CN203668003U - Half-dry sulfuric acid making device - Google Patents
Half-dry sulfuric acid making device Download PDFInfo
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- CN203668003U CN203668003U CN201320812895.XU CN201320812895U CN203668003U CN 203668003 U CN203668003 U CN 203668003U CN 201320812895 U CN201320812895 U CN 201320812895U CN 203668003 U CN203668003 U CN 203668003U
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- acid
- gas
- absorption tower
- hygroscopic
- moisture absorption
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 239000002253 acid Substances 0.000 claims abstract description 178
- 238000010521 absorption reaction Methods 0.000 claims abstract description 118
- 239000007789 gas Substances 0.000 claims abstract description 114
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000001035 drying Methods 0.000 claims abstract description 27
- 239000002918 waste heat Substances 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 29
- 238000006243 chemical reaction Methods 0.000 abstract description 22
- 239000006227 byproduct Substances 0.000 abstract description 14
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 10
- 229910052717 sulfur Inorganic materials 0.000 abstract description 6
- 239000011593 sulfur Substances 0.000 abstract description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 2
- 230000007797 corrosion Effects 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 29
- 239000005864 Sulphur Substances 0.000 description 22
- 229910052739 hydrogen Inorganic materials 0.000 description 16
- 238000001816 cooling Methods 0.000 description 14
- 239000001257 hydrogen Substances 0.000 description 13
- 239000000047 product Substances 0.000 description 9
- 150000002431 hydrogen Chemical class 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 235000011149 sulphuric acid Nutrition 0.000 description 7
- 239000001117 sulphuric acid Substances 0.000 description 7
- 230000001131 transforming effect Effects 0.000 description 7
- 238000005192 partition Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000003595 mist Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000003203 everyday effect Effects 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 230000000977 initiatory effect Effects 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 230000005494 condensation Effects 0.000 description 2
- 238000012937 correction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 201000004792 malaria Diseases 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006253 efflorescence Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000004093 laser heating Methods 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 206010037844 rash Diseases 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005987 sulfurization reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- 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
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- Drying Of Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model comprises a half-dry sulfuric acid making device, and relates to a sulfuric acid production device for generating SO2 and water after burning raw materials as acid gas containing hydrogen sulfide and sulfide. The half-dry sulfuric acid making device comprises a drying tower and a moisture absorbing tower, and further comprises a burning system, a converting system, a water-steam system, an absorbing system, a moisture absorption acid circulating system and a dry absorption acid circulating system. The drying tower for drying combustion-supporting gas is connected with the burning furnace; a waste heat boiler is behind the burning furnace, and is connected with a converter; the converter is connected with an overheat/cold-heat heat exchanger; the overheat/cold-heat heat exchanger is connected with the moisture absorbing tower; the moisture absorbing tower is connected with a first absorbing tower; an acid outlet of the moisture absorbing tower is connected with a moisture absorption acid circulating tank; a moisture absorption acid circulating pump in the tank is connected with a moisture absorption acid cooler; the moisture absorption acid cooler is connected with an acid separator in the moisture absorbing tower. Two-conversion and two-absorption can be realized for feed gas containing sulfur above 6%; the SO2 concentration of tail gas of the feed gas is below 100 ppm; one conversion and one absorption of autothermal balance can be realized for the feed gas even containing sulfur of 3%. The half-dry sulfuric acid making device has such characteristics as low corrosion, much byproduct steam, good tail gas discharge, low power consumption and low maintenance load.
Description
Technical field:
The utility model relates to the technology category of sulfuric acid production plant in Chemical Manufacture, especially with raw material sulfide hydrogen and vulcanize organic sour gas produce SO after burning
2time produce the sulphuric acid plant of water.
Background technology:
With fuel such as crude oil, coal and Sweet natural gases, association produces sulfide hydrogen and vulcanizes organic sour gas sulphur in sweetening process, and this sour gas can be used as the raw material of manufacturing sulfuric acid.When producing sulfurous gas after hydrogen sulfide and sulfuration organism burn, also produce water.At present, mainly contain two kinds taking this gas as the technique of raw material production sulfuric acid: dry method relieving haperacidity and wet method relieving haperacidity.
