyst is in the first SO2It is described under the action of oxidation catalyst
Part SO in denitration gas2It is oxidized to SO3, cooler is cooled to 410~430 DEG C between mixed gas enters first after oxidation；Again
Flow through the 2nd SO2Layer of oxidation catalyst is in the 2nd SO2Under the action of oxidation catalyst, part SO in gas after the cooling2Oxidation
For SO3, second oxidation mixed gas be cooled to 280~300 DEG C.The present invention is to the first SO2Oxidation catalyst and the 2nd SO2Oxygen
The source for changing catalyst does not have particular/special requirement, using SO well-known to those skilled in the art2Oxidation catalyst.The present invention
It is cooled down after oxidation, realizes the recycling for generating heat to oxidation process.
It obtains containing SO3Process gas after, the present invention described will contain SO3Process gas and crystalline silica nuclei at primary acids
Unit mixing is managed, condensation process is carried out, the sulfuric acid and remaining process gas that separation condensation generates.The present invention is to the titanium dioxide silicon wafer
The source of core does not have particular/special requirement, using commercial goods well-known to those skilled in the art.The present invention is in the condensation
In treatment process, to containing SO3Process gas cool down processing, with the crystalline silica nuclei be condensation promotor, make
Obtain the SO in process gas3It is hydrated as H2SO4, and further occurrence condenses under the effect of cooling.In the present invention, described
It cools and is preferably completed by cooling air.The present invention is realized by cooling air to containing SO3Process gas cool
Processing, cooling air are heated up, and the temperature of the remaining process gas after condensation process is cooled to 145~165 DEG C；It is heated
Cooling air can be used as combustion oxidation fuel, denitration process diluent air, oxidation cooling treatment air, oxidation processes
With air, it can be also used for preboiler water supply and mixed in winter with the cooling air of condenser under environment.
The present invention will preferably contain SO3Process gas further cooled down by first-stage condenser 16, process gas temperature drop
To 150~160 DEG C；In cooling procedure, part SO3It is hydrated as H2SO4, acid is in the vertical glass tube of first-stage condenser 16
It is condensed.The acid of concentration is collected in the brick lining acid collector of condenser bottom, realizes sulfuric acid and residue that condensation generates
The separation of process gas.The first control of acid fog device 17 constantly can spray into crystalline silica nuclei to first-stage condenser 16 while cooling, make
It is hydrated H2SO4Preferably condense into the bottom that sulfuric acid flows into first-stage condenser 16 along vertical glass tube.First-stage condenser 16 it is cold
But air is provided by the first cooling blower, and after first-stage condenser 16, cooling air is heated cooling air.
After obtaining remaining process gas, the remaining process gas is passed through second level SO by the present invention2After oxidation unit is aoxidized,
Condensation process is carried out in second level acid processing unit, obtains the sulfuric acid that condensation generates, residual gas is passed through tail gas treating unit progress
Vent gas treatment.In the present invention, the mode of the oxidation includes: by the residual gas and to enter second level SO2Oxidator it
Preceding some processes gas mixing, so that the temperature of residual gas rises to 200 DEG C；Mixed gas is warming up to 370~380 DEG C again
Afterwards, in the 3rd SO2Under the action of oxidation catalyst, so that remaining SO in the gaseous mixture2It is oxidized to SO3。
After completing re-oxidation, obtained gaseous mixture is passed through primary acids processing unit with crystalline silica nuclei and mixed by the present invention
It closes, carries out condensation process, obtain sulfuric acid.The present invention does not have particular/special requirement to the source of the crystalline silica nuclei, using ability
Commercial goods known to field technique personnel.The present invention is during the condensation process, to containing SO3Gaseous mixture carry out
Cool processing, is condensation promotor with the crystalline silica nuclei, so that the SO in gaseous mixture3It is hydrated as H2SO4, and
Further occurrence condenses under the effect of cooling.In the present invention, described cool preferably is completed by cooling air.This
Invention is realized by cooling air to containing SO3Gaseous mixture the processing that cools, cooling air is heated up, in gaseous mixture
SO3It is condensed into sulfuric acid, the temperature of residual gas is cooled to 85~105 DEG C.
