CN109761203A - A kind of high concentration SO2Convert acid-making process - Google Patents
A kind of high concentration SO2Convert acid-making process Download PDFInfo
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- CN109761203A CN109761203A CN201910161253.XA CN201910161253A CN109761203A CN 109761203 A CN109761203 A CN 109761203A CN 201910161253 A CN201910161253 A CN 201910161253A CN 109761203 A CN109761203 A CN 109761203A
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Abstract
The invention discloses a kind of high concentration SO2Acid-making process is converted, belongs to sulfur recovery technical field, comprising the following steps: (1) be mixed with O2Purification wet flue gas enter drying tower dehydration, be warming up to predetermined temperature into pre- heat exchanger later；(2) purifying smoke after heating up enters pre-converter catalyst layer and reacts, each catalyst layer of the flue gas Jing Guo pre-converter, SO2Concentration declines 7%, SO any for pre-inversion entrance2The flue gas of concentration, control outlet layer flue-gas temperature are lower than 620 DEG C；(3) flue gas cool-down that pre-converter comes out enters pre-absorption tower later and carries out absorbing relieving haperacidity for the first time, by absorbing SO to set temperature3And the flue gas after air distribution, into traditional SO2Convert acid making system；Present invention process is simple, of less demanding to the equipment such as blower, the converter working condition to be adapted to, and is a kind of high concentration SO being easily achieved2Conversion process.
Description
Technical field
The invention belongs to sulfur recovery technical fields, and in particular to a kind of high concentration SO2Convert acid-making process.
Background technique
In nonferrous metallurgy, with the gradually popularization of oxygen-rich smelting technology, into dioxy in the flue gas of flue gas acid preparing system
Change sulphur concentration reaches 20% or more and has become reality.Due to the limit of conversion catalyst resistance to extreme temperature (630 DEG C or so) and initiation temperature
System, under equilibrium conversion, smoke inlet SO2It is that conversion catalyst generally acknowledged in the world is acceptable most that concentration, which is no more than 14%,
High SO2Concentration.To conversion high concentration SO2Flue gas carries out a large amount of air distribution and is bound to cause relieving haperacidity conversion, does and inhale the huge of specification of equipment
Greatly, the overall economic efficiency of oxygen-enriched air smelting is also limited to a certain extent.How SO is broken through2The limitation of concentration is flue gas during smelting system
The research direction that sour industry needs actively to make great efforts.It is current that there are many highly concentrated SO2Flue gas acid preparing technique, but it converts entrance SO2It is dense
Degree generally does not exceed 19%, for this purpose, there is still a need for be incorporated to be equivalent to itself one times or more of dilution wind.
Summary of the invention
The purpose of the present invention is to provide a kind of high concentration SO2Acid-making process is converted, can adapt to any concentration SO2Flue gas
Conversion acid-making process, and be no more than the requirement of conversion catalyst limiting temperature, reduce subsequent acid-producing apparatus specification, realize energy conservation drop
Consumption.
The present invention provides a kind of high concentration SO2Convert acid-making process, comprising the following steps:
(1) it is mixed with O2Purification wet flue gas enter drying tower dehydration, be warming up to predetermined temperature into pre- heat exchanger later；
(2) purifying smoke after heating up enters pre-converter catalyst layer and reacts, each touching of the flue gas Jing Guo pre-converter
Matchmaker's layer, SO2Concentration declines 7%, SO any for pre-inversion entrance2The flue gas of concentration, control outlet layer flue-gas temperature are lower than
620℃；
(3) flue gas cool-down that pre-converter comes out enters pre-absorption tower later and carries out absorbing system for the first time to set temperature
Acid, by absorbing SO3And the flue gas after air distribution, into traditional SO2Convert acid making system.
Preferably, in step (1), purifying smoke enters pre- heat exchanger and is warming up to 390~420 DEG C.
Preferably, in step (2), SO any for pre-inversion entrance2The flue gas of concentration, control outlet layer flue-gas temperature
Lower than 600 DEG C.
Preferably, in step (3), the flue gas cool-down that pre-converter comes out is to 170~190 DEG C.