Dry method sulphuric acid plant is that sour gas is burned into SO
2, through waste heat boiler cool, work of water sprinkling for better material moisture is cooling to reduce after the moisture in gas again, wet SO
2gas enters the dry moisture, dried SO removed of drying tower
2gas is sent into and is transformed and absorption system by main blower.First, then the cold air that goes out main blower enters convertor and carries out SO more than need being heated to the combustion initiation temperature of catalyzer
2conversion, SO
2conversion is the reversible reaction of heat release, needs to remove reaction heat in conversion process, so convertor is the adiabatic reactor of multistage, and the intersegmental cooling heat of moving.The SO that reaction generates
3gas produces sulfuric acid product under being absorbed by the vitriol oil in absorption tower.Due to SO
2the reversibility of conversion reaction, improve SO
2transformation efficiency, increase intermediate absorption be both economical method, technique that Here it is so-called " double conversion and double absorption ", after transforming for the first time, (common 2 to 3 sections of beds) are cooling, enter the first absorption tower and sponge the SO having generated
3after, be heated to beds inlet temperature and enter convertor and carry out SO
2conversion for the second time, then after cooling, enter second absorption tower and sponge newly-generated SO
3.Compared with there is no " turns a suction " of intermediate absorption, the SO of double conversion and double absorption
2the dense height of gas, narrow-minded, total conversion rate is high, tail sequences, remarkable in economical benefits, become the leading technique of sulfuric acid apparatus.
The principal advantage of dry method relieving haperacidity is that corrodibility is little.Because dried SO
2in gas, almost there is no moisture, the dew-point temperature of the gas after conversion is low, the sour dense height of dew point, corrodibility are just little.The shortcoming of dry method relieving haperacidity is dried SO
2gas temperature is low, heating up needs heat, has SO
2the autothermal equilibrium point of gas concentration, gas is dense lower than after autothermal equilibrium point, just needs outside concurrent heating.The humidification process of cooling of dry method relieving haperacidity has not only lengthened operational path, and makes the SO generating in incinerator
3become dilute sulphuric acid.
Wet method acid-making process is that sour gas is burned into SO
2, cool and directly enter convertor to beds inlet temperature through waste heat boiler, through the SO transforming
3gas is condensed into sulfuric acid in condensing tower.So just shorten operational path, it has not had " malaria " of dry method relieving haperacidity---after wet hot gas humidification is cooling, dry, reheat intensification, but its gas all wets in whole process, and due to high humidity, gas dew point temperature after conversion is high, dew point sour dense low, corrodibility is just large.
The shortcoming of wet method relieving haperacidity is that corrodibility is large and acid mist is many.Due to the washiness in gas, can only adopt the mode of condensation by the SO in gas
3condensation is got off with water section, is to carry out condensed gas with Glass tubing in condensing tower, and this has hindered the reliability of condensing tower, has also reduced the scale of wet method sulphuric acid plant.In condensing tower exit gas, moisture content is far above SO
3content, the dew point acid of gas is dense low, there is no to reheat the economy transforming for the second time, and wet method relieving haperacidity can only be also once to transform.Although wet method relieving haperacidity reduces the dense SO reducing in tail gas of gas by increasing tolerance
2concentration, but be once to transform after all, the SO in condensing tower exit gas
2content is still very high.Condensing tower condensation is exactly to allow acid mist condense into the process of drop, in exhaust gas body, still contain a large amount of small-particle acid mists, common fiber mist eliminator is difficult to remove, and need to remove with electrostatic precipitator, or in exhaust gas body, add warm air to evaporate acid mist and the object that reaches " can't see ".
Summary of the invention:
The purpose of this utility model is to solve that the corrodibility of the hydrogeneous raw material wet method relieving haperacidity such as hydrogen sulfide is large and acid mist is many, the problem such as " malaria " of dry method relieving haperacidity.The advantage sum of collection dry method relieving haperacidity and wet method acid-making process, reaches the object that corrodibility is little, waste heat recovery is many, exhaust emissions is few.
Sulfuric acid is the material that has azeotropic point, and is maximum boiling point, and azeotropic point temperature is dense in 98.3% left and right at 330 DEG C, the acid of azeotropic point.