The present invention will preferably contain SO3Gaseous mixture further cooled down by secondary condenser 23, in cooling procedure
In, part SO3It is hydrated as H2SO4, the H that is hydrated2SO4It is condensed in the vertical glass tube of secondary condenser 23.Cold
The second control of acid fog device 24 constantly can spray into crystalline silica nuclei to secondary condenser 23 when but, make to be hydrated H2SO4Preferably condensation
The bottom of secondary condenser 23 is flowed into along vertical glass tube at sulfuric acid, clean process gas temperature is reduced to 95 DEG C at this time.It is dense
Contracting acid be collected in the brick lining acid collector of 23 bottom of secondary condenser, cooling air needed for secondary condenser 23 by
Second cooling blower provides, and the air after heating has following 3 purposes: cold with 23 entrance of secondary condenser under environment in winter
But air mixing, adjustment flue gas and preboiler water supply.
After the sulfuric acid that the present invention obtains condensation process twice mixes, as target product sulfuric acid；Specifically, the present invention will
Sulfuric acid is all collected in sulfuric acid storage tank 26 in the bottom of first-stage condenser 16 and secondary condenser 23.
Again after condensation process, residual gas is passed through tail gas treating unit and carries out vent gas treatment by the present invention.In the present invention
In, the vent gas treatment preferably includes the cooling treatment sequentially carried out and demisting processing；Residual gas after the cooling treatment
Temperature be preferably 60 DEG C；The present invention does not have particular/special requirement to the specific embodiment of the cooling treatment, using this field skill
Known to art personnel.The specific embodiment that the present invention handles the demisting does not have particular/special requirement, using this field
Known to technical staff.
After residual gas is preferably cooled to 60 DEG C in clean Gas Cooler by the present invention, enter demister later, herein
Place, acid mist concentration are lowered.The present invention is by the surplus heat after demisting treated residual gas and secondary condenser 23 heat
Chimney is discharged into after air mixing, the discharge temperature of process gas is 80 DEG C.
Below in conjunction with the embodiment in the present invention, the technical solution in the present invention is clearly and completely described.It is aobvious
So, described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Based on the reality in the present invention
Example is applied, every other embodiment obtained by those of ordinary skill in the art without making creative efforts all belongs to
In the scope of protection of the invention.
Embodiment 1
The specific work steps of above-mentioned wet process sulphuric acid plant is as follows:
Step 1: technique combustion unit 1 includes process gas burning boiler and stair oxidation blower 27.Contain in process gas
A large amount of spent acid and sulfuric acid gas, process gas and fuel gas are burnt in process gas burning boiler, stair oxidation blower
27 will spray into process gas burning boiler from the hot-air of first-stage condenser 16 and secondary condenser 23.It burns by process gas
After boiler burnup, spent acid and sulfuric acid gas in process gas are oxidized to SO2Gas contains SO after burning2Process gas temperature rises to
1100℃。
Step 2: technique combustion unit 1 is connected to waste heat recovery unit 2.Waste heat recovery unit 2 includes heat recovery boiler
And air preheater.Heat recovery boiler connects drum 30, and generation of burning contains SO2Process gas it is cold through heat recovery boiler
But to 580 DEG C, heat is the heat source that steam is generated for drum 30.Contain SO after heat recovery boiler is cooled2Technique
Gas is further cooled to 415 DEG C after air preheater.
Step 3: waste heat recovery unit 2 is connected to process gas dust removing units 3.Process gas dust removing units 3 are mainly removed including electrostatic
Dirt device.Process gas dust removing units 3 are electrostatic precipitator, after electrostatic precipitator, by further cold after air preheater
But to 415 DEG C containing SO2Process gas in a large amount of dirt be disposed of.
Step 4: process gas dust removing units 3 are connected to denitration unit 4.Denitration unit 4 includes liquid ammonia evaporator, ammonia/sky mixing
Device, diluent air, ammonia-spraying grid, denitration (SCR) reactor and denitration (SCR) catalyst composition.Since process gas is in step 1
A large amount of NOx is produced when middle burning, therefore the NOx in process gas is removed by denitration unit 4.Process gas is passed through
Temperature is down to 395 DEG C after electrostatic precipitator.Diluent air and process liquid ammonia evaporator by air preheater heating evaporate
Ammonia be sufficiently mixed in ammonia/sky mixer after ammonia sky gaseous mixture denitration (SCR) reactor is entered by ammonia-spraying grid, with
Process gas comes into full contact with, and after denitration (SCR) reactor equipped with denitration (SCR) catalyst, completes the removing of NOx.