Preferably, in step (2), SO in pre-converter entrance purifying smoke2Concentration is 11~18%, and control oxygen sulphur ratio is
One layer of catalyst is arranged in 1:1 or so, pre-converter, and the pre-inversion catalyst number of plies should be according to the highest SO of inlet flue gas2Concentration is arranged
Selection.
Preferably, in step (2), SO in pre-converter entrance purifying smoke2Concentration is 30~37%, and control oxygen sulphur ratio is
Three layers of catalyst are arranged in 1:3 or so, pre-converter.
Preferably, in step (2), SO in pre-converter entrance purifying smoke2Concentration is 18~30%, and control oxygen sulphur ratio is
Two layers of catalyst is arranged in 1:3 or so, pre-converter.
It is furthermore preferred that corresponding highest SO2Concentration is by two layers of pre-inversion catalyst design, purified highly concentrated SO2Flue gas is through overdrying
After dry tower removing moisture, it is warming up to predetermined temperature into pre- heat exchanger, enters one layer of catalyst layer reaction of pre-inversion later, and control
One layer of outlet temperature is made lower than 620 DEG C, controls two layers of outlet temperature into two layers of catalyst layer reaction of pre-inversion again after heat exchange cooling
Degree is also preferably below 620 DEG C, flue gas SO after each catalyst layer of pre-converter2Concentration declines 7%, enters after heat exchange cooling pre-
Absorption tower carries out absorbing relieving haperacidity for the first time, meanwhile, it is incorporated diluent air, the flue gas after air distribution enters traditional SO2Convert relieving haperacidity
System.
Further, the O in flue gas after pre-absorption2Concentration is extremely low, SO3All absorb relieving haperacidity, control after air distribution O in flue gas,
S ratio is close to 1:1, SO2Concentration is lower than 12%, enters SO later2Air blower, the SO that air blower comes out2Flue gas enters subsequent two turn two
It inhales acid making system and produces acid.
Further, diluent air can be directly incorporated from pre-absorption tower, can also first pass through SO2After concentrated acid desorption tower is dry from
It is incorporated after pre-absorption tower.
The present invention provides a kind of high concentration SO2Acid-making process is converted, which has the characteristics that as follows:
1) each catalyst layer of pre-inversion utilizes the catalyst filling amount far below equilibrium conversion to control SO2The extent of reaction with
Control conversion coating exit gas temperature.
2) air distribution is just carried out in the pre-absorption stage, effectively controls the specification of equipment of pre-converter.
3) after blower is placed in pre-absorption tower, acid making system is made there was only a SO2Blower avoids setting air blower and main wind
The problems such as chain control is complicated between the stuck guide vane of machine pressure unmatched and blower.
4) pre-inversion layer is located at SO2Before blower, negative pressure is conducive to the conversion ratio of control pre-inversion layer.
5) smaller with air quantity, it is 50% or so, the specification of acid-producing apparatus after blower can be effectively controlled.
6) compared to other highly concentrated SO2Acid-making process, such as: the flue gas recirculation of Lurgi, the constant temperature conversion of Bayer, Meng Mo
Gram double raw material method relieving haperacidity conversion process, the complexity of present invention process wants much lower, to fit to equipment such as blower, converters
The working condition answered is of less demanding, and process flow is simple, is a kind of high concentration SO being easily achieved2Conversion process.
Detailed description of the invention
Fig. 1 is the device and flow chart of the embodiment of the present invention 1.
Fig. 2 is the device and flow chart of the embodiment of the present invention 2.
Fig. 3 is the device and flow chart of the embodiment of the present invention 3.
Specific embodiment
The technical scheme in the embodiments of the invention will be clearly and completely described below, it is clear that described implementation
Example is only a part of the embodiment of the present invention, rather than whole embodiments, based on the embodiments of the present invention, ordinary skill
Personnel's every other embodiment obtained without making creative work, shall fall within the protection scope of the present invention.
The invention will be further described with attached drawing combined with specific embodiments below.
