CN202864918U - Waste gas treatment system of acid gas - Google Patents
Waste gas treatment system of acid gas Download PDFInfo
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- CN202864918U CN202864918U CN 201220564443 CN201220564443U CN202864918U CN 202864918 U CN202864918 U CN 202864918U CN 201220564443 CN201220564443 CN 201220564443 CN 201220564443 U CN201220564443 U CN 201220564443U CN 202864918 U CN202864918 U CN 202864918U
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Abstract
The utility model provides a waste gas treatment system of acid gas, consisting of a rich acid gas heating reaction treatment unit, a Claus treatment unit, a Claus tail gas and pool acid gas burning unit, a burned tail gas catalytic oxidation acid making unit, a secondary transition acid making unit and a tail gas re-heating unit. The waste gas treatment system of acid gas disclosed by the utility model has the advantages that the sulfur recovery rate of the whole set of acid gas treatment system can reach to be more than 99.99%, SO2 concentration of the tail gas discharged into atmosphere is 100mg/m<3>, and no waste liquor is discharged in the system. Besides, the transition rate and the charging concentration satisfy the highest standard of discharging limits in the industry.
Description
Technical field
The utility model relates to a kind of sour gas flare system.
Background technology
In the production processes such as petrochemical complex, Coal Chemical Industry, sulphur in the raw material finally changes into the high-concentration acidic wastewater gas of sulfide hydrogen tens percent in the course of processing, hydrogen sulfide is a kind of to safety and the very harmful material of environment, must process or reclaim before discharging.For fairly large sulfur recovery (greater than several thousand ton/years), for the ease of sale and the accumulating of product, usually adopt Crouse's recovery technology of sulfur that hydrogen sulfide is changed into sulphur.
The conventional Claus recovery technology of sulfur is comprised of a thermal response section and several catalyst reaction section.Namely contain H
2The sour gas of S carries out incomplete combustion with air in roasting kiln, strictly control air quantity, makes H
2The SO that generates after the S burning
2Amount satisfies H
2S/SO
2Molecular ratio equals or near 2, H
2S and SO
2At high temperature react generting element sulphur, be subjected to the restriction of thermodynamic condition, remaining H
2S and SO
2Enter catalyst reaction section under the effect of catalyzer, proceed the reaction of generting element sulphur.The elementary sulfur that generates reaches the purpose of recovery through condensation separation.
In the reaction that the thermal response section occurs, the chemical equation of main reaction is as follows:
H
2S+3/2O
2---SO
2+H
2O
2H
2S+SO
2---3/2S
2+2H
2O
The chemical equation of side reaction is as follows:
C
nH
(2n+2)+(3n+1)/2O
2---(n+1)H
2O+nCO
2
H
2S+CO
2---COS+H
2O
CH
4+2S
2---CS
2+2H
2S
2NH
3+3/2O
2---3H
2O+N
2
CO
2+3/2S
2---CS
2+SO
2
In the reaction that catalyst reaction section occurs, the chemical equation of main reaction is as follows:
2H
2S+SO
2---3/xS
x+2H
2O
Side reaction (mainly is COS and CS
2Hydrolysis reaction) chemical equation is as follows:
COS+H
2O---CO
2+H
2S
CS
2+2H
2O---CO
2+2H
2S
In order to guarantee the running of Crouse's sulfur recovery system stability and safety, improve the rate of recovery of sulphur, need to improve as far as possible H in the sour gas
2S concentration and raising thermal response furnace temperature, it is highly beneficial to the sulphur transformation efficiency to improve the thermal response furnace temperature, and simultaneous temperature is higher, more is unfavorable for CS
2Generation.
Since the '30s improvement in this century Crouse sulphur recovery method realizes industrialization, sulphur recovery production equipment take the hydrogen sulfide sour gas as raw material is developed rapidly, but Kraus process there is no much variations at operational path for a long time, and that generally adopts remains single flow or shunting technique.Owing to be subjected to the restriction of chemical equilibrium and reversible reaction under the temperature of reaction, even in the good situation of equipment and operational condition, use active good catalyzer and three grades of claus process, sulfur recovery rate is the highest also can only to reach 95%～97%, still has 3%～5% sulphur with SO
2Form discharge, will cause serious problem of environmental pollution if enter atmosphere, therefore need to adopt the sulfur recovery tail gas treatment process to solve.
So far realized nearly 20 kinds more than of industrialized tail gas clean-up technique.Mainly be divided into the three major types such as low-temperature Claus method, selective oxidation method, Reducing and absorption method.
The low-temperature Claus method
Take MCRC, CBA technique as representative.
The MCRC recovery technology of sulfur is the patented technology of Canadian Delta company mineral products and chemical resource company (Mineraland Chemical Resource Co.) exploitation.This technique is in the situation that is lower than the sulphur dew point, H on solid catalyst
2S and SO
2Proceed claus reaction, because temperature is lower, after the sulphur of gaseous state condenses, be conducive to molecular balance and move towards the direction that generates sulphur, enlarged markedly sulfur recovery rate, MCRC transforms progression two kinds of three grades and level Four, three grades of the sulfur recovery rates of design are 98.5%, and level Four can reach 99%.This method comparatively speaking simple, the facility investment of flow process and process cost is lower.