Step 5: denitration unit 4 is connected to level-one SO2Aoxidize cooling unit 5.Level-one SO2Aoxidizing cooling unit 5 includes level-one
SO2Oxidation reactor 10, two layers of SO2Cooler and secondary process hot-air heater 14 between oxidation catalyst, bed.The process gas of denitration
Into SO2It is mixed before oxidation reactor with the air after air preheater preheats, process gas is diluted.Then dilute
Process gas after releasing passes through the first SO2Layer of oxidation catalyst 11, the part SO after the catalysis of catalyst in process gas2Conversion
For SO3A large amount of reaction heat are discharged simultaneously, process gas temperature rises to 540 DEG C, and after cooler 12 between first, temperature is reduced to
420℃.Then, process gas enters the 2nd SO2Layer of oxidation catalyst 13, and have part SO2It is converted into SO3It discharges simultaneously a large amount of anti-
Heat is answered, process gas temperature rises to 440 DEG C.After secondary process hot-air heater 14, temperature is reduced to 390 DEG C, then by the
Process gas is set to be cooled to 290 DEG C after cooler 15 between two.A large amount of reaction heat of catalysis reaction release pass through cooling between first
Device 12 recycles heat, generates steam for drum 30 and provides part of heat energy.
Step 6: level-one SO2It aoxidizes cooling unit 5 and is connected to primary acids processing unit 6.Primary acids processing unit 6 includes one
Grade condenser 16, the first control of acid fog device 17, the first cooling blower and feedwater preheater.By level-one SO2Oxidation reaction
A large amount of SO in process gas after the oxidation of device 102It is converted into SO3, carried out by process gas after cooling by first-stage condenser 16
Further cooling, process gas temperature is down to 155 DEG C.In cooling procedure, part SO3It is hydrated as H2SO4, acid is in level-one condensation
It is condensed in the vertical glass tube of device 16.The acid of concentration is collected in the brick lining acid collector of condenser bottom.In cooling
When the first control of acid fog device 17 can constantly to first-stage condenser 16 spray into crystalline silica nuclei, make be hydrated H2SO4Preferably condense into
Sulfuric acid flows into the bottom of first-stage condenser 16 along vertical glass tube.The cooling air of first-stage condenser 16 is by the first cooling blower
It provides, after first-stage condenser 16, cooling air is heated cooling air, and the air after heating has following 5 purposes: burning
Boiler auxiliary combustion air, denitration (SCR) enter level-one SO with diluent air, process gas2It is diluent air before oxidation reactor 10, pre-
It is mixed under heat boiler water supply and in winter environment with the cooling air of first-stage condenser 16.
Step 7: primary acids processing unit 6 is connected to second level SO2Oxidation unit 7.Second level SO2Oxidation unit 7 includes process gas
Mixer 19, level-one technique hot-air heater 20, auxiliary burner 28, secondary process gas oxidation fan 29, control of acid fog device, second level
SO2Oxidator and setting are in second level SO2The 3rd SO in oxidator2Layer of oxidation catalyst 22.Work after first-stage condenser 16
Skill gas and entrance second level SO2Oxidator before some processes gas mixed in process gas mixer 19, technique temperature
Degree rises to 200 DEG C, then rises to 370 DEG C through process gas temperature after level-one technique hot-air heater 20.Subsequent process gas enters two
Grade SO2Oxidator carry out oxidation further, make in level-one SO2Oxidator in do not have conversion SO2Further it is oxidized to
SO3.Auxiliary burner 28 enters second level SO in process gas2The temperature of oxidator do not reach 370 DEG C and make to open, usually open
It is opened when vehicle.
Step 8: second level SO2Oxidation unit 7 is connected to second level acid processing unit 8.Second level acid processing unit 8 includes that second level is cold
Condenser 23, the second control of acid fog device 24, the second cooling blower and sulfuric acid storage tank 26.It is cold by second level by process gas after cooling
Condenser 23 is further cooled down, in cooling procedure, part SO3It is hydrated as H2SO4, acid is in the vertical of secondary condenser 23
It is condensed in glass tube.The second control of acid fog device 24 constantly can spray into crystalline silica nuclei to secondary condenser 23 while cooling,
Make to be hydrated H2SO4Preferably condense into the bottom that sulfuric acid flows into secondary condenser 23 along vertical glass tube.Clean technique at this time
Temperature degree is reduced to 95 DEG C.The acid of concentration is collected in the brick lining acid collector of 23 bottom of secondary condenser, B-grade condensation
Cooling air needed for device 23 is provided by the second cooling blower, and the air after heating has following 3 purposes: in winter under environment with
Cooling air mixing, adjustment flue gas and the preboiler water supply of 23 entrance of secondary condenser.First-stage condenser 16 and second level are cold
Sulfuric acid is all collected in sulfuric acid storage tank 26 in the bottom of condenser 23.