Embodiment 1
The present invention is described in detail as follows in conjunction with attached drawing 1 and embodiment:
SO in wet flue gas from cleaning procedure2Concentration is 29%, O2Concentration is 10%, is introduced into drying tower dehydration (no leakage
Wind), enter pre- II heat exchanger later, gas temperature rises to 190 DEG C from 45 DEG C, enters pre- I heat exchanger afterwards, and temperature rises
To 390 DEG C, then into one layer of catalyst reaction of pre-converter, SO in flue gas after reaction2Concentration is down to 22%, O2Concentration is down to 6.5%,
SO3Concentration is 7%, and the 600 DEG C of high-temperature flue gas come out from pre- one layer of conversion reaction first pass through pre- I heat exchanger heat exchange and are cooled to
400 DEG C, enter pre- two layers catalytic converting, SO in flue gas after reaction afterwards2Concentration is down to 15%, O2Concentration is down to 3%, SO3Concentration is
14%；The 600 DEG C of high-temperature flue gas come out from pre- two layers of converter enter 1# waste heat boiler, by-product 5.5MPa middle pressure steam；Flue gas
Temperature enters pre- II heat exchanger after being down to 315 DEG C and exchanges heat, and temperature drops to 170 DEG C, later SO3Flue gas be sent to pre-absorption tower into
Row absorbs relieving haperacidity for the first time, and diluent air can pass through SO2Concentrated acid desorption tower drying and dehydrating, then the SO come out with pre-absorption tower2Flue gas
It mixes to SO2/O2For volume ratio close to 1:1, diluent air is about SO2The 50% of flue gas；By absorbing SO3And 45 DEG C after air distribution
SO in flue gas2Concentration is down to 11%, O2Concentration rises to 10%, enters SO afterwards2Main blower pressurization；95 DEG C of cigarettes that air blower comes out
Gas enters conventional double-absorption acid making system, and this example accesses III, I-IV, II double-absorption process, wherein three layers are converted to come
SO3Flue gas can pass through waste heat boiler by-product 5.5MPa middle pressure steam.
In order to cope with the flue gas variation of fluctuation, it is equipped with dilution wind on drying tower inlet tube and is blended into mouth, and leakproofness is housed
Can preferable semisphere valve, adjust valve group, enter system exhaust gas volumn it is smaller when (such as: when normal 30%), can be directly to drying tower
Being blended into dilution wind reduces SO2For concentration to 7%, flue gas manages (not into pre-inversion, pre-absorption system) by the short circuit of pre-reformer
Afterwards, directly into SO2Blower is sent into routine 3+1 double-absorption system relieving haperacidity.When tolerance restores normal, drying tower dilution wind is shut
Valve, air is then through SO2SO is mixed into after concentrated acid desorption tower is dry2Blower.
Embodiment 2
The present invention is described in detail as follows in conjunction with attached drawing 2 and embodiment:
SO in wet flue gas from cleaning procedure2Concentration is 18%, O2Concentration is 17%, is introduced into drying tower dehydration (no leakage
Wind), enter pre- I heat exchanger later；Gas temperature rises to 420 DEG C from 45 DEG C, and one layer of catalyst of laggard pre-converter reacts, instead
SO in flue gas after answering2Concentration is down to 11%, O2Concentration is down to 13.5%, SO3Concentration is 7%, is come out from pre- one layer of conversion reaction
600 DEG C of high-temperature flue gas are cooled to 255 DEG C by the heat exchange of pre- I heat exchanger, enter the water supply of economizer preboiler afterwards；Flue-gas temperature
Enter pre-absorption tower after being down to 190 DEG C to carry out absorbing relieving haperacidity for the first time；Absorb SO3SO in 60 DEG C of flue gases afterwards2Concentration rises to
11.8%, O2Concentration rises to 14.5%, enters back into SO2Main blower pressurization；Air blower comes out 110 DEG C of SO2Flue gas enters normal
It is system converting to advise 3+1.
Exhaust gas volumn and SO are generated in order to cope with to smelt2The big ups and downs of concentration, while being set before drying tower and pre-absorption tower
There is dilution wind to be blended into mouth, and equipped with the preferable semisphere valve of sealing performance, adjusting valve group.When the exhaust gas volumn very little for entering this system
When, wind can be released from drying tower thinning by SO2Concentration is down to 7%, and flue gas is by the short circuit pipe of pre-inversion absorption plant (not into prerotation
Change system) afterwards directly into SO2Blower is sent into routine 3+1 double-absorption system relieving haperacidity.When tolerance restores normal, drying tower is shut
Air-valve is diluted, air is then incorporated from pre-absorption tower.