Because temperature is lower, thereby COS, CS
2Can't transform decomposition Deng organic sulfide in tail gas, the method is to sulphur part H processed simultaneously
2S/SO
2Proportion requirement strict.
The selective oxidation method:
Take the Super claus process as representative.Super Crouse (super Crouse) technique is the patented technology of Dutch Comprimo company exploitation, industrialization in 1988.
This technique is to increase the reactor that catalyst for selective oxidation is housed after Crouse's sulphur recovery, and this catalyzer is with H
2The direct selective oxidation of S becomes elementary sulfur, in order substantially not contain SO in the final stage claus reaction device outlet that makes the upstream sulfur recovery facility
2, must make the excessive operation of sulphur recovery employing hydrogen sulfide this moment, rather than conventional control H
2S/SO
2=2 operation measure makes in the tail gas of the final stage reactor that leaves sulphur recovery and contains 0.8%～1.5%(v) hydrogen sulfide.When adopting this flow process, when the reaction of carrying out before the reactor of catalyst for selective oxidation being housed being secondary and transforming, sulfur recovery rate is 99%.This technical process is simple, and operation is reliable, and facility investment and process cost are low.
The Reducing and absorption method
Take SCOT, RAR technique as representative.
The primary process of this technique is: tail gas of sulphur and hydrogen are mixed to about 300 ℃ (or heat by other type of heating) at the high-temperature flue gas of online roasting kiln mixing section and fuel gas burning after, enter the SCOT reactor, under the hydrogenation catalyst effect, make sulphur and sulfide (S in the tail gas
6, S
8, COS, CS
2) almost all being transformed into hydrogen sulfide, this Process Gas enters desulfuration absorbing tower after cooling, and almost all hydrogen sulfide and partial CO 2 are made in the tail gas total sulfur less than 300ppm, discharging after tail gas burns by solvent absorbing.The rich solution that has absorbed hydrogen sulfide, carbonic acid gas enters regenerator column, and the regeneration overhead sour gas is delivered to sulfur recovery as raw material, and the lean solution after the regeneration returns the absorption tower and recycle.This technique is to utilize sulphur and the sulfide hydrogenating reduction in the tail gas of sulphur or be hydrolyzed into hydrogen sulfide, and through the hydramine solvent absorbing to reach the purpose of cleaning of off-gas, degree of purification is the highest in present various exhaust gas treating methods, total sulfur in the tail gas can be reduced to below the 300ppm, and the total yield of sulphur can reach 99.8%.But this method technical process is complicated, and facility investment and process cost also occupy first of the various exhaust gas treating methods, and in general, the facility investment of SCOT vent gas treatment is suitable with the facility investment of sulphur recovery approximately.
Generally speaking, in this three classes treatment process, the advantages such as technical process is simple though the selective oxidation processes take Super Crouse as representative and the low-temperature Claus technique take MCRC as representative have, less investment, process cost are low, but sulfur recovery rate is low, can only reach 99%, can not satisfy in the existing national source of atmospheric pollution emission standard SO
2Emission concentration is less than 550mg/m
3Requirement; Conventional reduction absorption technique flow process take SCOT as representative is complicated, investment is high, process cost is high, though can satisfy existing environmental requirement, desulfurization degree can only reach 99.8%, can not satisfy higher environmental protection standard.
In recent years, the Coal Chemical Industry industry had obtained develop rapidly in China, and the Acidic Gas Treating problem of coming has with it brought larger challenge then for existing sulfur recovery technique.The sour gas of Coal Chemical Industry industry has own characteristic.Large-minded, concentration of hydrogen sulfide low (volume percent only has twenties percent to thirties usually), and the concentration of COS high (sometimes up to 5%), and often there are one or several strands of poor sour gas of lower concentration in the Coal Chemical Engineering Project, the concentration of hydrogen sulfide only has percentum in the poor sour gas, and in the lower situation, the processing of the poor sour gas of lower concentration is more difficult in the main concentration of sour gas own, often adopt at present poor sour gas preconcentration concentrate, and then enter the claus reaction device.This causes the technical process of system long, and control is complicated, and investment is high.
And aspect the industry policy of country higher environmental requirement is being proposed the Coal Chemical Industry industry, because the restriction of environmental capacity, requirement to the emission concentration of sulfur recovery rate and sulphur is higher, usually require sulfur recovery rate to reach more than 99.8%, even some project demand sulfur recovery rates reach more than 99.97% SO
2Emission concentration is less than 100mg/m
3Even and present various Crouse+Reducing and absorption and improvement technique thereof adopt the new patent solvent, tail gas collecting and recovery with molten sulfur degasification, poor sour gas to lower concentration adopts the preconcentration concentrate to improve thermal response stove temperature of combustion, even increase the various measures such as tail gas Reducing and absorption COS hydrolysis reactor, the SO in the tail gas
2Emission concentration also can only reach the about 300mg/m of 50～100ppm(
3).