Step 9: second level acid processing unit 8 is connected to tail gas treating unit 9.Tail gas treating unit 9 is gas-cooled including cleaning technology
But device and demister.After cleaning technology gas is cooled to 60 DEG C in clean Gas Cooler, enter demister later, here, acid
Mistiness degree is lowered.Chimney, process gas are discharged into after superfluous hot-air mixing after cleaning technology gas and the heating of secondary condenser 23
Discharge temperature be 80 DEG C.
Embodiment 2
Process gas is handled in the way of embodiment 1, prepares sulfuric acid；The sulfuric acid concentration being prepared reaches
98%, meet commerical grade sulfuric acid standard, it can direct marketing.
Pass through SO2Detector detects the tail gas of discharge, SO in tail gas after treatment2It is up to standard.
Embodiment 3
To containing SO in the way of embodiment 12It is handled with the substance of the spent acid of the element containing S, prepares sulfuric acid；Preparation
Obtained sulfuric acid concentration reaches 98%, meets commerical grade sulfuric acid standard, can direct marketing.
Pass through SO2Detector detects the tail gas of discharge, can obtain, SO in tail gas after treatment2It is up to standard.
Embodiment 4
To containing SO in the way of embodiment 12It is handled with the substance of the spent acid containing S, is also contained in handled substance
Ammonia prepares sulfuric acid；The sulfuric acid concentration being prepared reaches 98%, meets commerical grade sulfuric acid standard, can direct marketing.
Pass through SO2Detector detects the tail gas of discharge, SO in tail gas after treatment2It is up to standard.
Embodiment 5
To containing SO in the way of embodiment 12It is handled with the substance of spent acid, also contains alkene in handled substance
Hydrocarbon prepares sulfuric acid；The sulfuric acid concentration being prepared reaches 98%, meets commerical grade sulfuric acid standard, can direct marketing.
Pass through SO2Detector detects the tail gas of discharge, SO in tail gas after treatment2It is up to standard.
Above embodiments the result shows that, the present invention adapt to wide scope of material, sour gas, Waste Sulfuric Acid can be handled simultaneously
Deng most sulphur-containing exhaust gas and spent acid, sour gas allows NH without dehydration in raw material3With the presence of hydro carbons；Operate bullet
Property range is big；Sulphur high conversion rate, tail gas can directly meet discharge standard；Do not need to consume in sweetening process any chemicals or its
Its additive, also without spent acid and other waste liquid outlets, environmental protection pressure is small；And process unit recycles a large amount of mesohigh simultaneously
Steam, low energy consumption, and heat recovery efficiency is high, and cooling-water consumption is low, and operating cost also accordingly substantially reduces.
It is also possible to realize the desulfurization and denitrification integral of refinery processes gas in conjunction with SCR denitration process.
Specific examples are applied in the present invention, and principle and implementation of the present invention are described, above embodiments
Illustrate to be merely used to help understand method and its core concept of the invention；At the same time, for those skilled in the art, according to
According to thought of the invention, there will be changes in the specific implementation manner and application range.In conclusion the content of the present specification
It should not be construed as limiting the invention.