Water sulphur is than representing H in gas
2o and SO
3mol ratio, be 1.092 with the dense 98.3% corresponding gas phase water sulphur ratio of azeotropic point acid.When water sulphur than be greater than 1.092 gas dewfall time, the acid of its dew point is dense is less than 98.3%; And when water sulphur than be less than 1.092 gas dewfall time, the acid of its dew point is dense is just greater than 98.3%.
With hydrogen sulphur than the mol ratio that represents hydrogen atom and sulphur atom in gas, as dry H
2s gas, its hydrogen sulphur ratio is 2.0.If burn this H with dry air
2s gas, the H of the flue gas obtaining
2o and SO
2mol ratio approach 1.0.Work as SO
2transformation efficiency exceed 91.5% after, the water sulphur of gas is greater than 1.092 than just, the acid of dew point is at this moment dense has just crossed azeotropic point and has significantly improved.
The technical scheme that the utility model adopts is:
Half-dried legal system sulfuric acid apparatus, comprise drying tower, moisture absorption tower, gas system also comprises incineration system---air filter, main blower, incinerator, conversion system---convertor, one or more gas heat exchanger, boiler circuit---waste heat boiler, one or more vapor superheater, one or more oiler feed economizer, absorption system---the first absorption tower and second absorption tower etc.; Acid system comprises the hygroscopic acid recycle system---hygroscopic acid water cooler, hygroscopic acid recycle pump, hygroscopic acid circulation groove, and the dry acid circulation system of inhaling---do the sour circulation groove of suction, dry acid circulating pump, dry acid cooler, absorb acid circulating pump, absorption acid cooler etc.
Its principal character is: the drying tower (3) of dry combustion-supporting gas is connected with sour gas incinerator (4), and incinerator is connected with waste heat boiler (5), and waste heat boiler is connected with convertor (6); The gas transforming for the first time through convertor is connected with overheated/hot and cold heat exchanger (14) with pipeline, and overheated/hot and cold heat exchanger is connected with moisture absorption tower (7), and moisture absorption tower is connected with the first absorption tower (8); The outlet of moisture absorption tower acid is connected with hygroscopic acid circulation groove (27), hygroscopic acid recycle pump (28) has been installed in hygroscopic acid circulation groove, hygroscopic acid circulating-pump outlet is connected with hygroscopic acid water cooler (26), and hygroscopic acid water cooler is connected with the acid trap in moisture absorption tower.
Allow combustion air into incinerator at drying tower inner drying, remove after airborne all or part of moisture, entering incinerator burns sulfide hydrogen and vulcanizes organic sour gas, hydrogen sulphur ratio in incinerator is controlled between 1.3 to 2.1, cool to after more than the combustion initiation temperature of catalyzer through waste heat boiler, directly enter convertor and transform for the first time, transform for the first time and conventionally adopt 1 to 3 section of beds, through transforming for the first time the SO of generation
3in moisture absorption tower, be absorbed into sulfuric acid with the moisture major part in gas.Moisture absorption tower exit gas enters the first absorption tower again and sponges remaining SO
3and moisture.
The first absorption tower exit gas can also reheat to after more than the combustion initiation temperature of catalyzer with the heat of conversion system, enters convertor and transforms for the second time, through transforming for the second time the SO of generation
3gas is absorbed into sulfuric acid in second absorption tower, and second absorption tower outlet tail gas directly discharges atmosphere.
Complete most of H in gas phase with moisture absorption tower
2o and SO
3absorption, the water sulphur of moisture absorption tower inlet gas is than between 0.88 to 1.08, by the hydrogen sulphur in incinerator when for the first time the factor such as transformation efficiency determine.Moisture absorption tower recycle acid concentration is exactly the H absorbing
2o and SO
3the concentration of one-tenth acid, by enter in moisture absorption tower gas water sulphur when the factor such as recycle acid temperature determine, do not add water or go here and there acid to the hygroscopic acid recycle system.