Embodiment 3
The present invention is described in detail as follows in conjunction with attached drawing 3 and embodiment:
Contain SO from cleaning procedure2The wet flue gas of 40% or more concentration is introduced into drying tower dehydration, drying tower air distribution to cigarette
SO in gas2Concentration 37%, O2Concentration enters pre- II heat exchanger after being 13%；It is handed over by pre- II heat, gas temperature rises from 45 DEG C
To 190 DEG C, enter pre- I heat exchanger afterwards, temperature rises to 400 DEG C, then into one layer of catalyst reaction of pre-converter, flue gas after reaction
Middle SO2Concentration is down to 30%, O2Concentration is down to 9.5%, SO3Concentration is 7%, the 600 DEG C of high temperature come out from pre- one layer of conversion reaction
Flue gas first passes through pre- I heat exchanger heat exchange and is cooled to 400 DEG C, enters pre- two layers catalytic converting, SO in flue gas after reaction afterwards2Concentration
It is down to 23%, O2Concentration is down to 6%, SO3Concentration is 14%；The 600 DEG C of high-temperature flue gas come out from pre- two layers of converter enter more than 1#
Heat boiler, by-product 5.5MPa middle pressure steam；400 DEG C of high-temperature flue gas of 1# boiler export enter pre- three layers catalytic converting, cigarette after reaction
SO in gas2Concentration is down to 16%, O2Concentration is down to 2.5%, SO3Concentration is 21%.600 DEG C of high temperature that pre- three layers of converter comes out
Flue gas enters 2# waste heat boiler, by-product 5.5MPa middle pressure steam.Flue-gas temperature enters pre- II heat exchanger after being down to 315 DEG C and changes
Heat, temperature drop to 180 DEG C, the SO after heat exchange3Flue gas is sent to pre-absorption tower and carries out absorbing relieving haperacidity for the first time；It dilutes wind and passes through SO2
Concentrated acid desorption tower drying and dehydrating, then the SO come out with pre-absorption tower2Flue gas is mixed to SO2/O2Volume ratio is close to 1:1, diluent air
About SO2The 60% of flue gas；Through absorbing SO3And SO in 45 DEG C of flue gases of air distribution mixing2Concentration is down to 11.5%, O2Concentration rises to
10.9%, enter SO afterwards2Main blower pressurization, pressurized 95 DEG C of flue gases enter conventional (two turn two of the relieving haperacidity of double-absorption system
It inhales process to omit).
The big ups and downs for generating exhaust gas volumn are smelted in order to cope with, dilution wind is equipped in drying tower inlet tube and is blended into mouth, and fill
There are the preferable semisphere valve of sealing performance, adjusting valve group directly can be blended into dilution wind to drying tower when entering system exhaust gas volumn very little
Reduce SO2Concentration is to 7%, and flue gas is after the short circuit pipe (not into pre-conversion system) of pre-inversion absorption plant, directly into SO2Wind
Machine is sent into routine 3+1 double-absorption system relieving haperacidity.When tolerance restores normal, drying tower dilution air-valve is shut, air is then through SO2
The dry laggard SO of concentrated acid desorption tower2Blower.
Although the embodiments of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is not considered as limiting the invention, those skilled in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, modifies, replacement and variant.
Claims (10)
1. a kind of high concentration SO2Convert acid-making process, which comprises the following steps:
(1) it is mixed with O2Purification wet flue gas enter drying tower dehydration, be warming up to predetermined temperature into pre- heat exchanger later；
(2) purifying smoke after heating up enters pre-converter catalyst layer and reacts, each catalyst layer of the flue gas Jing Guo pre-converter,
SO2Concentration declines 7%, SO any for pre-inversion entrance2The flue gas of concentration, control outlet layer flue-gas temperature are lower than 620
℃；
(3) flue gas cool-down that pre-converter comes out enters pre-absorption tower later and carries out absorption relieving haperacidity for the first time, warp to set temperature
Cross absorption SO3And the flue gas after air distribution, into traditional SO2Convert acid making system.
2. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (1), purifying smoke into
Enter pre- heat exchanger and is warming up to 390~420 DEG C.
3. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (2), for pre-inversion
Any SO of entrance2The flue gas of concentration, control outlet layer flue-gas temperature are lower than 600 DEG C.
4. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (3), pre-converter goes out
The flue gas cool-down come is to 170~190 DEG C.
5. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (2), pre-converter enters
SO in mouth purifying smoke2Concentration is 11~18%, and control oxygen sulphur ratio is 1:1 or so, and one layer of catalyst, pre-inversion is arranged in pre-converter
The catalyst number of plies should be according to the highest SO of inlet flue gas2Concentration selects to be arranged.
6. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (2), pre-converter enters
SO in mouth purifying smoke2Concentration is 30~37%, and control oxygen sulphur ratio is 1:3 or so, and three layers of catalyst are arranged in pre-converter.
7. high concentration SO according to claim 12Convert acid-making process, which is characterized in that in step (2), pre-converter enters
SO in mouth purifying smoke2Concentration is 18~30%, and control oxygen sulphur ratio is 1:3 or so, and two layers of catalyst is arranged in pre-converter.
8. high concentration SO according to claim 72Convert acid-making process, which is characterized in that corresponding two layers of pre-inversion catalyst is set
Meter, purified highly concentrated SO2Flue gas is warming up to predetermined temperature into pre- heat exchanger, later after drying tower removes moisture
It into one layer of catalyst layer reaction of pre-inversion, and controls one layer of outlet temperature and is lower than 620 DEG C, again into pre-inversion after heat exchange cooling
Two layers of catalyst layer reaction, control two layers of outlet temperature and are also preferably below 620 DEG C, flue gas SO after each catalyst layer of pre-converter2
Concentration declines 7%, and pre-absorption tower is entered after heat exchange cooling and carries out absorbing relieving haperacidity for the first time, meanwhile, it is incorporated diluent air, air distribution
Flue gas afterwards enters traditional SO2Convert acid making system.
9. high concentration SO according to claim 82Convert acid-making process, which is characterized in that the O in flue gas after pre-absorption2
Concentration is extremely low, SO3Relieving haperacidity are all absorbed, O, S ratio are controlled in flue gas after air distribution close to 1:1, SO2Concentration is lower than 12%, enters later
SO2Air blower, the SO that air blower comes out2Flue gas enters subsequent double-absorption acid making system and produces acid.
10. high concentration SO according to claim 82Convert acid-making process, which is characterized in that diluent air can directly from
Pre-absorption tower supplying, can also first pass through SO2It is incorporated after pre-absorption tower after concentrated acid desorption tower is dry.
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Cited By (4)
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| CN110538543A (en) * | 2019-08-30 | 2019-12-06 | 楚雄滇中有色金属有限责任公司 | Method for stably reaching standard of tail gas in initial stage of acid making and coproduction by smelting flue gas |
| CN112441566A (en) * | 2019-08-29 | 2021-03-05 | 中石化南京化工研究院有限公司 | Distributed SO of sulfuric acid device2Transformation method |
| CN112875653A (en) * | 2021-02-06 | 2021-06-01 | 易门铜业有限公司 | Acid temperature and acid concentration balancing system and method for high-concentration flue gas acid making |
| CN114572939A (en) * | 2022-04-01 | 2022-06-03 | 陕西莹钰化工设备有限公司 | Original SO2Technology for preparing sulfuric acid by partial pre-conversion |
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| CN112441566A (en) * | 2019-08-29 | 2021-03-05 | 中石化南京化工研究院有限公司 | Distributed SO of sulfuric acid device2Transformation method |
| CN110538543A (en) * | 2019-08-30 | 2019-12-06 | 楚雄滇中有色金属有限责任公司 | Method for stably reaching standard of tail gas in initial stage of acid making and coproduction by smelting flue gas |
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| CN112875653A (en) * | 2021-02-06 | 2021-06-01 | 易门铜业有限公司 | Acid temperature and acid concentration balancing system and method for high-concentration flue gas acid making |
| CN112875653B (en) * | 2021-02-06 | 2022-06-24 | 易门铜业有限公司 | Acid temperature and acid concentration balancing system and method for high-concentration flue gas acid making |
| CN114572939A (en) * | 2022-04-01 | 2022-06-03 | 陕西莹钰化工设备有限公司 | Original SO2Technology for preparing sulfuric acid by partial pre-conversion |
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