Claims (10)
1. a kind of wet process sulphuric acid plant, which is characterized in that including being sequentially connected logical technique combustion unit (1), waste heat recycling
Unit (2), process gas dust removing units (3), denitration unit (4), level-one SO2Aoxidize cooling unit (5), primary acids processing unit
(6), second level SO2Oxidation unit (7), second level acid processing unit (8) and tail gas treating unit (9)；The level-one SO2Oxidation cooling
Unit includes level-one SO2Oxidation reactor (10) and from top to bottom it is successively set on the level-one SO2In oxidation reactor
One SO2Cooler (12), the 2nd SO between layer of oxidation catalyst (11), first2Layer of oxidation catalyst (13), secondary process gas add
Cooler (15) between hot device (14) and second, the level-one SO2The air inlet of oxidation reactor (10) and the out of stock unit
(4) gas outlet is connected, the primary acids processing unit (6) include first-stage condenser (16) and with the first-stage condenser
The first control of acid fog device (17) being connected and the first cooling blower, the level-one SO2The gas outlet of oxidation reactor (10) with
The air inlet of the first-stage condenser (16) is connected, the second level SO2Oxidation unit (7) include process gas mixer (19),
Level-one technique hot-air heater (20) and second level SO2Oxidation reactor (21), the air inlet difference of the process gas mixer (19)
Gas outlet and the second level SO with the first-stage condenser (16)2The air inlet pipeline of oxidation reactor (21) is connected, described
The air inlet of level-one technique hot-air heater (20) respectively with the process gas mixer (19) and the second level SO2Oxidation reactor
(21) gas outlet is connected, the gas outlet of the level-one technique hot-air heater (20) and the second level SO2Oxidation reactor
(21) air inlet is connected, the gas outlet of the level-one technique hot-air heater (20) and the second level SO2Oxidation reactor
(21) cooler between the pipeline between air inlet passes through described second, the second level SO2Is provided in oxidation reactor
Three SO2Layer of oxidation catalyst (22), the second level acid processing unit include secondary condenser (23), the second control of acid fog device
(24), the second cooling blower and sulfuric acid storage tank (26), the gas outlet of the level-one technique hot-air heater (20) also with the second level
The air inlet of condenser (23) is connected, the secondary condenser (23) respectively with the second control of acid fog device (24) and described
Second cooling blower is connected, the first-stage condenser (16) and the secondary condenser (23) with the sulfuric acid storage tank (26)
It is connected, the gas outlet of the secondary condenser (23) is connected with the tail gas treating unit (9).
2. wet process sulphuric acid plant according to claim 1, which is characterized in that the technique combustion unit (1) includes work
Skill gas burning boiler, the waste heat recovery unit (2) include heat recovery boiler and air preheater, the process gas dedusting list
First (3) include electrostatic precipitator, and the denitration unit (4) includes liquid ammonia evaporator, ammonia/sky mixer, diluent air, spray ammonia lattice
Grid, Benitration reactor and denitrating catalyst, the tail gas treating unit (9) includes cleaning technology Gas Cooler and demister.
3. wet process sulphuric acid plant according to claim 2, which is characterized in that the technique combustion unit (1) further includes
One end of stair oxidation blower (27), the stair oxidation blower (27) is connected with the process gas burning boiler, and described one
The other end gas outlet phase with the first-stage condenser (16) and the secondary condenser (23) respectively of grade oxidation fan (27)
Connection.
4. wet process sulphuric acid plant according to claim 3, which is characterized in that the level-one technique hot-air heater (20) goes out
Port and the second level SO2It is provided on pipeline between the air inlet of oxidation reactor (21) auxiliary burner (28), it is described
Auxiliary burner (28) is close to the second level SO2Oxidation reactor (21).
5. wet process sulphuric acid plant according to claim 4, which is characterized in that the process gas mixer (19) and described one
Secondary process gas oxidation fan (29) is provided between grade technique hot-air heater (20)；
The air preheater is connected with the burning boiler；
The gas outlet of the first-stage condenser (16) is connected with the air inlet of the secondary condenser (23).
6. wet process sulphuric acid plant according to claim 5, which is characterized in that further include a drum (30), the drum
(30) cooler (12), the secondary process hot-air heater (14) and the heat recovery boiler phase between described first respectively
Connection.