For guaranteeing the H in gas phase
2o and SO
3be to absorb into acid instead of be condensed into acid, key depends on into moisture absorption tower temperature and the coupling of entering tower acid temperature.Entering tower temperature can not be lower than dew-point temperature, and entering tower acid temperature can not be too low, otherwise can generate a large amount of acid mists in tower.Moisture absorption tower recycle acid temperature, between 100 DEG C to 250 DEG C, is determined by the heat-eliminating medium of hygroscopic acid water cooler.If enter tower acid temperature control 185 DEG C of left and right, this recycle acid water cooler can be produced the saturation steam that vapor pressure is 0.5MPa left and right, now SO
3total absorptivity more than 90%.
The premiere feature of moisture absorption tower is to absorb steam in gas phase, in the specific absorption of Ta Zhongshui also more than 90%.Then the gas that goes out moisture absorption tower enter the first absorption tower, just can further absorb with the acid temperature acid on traditional absorption tower is dense.
The object that drying tower is set is to regulate the hydrogen sulphur ratio in incinerator, is regulated by drying tower drying efficiency (normally using drying tower gas bypassing) and sulphur burning amount.The predrying device of air can be set before drying tower, remove airborne part moisture with siccative, to regulate product acid concentration.
In addition, had drying tower, system oneself has just had dry air, in the time of device emergency shutdown or orderly shutdown, can carry out with this dry air hot blow and the cold blowing of gas system, sweep the steam existing in most system, thereby avoid equipment corrosion and catalyzer efflorescence.
The advantage of semidrying relieving haperacidity is: corrodibility is little, byproduct steam is many, tail sequences, power consumption is low, maintenance is few.The outlet of the 2nd section of convertor and after, dew point acid is dense just more than 99.0%, its corrodibility is greatly reduction just.To hydrogen sulfide content, at 42% unstripped gas, the steam productive rate of acid per ton is 2.68 tons, wherein 4.4MPa, 0.66 ton of the low-pressure saturated steam of 2.02 tons of middle pressure superheated vapours, 0.5MPa of 435 DEG C.The unstripped gas more than 6% for hydrogen sulfide and sulfurous organic compound total sulfur content, can realize double conversion and double absorption, the SO of its tail gas
2concentration is below 100ppm; Even if 3%, also can realizing one of autothermal equilibrium, total sulfur content turns a suction.Semidrying relieving haperacidity does not need cooling air, there is no cooling blower, the SO of semidrying relieving haperacidity
2the air quantity of the dense height of gas, main blower is little, power consumption is just low, 1/4th of the not enough wet method relieving haperacidity of the sour power consumption of ton of semidrying relieving haperacidity.
Below in conjunction with accompanying drawing, the utility model is elaborated.
Brief description of the drawings:
Fig. 1, the gas system structural representation of embodiment 1;
Fig. 2, the acid system structural representation of embodiment 1;
Fig. 3, the gas system structural representation of embodiment 2;
Fig. 4, the gas system structural representation of embodiment 3.
In each accompanying drawing: 1 air filter, 2 gas blowers, 3 drying towers, 4 incinerators, 5 waste heat boilers, 6 convertors, 7 moisture absorption towers, 8 first absorption towers, 9 second absorption towers, 10 chimneys; 11 high temperature superheaters, 12 overheated/economizer, 13 hot heat exchangers, 14 overheated/hot and cold heat exchanger; 21 dry acid coolers, 22 dry acid circulating pumps, the sour circulation groove of 23 dry suction, 24 absorb acid cooling, 25 absorb acid circulating pumps, 26 hygroscopic acid water coolers, 27 hygroscopic acid circulation grooves, 28 hygroscopic acid recycle pumps; 31 air preheater C, 32 air preheater B, 33 air preheater A, 34 overheated/economizer, 35 absorption towers; The predrying device of 41 air, 42 vapor superheaters, 43 air preheater E, 44 air preheater D, 45 economizers, 46 gas heat exchangers.
Embodiment:
Below in conjunction with embodiment, the utility model is described further.
Embodiment 1
A kind of raw material is the semidrying sulphuric acid plant of hydrogen sulfide containing sour gas, gas system structure, as Fig. 1, comprises air filter, gas blower, drying tower, incinerator, waste heat boiler, convertor, high temperature superheater, hot heat exchanger, overheated/hot and cold heat exchanger, moisture absorption tower, the first absorption tower, overheated/economizer, second absorption tower, chimney.Acid system structure, as Fig. 2, comprises hygroscopic acid water cooler, hygroscopic acid recycle pump, hygroscopic acid circulation groove, the sour circulation groove of dry suction, dry acid circulating pump, dry acid cooler, absorbs acid circulating pump, absorbs acid cooler.
Its principal character is: drying tower (3) is connected with incinerator (4), and incinerator is connected with waste heat boiler (5), and waste heat boiler is connected with convertor (6); The gas transforming for the first time through convertor is connected with overheated/hot and cold heat exchanger (14) with pipeline, and overheated/hot and cold heat exchanger is connected with moisture absorption tower (7), and moisture absorption tower is connected with the first absorption tower (8); The outlet of moisture absorption tower acid is connected with hygroscopic acid circulation groove (27), hygroscopic acid recycle pump (28) has been installed in hygroscopic acid circulation groove, hygroscopic acid circulating-pump outlet is connected with hygroscopic acid water cooler (26), and hygroscopic acid water cooler is connected with the acid trap in moisture absorption tower.
Concentration of hydrogen sulfide 42% in the sour gas raw material of this half-dried legal system sulfuric acid apparatus, also contains a small amount of hydrogen and sulfurous organic compound, and the hydrogen sulphur ratio of unstripped gas is 1.99.Unit scale be every day 200 tons of sulfuric acid (with 100%H
2sO
4meter), local normal atmosphere is 81kPa.
Air after filtration, after air blower pressurization, enters drying tower.Dried dry air enters incinerator, with the direct mixed firing of sour gas.Go out the SO in incinerator gas
2concentration is that 7.8% (butt), temperature enter middle pressure steam boiler 1100 DEG C of left and right, is cooled to 420 DEG C and enters the 1st section of convertor through moving heat, transforms for the first time (transform and have 3 sections of beds for the first time).The 1st section transforms bed temperature out 560 DEG C of left and right, after high temperature superheater cooling, entering the 2nd section of convertor transforms, then enter again the 3rd section of conversion of convertor through hot heat exchanger cooling, the 3rd section of conversion outlet arranges overheated/hot and cold heat exchanger, temperature dropped to 260 DEG C of left and right and enter moisture absorption tower.Moisture in gas more than 90% and SO
3under being absorbed by hygroscopic acid in moisture absorption tower, moisture absorption tower exit gas enters the first absorption tower and absorbs further.
The water sulphur ratio of moisture absorption tower inlet gas is 1.035.Moisture absorption tower absorbs the SO in gas with recycle acid
3and water, the hygroscopic acid recycle system is moisture absorption tower, hygroscopic acid circulation groove, hygroscopic acid recycle pump, hygroscopic acid water cooler.The hygroscopic acid water cooler of this device is vapour generator, the saturation steam of by-product 0.5MPa, moisture absorption tower import recycle acid temperature in 185 DEG C of left and right, recycle acid concentration in 99.3% left and right.Moisture absorption tower absorbs the acid string getting off toward dry dry sour side of inhaling sour circulation groove.
The first absorption tower exit gas passes through respectively hot and cold heat exchanger and hot heat exchanger, enters the 4th section of convertor and transform for the second time after heated intensification.The 4th section of exit gas of convertor enters overheated/economizer and cools, and then enters second absorption tower, and second absorption tower exit gas is directly from chimney emptying.
Dry three towers of inhaling share a sour circulation groove.Dried side with absorb between side with partition wall separate, partition wall bottom is communicated with.Dry acid circulation is groove, pump, acid cooler, tower, groove.Two absorption towers share an acid circulating pump and an acid cooler, after the lower tower acid of two towers merges, get back to and absorb sour circulation groove, and absorbing acid circulation is groove, pump, acid cooler, Liang Ta, groove.Absorption acid concentration is controlled by being dried string acid amount, and absorption side string goes out acid and flows to dried side by partition wall bottom.Product acid is drawn from dry acid cooler outlet, and product acid concentration determines by airborne moisture, and the product acid concentration under the hottest monthly mean temperature and medial humidity is 95.3%.