7. a kind of method for carrying out wet desulphurization using any one of claim 1~6 described device, comprising the following steps:
(1) process gas and fuel are passed through the technique combustion unit and carry out combustion oxidation, obtained containing SO2Process gas；Institute
It states process gas and contains sour gas and acid solution, H in the sour gas2The volume content of S is 3~60%；
(2) contain SO for what the step (1) obtained2Process gas by waste heat recovery unit carry out it is cooling after, obtained cooling
Process gas enters back into process gas dust removing units and is dusted processing, obtains except dust and gas；
(3) denitration process is carried out except dust and gas is passed through the denitration unit by what the step (2) obtained, obtains denitration gas；
(4) the denitration gas that the step (3) obtains is passed through level-one SO2Oxidation cooling unit carries out oxidation cooling, obtains containing SO3
Process gas；
(5) step (4) is obtained containing SO3Process gas be passed through primary acids processing unit with crystalline silica nuclei and mix, carry out
Condensation process, the sulfuric acid and remaining process gas that separation condensation generates；
(6) the remaining process gas that the step (5) obtains is passed through second level SO2After oxidation unit is aoxidized, oxidation product is led to
Enter to second level acid processing unit carry out condensation process, obtain condensation generate sulfuric acid, residual gas be passed through tail gas treating unit into
End of line gas disposal.
8. the method according to the description of claim 7 is characterized in that in the step (1) combustion oxidation temperature be 1000~
1200℃。
9. the method according to the description of claim 7 is characterized in that the cooling mode of oxidation in the step (4) include: by
The denitration gas and air are passed through level-one SO2After oxidation reactor mixing, the first SO is flowed through2Layer of oxidation catalyst is in the first SO2Oxygen
Under the action of changing catalyst, part SO in the denitration gas2It is oxidized to SO3, it is cooling between mixed gas enters first after oxidation
Device is cooled to 410~430 DEG C；Pass through the 2nd SO2Layer of oxidation catalyst is in the 2nd SO2It is described cold under the action of oxidation catalyst
But part SO in gas after2It is oxidized to SO3, second oxidation mixed gas sequentially enter secondary process hot-air heater and second
Between cooler be cooled to 280~300 DEG C.
10. the method according to the description of claim 7 is characterized in that the temperature of the remaining process gas in the step (5) is
145~165 DEG C；
The temperature of residual gas is 85~105 DEG C in the step (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810934729.4A CN108975285A (en) | 2018-08-16 | 2018-08-16 | A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810934729.4A CN108975285A (en) | 2018-08-16 | 2018-08-16 | A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108975285A true CN108975285A (en) | 2018-12-11 |
Family
ID=64552911
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810934729.4A Pending CN108975285A (en) | 2018-08-16 | 2018-08-16 | A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108975285A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110282606A (en) * | 2019-07-05 | 2019-09-27 | 科洋环境工程（上海）有限公司 | The wet processing system and technique of aqueous sulphur cream and desulfurization waste liquor |
| CN111841310A (en) * | 2020-07-02 | 2020-10-30 | 宁波科新化工工程技术有限公司大连分公司 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
| CN112569735A (en) * | 2020-11-27 | 2021-03-30 | 株洲宏大高分子材料有限公司 | Method and device for removing sulfuric acid smoke in tail gas pipeline of flue gas acid making system |
| CN117326533A (en) * | 2023-06-15 | 2024-01-02 | 广东宏瑞能源科技股份有限公司 | Method for preparing reagent-grade sulfuric acid by wet acid preparation process and system for producing multi-concentration high-grade sulfuric acid |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3490868A (en) * | 1964-11-06 | 1970-01-20 | Zieren Chemiebau Gmbh Dr A | Method of recovery of sulphuric acid |
| CN1070839A (en) * | 1991-08-16 | 1993-04-14 | 奈密克·安斯托尔特 | The method of the loaded waste gas that the clean oil combustion apparatus is discharged |
| JPH05139708A (en) * | 1991-05-24 | 1993-06-08 | Haldor Topsoee As | Method for regenerating used sulfuric acid |
| CN101746737A (en) * | 2008-12-11 | 2010-06-23 | 上海宝钢化工有限公司 | Preparation method and device of sulfuric acid |
| CN102092688A (en) * | 2011-02-12 | 2011-06-15 | 李金山 | Technological process for producing acid with sulfur-containing gas |