5.5 tons of the saturation steams of this embodiment by-product 4.4MPa per hour, 16.8 tons of the middle pressure superheated vapours of 435 DEG C and 0.5MPa, adding up to byproduct steam is 22.3 tons per hour.The steam productive rate of amounting to acid per ton is 2.68 tons, wherein in sour by-product per ton, presses 2.02 tons of superheated vapours, 0.66 ton of low-pressure saturated steam.
This embodiment emission 20830Nm3 per hour, amounts to acid discharge 2533Nm3 per ton.In tail gas, SO2 content is 95ppm, i.e. 270mg/Nm3.
A kind of raw material is the semidrying sulphuric acid plant of the sour gas of sulfur-bearing, gas system structure is as Fig. 3, comprises air filter, gas blower, drying tower, 3 air preheaters, incinerator, overheated/economizer, convertor, waste heat boiler, moisture absorption tower, absorption tower.Acid system comprises hygroscopic acid water cooler, hygroscopic acid recycle pump, hygroscopic acid circulation groove, dry sour circulation groove, dry acid circulating pump, the dry acid cooler of inhaling inhaled inhaled.
Its principal character is: the drying tower (3) of dry air is connected with air preheater A (33), air preheater A is connected with air preheater B (32), air preheater B is connected with air preheater C (31), air preheater C is connected with incinerator (4), incinerator is connected with overheated/economizer (34), overheated/economizer is connected with convertor (6), convertor is connected with waste heat boiler (5), waste heat boiler is connected with air preheater A, air preheater A is connected with moisture absorption tower (7), moisture absorption tower is connected with absorption tower (35), the outlet of moisture absorption tower acid is connected with hygroscopic acid circulation groove (27), hygroscopic acid recycle pump (28) has been installed in hygroscopic acid circulation groove, hygroscopic acid circulating-pump outlet is connected with hygroscopic acid water cooler (26), and hygroscopic acid water cooler is connected with the acid trap in moisture absorption tower.
Main containing COS and hydrogen sulfide in the sour gas raw material of this half-dried legal system sulfuric acid apparatus, total sulfur-bearing is 4%, and the hydrogen sulphur ratio of unstripped gas is 1.96, and raw gas flow is 9000Nm3/h, per hour to the supplementary 150kg sulphur of incinerator.Unit scale is to produce 48 tons of sulfuric acid every day (with 100%H
2sO
4meter), local normal atmosphere is 100kPa.
Air after filtration is after air blower pressurization, and part enters drying tower and is dried by the vitriol oil.After dry, wet air mixes, enter incinerator be converted the 3rd section of device, the 2nd section and the 1st section of exit gas laser heating in 3 air preheaters after, with sour gas and sulphur mixed firing.Go out the SO in incinerator gas
2concentration is 3.3% left and right (butt), enters steam superheating/economizer, enters the 1st section of convertor and carry out SO after moving heat drop temperature
2transform, the 1st section transforms bed temperature out 480 DEG C of left and right, after air preheater C cooling, enter convertor and carry out the 2nd section of conversion, the 2nd section transforms outlet and after air preheater B cooling, enters the 3rd section of convertor and transform, and the 3rd section of outlet drops to 240 DEG C of left and right through waste heat boiler and air preheater A by temperature and enter moisture absorption tower.Moisture absorption tower exit gas enters absorption tower.
The water sulphur ratio of moisture absorption tower inlet gas is 1.026.Moisture absorption tower absorbs the SO in gas with recycle acid
3and water, the hygroscopic acid recycle system is moisture absorption tower, hygroscopic acid circulation groove, hygroscopic acid recycle pump, hygroscopic acid water cooler.The hygroscopic acid water cooler of this device is vapour generator, the saturation steam of by-product 0.5MPa, moisture absorption tower import recycle acid temperature in 180 DEG C of left and right, recycle acid concentration in 99.5% left and right.Moisture absorption tower absorbs the sulfuric acid string getting off toward the sour circulation groove of dry suction.
Dry two towers of inhaling share a sour circulation groove, dried side with absorb between side with partition wall separate, partition wall bottom is communicated with, sour from absorption effluent to dried side.Dry acid circulation and absorption acid circulation are all groove, pump, acid cooler, tower, groove.Absorb acid concentration by being dried the control of string acid amount, absorb side string and go out acid by the outflow of partition wall bottom.Product acid is drawn from dry acid cooler outlet, and product acid concentration is determined by airborne moisture, between 97.6% to 98.4%.
1.5 tons of the saturation steams of this embodiment by-product 3.82MPa per hour, 2.8 tons of the middle pressure superheated vapours of 350 DEG C and 0.5MPa, adding up to byproduct steam is 4.3 tons per hour.The steam productive rate of amounting to acid per ton is 2.12 tons, wherein in sour by-product per ton, presses 1.38 tons of superheated vapours, 0.75 ton of low-pressure saturated steam.
What this embodiment adopted is one turns one and absorbs metallization processes, and emission 13500Nm3 per hour, amounts to acid discharge 6750Nm3 per ton.In tail gas, SO2 content is 515ppm, and absorption tower exit gas need to also carry out tail gas absorption.
A kind of raw material is the semidrying sulphuric acid plant of hydrogen sulfide containing sour gas, gas system structure, as Fig. 4, comprises the predrying device of air, drying tower, gas blower, air preheater D, air preheater E, incinerator, waste heat boiler, vapor superheater, convertor, gas heat exchanger, moisture absorption tower, the first absorption tower, economizer, second absorption tower, chimney.Acid system comprises hygroscopic acid water cooler, hygroscopic acid recycle pump, hygroscopic acid circulation groove, dry sour circulation groove, dry acid circulating pump, the dry acid cooler of inhaling inhaled inhaled.
Its principal character is: the drying tower (3) of dry air is connected with gas blower (2), gas blower is connected with air preheater D (44), air preheater D is connected with air preheater E (43), air preheater E is connected with incinerator (4), incinerator is connected with waste heat boiler (5), waste heat boiler is connected with vapor superheater (42), vapor superheater is connected with convertor (6), convertor is connected with gas heat exchanger (46), gas heat exchanger is connected with moisture absorption tower (7), and moisture absorption tower is connected with the first absorption tower (8); The outlet of moisture absorption tower acid is connected with hygroscopic acid circulation groove (27), hygroscopic acid recycle pump (28) has been installed in hygroscopic acid circulation groove, hygroscopic acid circulating-pump outlet is connected with hygroscopic acid water cooler (26), and hygroscopic acid water cooler is connected with the acid trap in moisture absorption tower.
Main sulfide hydrogen in the sour gas raw material of this half-dried legal system sulfuric acid apparatus, concentration of hydrogen sulfide is 10%, and the hydrogen sulphur ratio of unstripped gas is 2.02.Unit scale be every day 100 tons of sulfuric acid (with 100%H
2sO
4meter), local normal atmosphere is 100kPa.
Air after the moisture (depending on the humidity of air) with siccative removal 25% to 75%, enters the drying tower vitriol oil further dry in the predrying device of air.Dried air, after main blower pressurization, is converted respectively after the 3rd section of device and the 1st section of exit gas heat and enters incinerator, with sour gas mixed firing in two air preheaters.The SO2 concentration going out in incinerator gas is that 5% left and right (butt), temperature are 850 DEG C of left and right, enter middle pressure steam boiler and vapor superheater, after moving heat drop temperature, enter the 1st section of convertor and transform for the first time (transform and have 2 sections of beds for the first time).The 1st section transforms bed temperature out 510 DEG C of left and right, enters convertor and carry out the 2nd section of conversion after air preheater E cooling, and the 2nd section of conversion outlet arranges gas heat exchanger, temperature dropped to 250 DEG C of left and right and enter moisture absorption tower.Moisture absorption tower exit gas enters the first absorption tower.
The water sulphur ratio of moisture absorption tower inlet gas is 1.054.Moisture absorption tower absorbs the SO in gas with recycle acid
3and water, the hygroscopic acid recycle system is moisture absorption tower, hygroscopic acid circulation groove, hygroscopic acid recycle pump, hygroscopic acid water cooler.The hygroscopic acid water cooler of this device is vapour generator, the saturation steam of by-product 0.6MPa, moisture absorption tower import recycle acid temperature in 180 DEG C of left and right, recycle acid concentration in 99.0% left and right.Moisture absorption tower absorbs the sulfuric acid string getting off toward the sour circulation groove of dry suction.