| CN102698596A (en) * | 2012-05-31 | 2012-10-03 | 杨秋良 | Method for preparing sulfuric acid by catalytically oxidizing low-concentration sulfur dioxide in baking flue gas |
| CN208980334U (en) * | 2018-08-16 | 2019-06-14 | 北京美斯顿科技开发有限公司 | A kind of wet process sulphuric acid plant |
-
2018
- 2018-08-16 CN CN201810934729.4A patent/CN108975285A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3490868A (en) * | 1964-11-06 | 1970-01-20 | Zieren Chemiebau Gmbh Dr A | Method of recovery of sulphuric acid |
| JPH05139708A (en) * | 1991-05-24 | 1993-06-08 | Haldor Topsoee As | Method for regenerating used sulfuric acid |
| CN1070839A (en) * | 1991-08-16 | 1993-04-14 | 奈密克·安斯托尔特 | The method of the loaded waste gas that the clean oil combustion apparatus is discharged |
| CN101746737A (en) * | 2008-12-11 | 2010-06-23 | 上海宝钢化工有限公司 | Preparation method and device of sulfuric acid |
| CN102092688A (en) * | 2011-02-12 | 2011-06-15 | 李金山 | Technological process for producing acid with sulfur-containing gas |
| CN102698596A (en) * | 2012-05-31 | 2012-10-03 | 杨秋良 | Method for preparing sulfuric acid by catalytically oxidizing low-concentration sulfur dioxide in baking flue gas |
| CN208980334U (en) * | 2018-08-16 | 2019-06-14 | 北京美斯顿科技开发有限公司 | A kind of wet process sulphuric acid plant |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110282606A (en) * | 2019-07-05 | 2019-09-27 | 科洋环境工程（上海）有限公司 | The wet processing system and technique of aqueous sulphur cream and desulfurization waste liquor |
| CN111841310A (en) * | 2020-07-02 | 2020-10-30 | 宁波科新化工工程技术有限公司大连分公司 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
| CN112569735A (en) * | 2020-11-27 | 2021-03-30 | 株洲宏大高分子材料有限公司 | Method and device for removing sulfuric acid smoke in tail gas pipeline of flue gas acid making system |
| CN117326533A (en) * | 2023-06-15 | 2024-01-02 | 广东宏瑞能源科技股份有限公司 | Method for preparing reagent-grade sulfuric acid by wet acid preparation process and system for producing multi-concentration high-grade sulfuric acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108975285A (en) | A kind of wet process sulphuric acid plant and a kind of method of wet desulphurization | |
| CN103303872B (en) | System device and method for recycling sulfur dioxide from fume to prepare sulfur | |
| US8877152B2 (en) | Oxidation system and method for cleaning waste combustion flue gas | |
| CN107954403B (en) | Resource-saving waste acid treatment process and device | |
| EP1950176A2 (en) | Process for removing contaminants from gas streams | |
| CN203781842U (en) | New sulfur recovery device | |
| CN103072957A (en) | Technology for preparing sulfuric acid | |
| CN206680184U (en) | A kind of system that high-concentration sulfuric acid is continuously and stably produced using sour gas | |
| CN205527748U (en) | Sour regenerating unit of sulfur waste | |
| CN101301567B (en) | Process for removing contaminants from gas streams | |
| CN205653162U (en) | System for sulphuric acid is prepared to sulphur waste liquid that contains that utilizes coal gas wet oxidation process to produce | |
| CN109052335A (en) | A kind of method of sulfur gas reduction Waste Sulfuric Acid sulfur dioxide liquid and sulfuric acid | |
| CN106955571A (en) | A kind of industrial smoke ozone step-by-step oxidation absorbs the device and method of simultaneous SO_2 and NO removal | |
| CN106621768A (en) | Ammonia process of desulfurization integral purification device and method for acid gas sulfur recovery tail gas | |
| CN101254392A (en) | Energy-saving type sodium sulphite circulation desulfurizing device and method | |
| CN207016486U (en) | A kind of system that sulfuric acid is produced using sour gas | |
| CN104229755A (en) | Method for preparing sulfuric acid from sulfur | |
| CN102512910B (en) | Smoke heat exchange process for recycling evaporated water of gas desulfurization system | |
| CN102530882A (en) | Method and device for reclaiming dehydrated sulfur | |
| CN208292665U (en) | A kind of resource-conserving Waste acid treating device | |
| CN110332552A (en) | The organic liquid waste recycling treatment system and its method of the sulphur containing chlorine | |
| CN213569540U (en) | Desulfurization waste liquid system acid system | |
| CN108654363A (en) | Couple waste heat of coke-oven flue gas and amounts of sulphur contaminants acid-making process | |
| CN211274164U (en) | Ammonia-containing tail gas treatment device for dry ammonium workshop section in alkali industry | |
| CN103611417B (en) | A kind of coke oven exhaust gas wet denitration method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20181211 |