The first absorption tower exit gas enters gas heat exchanger, enters the 3rd section of convertor and transform for the second time after heated intensification.The 3rd section of exit gas of convertor enters economizer and air preheater D cools, and then enters second absorption tower, and second absorption tower exit gas is directly from chimney emptying.
Dry three towers of inhaling share a sour circulation groove, an acid circulating pump and an acid cooler.Acid circulation is groove, pump, acid cooler, three towers, groove.Product acid is drawn from the outlet of dry suction acid cooler, and product acid concentration is 98.3% left and right, is regulated by the drying efficiency of predrying device.
2.9 tons of the saturation steams of this embodiment by-product 3.82MPa per hour, 5.8 tons of the middle pressure superheated vapours of 450 DEG C and 0.6MPa, adding up to byproduct steam is 8.7 tons per hour.The steam productive rate of amounting to acid per ton is 2.09 tons, wherein in sour by-product per ton, presses 1.38 tons of superheated vapours, 0.71 ton of low-pressure saturated steam.
This embodiment emission 16870Nm3 per hour, amounts to acid discharge 4286Nm3 per ton.In tail gas, SO2 content is 90ppm, i.e. 255mg/Nm3.
Although above-mentioned 3 specific embodiments have been described the utility model, this description does not mean that and is construed as limiting.With reference to after description of the present utility model, for person skilled in the art, obviously can make various corrections to the disclosed embodiments.Within various similar correction all falls into claim scope of the present utility model.
Claims (2)
1. half-dried legal system sulfuric acid apparatus, taking sour gas as raw material, comprise drying tower, moisture absorption tower, gas system also comprises air filter, main blower, incinerator, convertor, gas heat exchanger, waste heat boiler, vapor superheater, economizer, the first absorption tower and second absorption tower etc., acid system comprises hygroscopic acid water cooler, hygroscopic acid recycle pump, hygroscopic acid circulation groove, the sour circulation groove of dry suction, dry acid circulating pump, dry acid cooler, absorbs acid circulating pump, absorbs acid cooler etc., it is characterized in that:
The drying tower (3) of dry combustion-supporting gas is connected with incinerator (4), and incinerator is connected with waste heat boiler (5), and waste heat boiler is connected with convertor (6);
Convertor is connected with overheated/hot and cold heat exchanger (14), and overheated/hot and cold heat exchanger is connected with moisture absorption tower (7), and moisture absorption tower is connected with the first absorption tower (8).
2. half-dried legal system sulfuric acid apparatus according to claim 1, it is characterized in that: the outlet of moisture absorption tower acid is connected with hygroscopic acid circulation groove (27), hygroscopic acid recycle pump (28) has been installed on hygroscopic acid circulation groove, hygroscopic acid circulating-pump outlet is connected with hygroscopic acid water cooler (26), and hygroscopic acid water cooler is connected with the acid trap in moisture absorption tower.
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| CN201320812895.XU CN203668003U (en) | 2013-12-12 | 2013-12-12 | Half-dry sulfuric acid making device |
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| CN201320812895.XU CN203668003U (en) | 2013-12-12 | 2013-12-12 | Half-dry sulfuric acid making device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105129746A (en) * | 2015-09-09 | 2015-12-09 | 茌平县明大化工有限公司 | Method for cleanly producing food additive sulfuric acid |
| US9815693B2 (en) | 2013-07-18 | 2017-11-14 | Shell Oil Company | Processes for producing sulfuric acid from sour tail gas field |
| CN110655044A (en) * | 2019-11-01 | 2020-01-07 | 武汉青江化工黄冈有限公司 | Reagent sulfuric acid production device and process |
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
-
2013
- 2013-12-12 CN CN201320812895.XU patent/CN203668003U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9815693B2 (en) | 2013-07-18 | 2017-11-14 | Shell Oil Company | Processes for producing sulfuric acid from sour tail gas field |
| CN105129746A (en) * | 2015-09-09 | 2015-12-09 | 茌平县明大化工有限公司 | Method for cleanly producing food additive sulfuric acid |
| CN110655044A (en) * | 2019-11-01 | 2020-01-07 | 武汉青江化工黄冈有限公司 | Reagent sulfuric acid production device and process |
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
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