In addition, in these techniques, the Claus tail gases behind the hydrogenation needs chilling before entering solvent absorbing, also can produce sulfide hydrogen acid waste water in quenching process, need to take extra measure to process these acid waste water.
Summary of the invention
In view of the problems referred to above that exist in present both at home and abroad Crouse's sulphur recovery and the tail gas treatment process thereof, the purpose of this utility model is to propose a kind of sour gas flare system, can effectively process the sulfocompound in the sour gas, make it reach higher sulfur recovery rate, satisfy stricter exhaust emission standard, and system stability is reliable, less investment, process cost is low, all has excellent operation elasticity under various operating modes.
For achieving the above object, the utility model provides a kind of sour gas flare system, comprising:
Rich sour gas air supply unit is used for providing rich sour gas;
Combustion-supporting gas air supply unit is used for providing combustion-supporting gas;
Poor sour gas air supply unit is used for providing poor sour gas;
Rich sour gas thermal response processing unit, be connected in the downstream of described rich sour gas air supply unit and described combustion-supporting gas air supply unit, be used for carrying out the desulfurization processing by the combustion-supporting described rich sour gas that will pass into described rich sour gas thermal response processing unit of described combustion-supporting gas;
Crouse's processing unit is connected in the downstream of described rich sour gas thermal response processing unit, and the gas after being used for described rich sour gas thermal response processing unit desulfurization processed further carries out desulfurization and processes and produce Claus tail gases;
Claus tail gases and poor sour gas burn the unit, be connected in the downstream of described Crouse's processing unit and the downstream of described poor sour gas air supply unit, be used for burning the molten sulfur degasification tail gas that produces after described poor sour gas, described Claus tail gases and the described rich sour gas thermal response processing unit of process and the described Crouse's processing unit desulfurization processing and producing waste gas from incinerator;
Incineration tail gas catalyzed oxidation relieving haperacidity unit is connected in the downstream that described Claus tail gases and poor sour gas burn the unit, is used for the SO with described waste gas from incinerator
2Change into SO
3, and be combined with water and be condensed into sulfuric acid;
Secondary transforms the relieving haperacidity unit, is connected in the downstream of described incineration tail gas catalyzed oxidation relieving haperacidity unit, is used for further with SO
2Change into SO
3, and be combined with water and be condensed into sulfuric acid; And
The exhaust gas reheater unit is connected in the downstream that described secondary transforms the relieving haperacidity unit, is used for described secondary is transformed the waste gas heating that the relieving haperacidity unit produces;
Described rich sour gas air supply unit and described Claus tail gases and poor sour gas burn between the unit and are provided with: can make at least part of described rich sour gas enter described Claus tail gases and poor sour gas burns the connection line of unit, and the flow regulation device that is used for regulating the described rich sour gas flow of described connection line.
In the utility model one embodiment, described rich sour gas thermal response processing unit comprises for the H with described rich sour gas 1/3rd
2S burns into SO
2Combustion unit, the SO that generates for described burning
2With remaining described H
2S reacts thermal reactor, the waste heat exchanger that is used for heat exchange that generates sulphur and the first step sulfur condenser that is used for condensation sulphur therein.
In the utility model one embodiment, described Crouse's processing unit comprises one-level Crouse treatment unit and secondary Crouse treatment unit, and described one-level Crouse's treatment unit comprises makes remaining SO
2And H
2Claus reaction occurs with the one-level claus reaction device that generates sulphur and is used for the second stage sulfur condenser of the sulphur that the described one-level claus reaction of condensation device produces in S, is used to described one-level claus reaction device that heat is provided from the again thermal bypass gas of the described waste heat exchanger of described rich sour gas thermal response processing unit.
In the utility model one embodiment, described secondary Crouse treatment unit comprises to be made through remaining SO after described one-level Crouse's treatment unit
2And H
2Continue to occur between the S claus reaction with the secondary claus reaction device that generates sulphur, be used to described secondary claus reaction device that Crouse's reheater of heat is provided and be used for the third stage sulfur condenser of the sulphur that the described secondary claus reaction of condensation device produces.
In the utility model one embodiment, described Claus tail gases and poor sour gas burn the unit and comprise be used to the incinerator that burns described Claus tail gases, described poor sour gas and described molten sulfur degasification tail gas, are used for burning the SO of rear generation
2, CO
2And H
2O carries out the incinerator waste heat exchanger of heat exchange cooling and is used for the fume extractor of combustion gas.
In the utility model one embodiment, described incineration tail gas catalyzed oxidation relieving haperacidity unit comprises the SO in the waste gas from incinerator that described incinerator is produced
2Change into SO
3And be combined into the first step convertor of sulfuric acid with water and with the first step condenser of described condensation of sulfuric acid.
In the utility model one embodiment, described secondary conversion relieving haperacidity unit comprises further will be from the SO of described first step condenser
2Change into SO
3And be combined into the second stage convertor of sulfuric acid with water and with the second stage condenser of described condensation of sulfuric acid.
In the utility model one embodiment, described second stage convertor also comprises the second convertor well heater, and described incinerator waste heat exchanger is passed to described the second convertor well heater with heat.
In the utility model one embodiment, described exhaust gas reheater unit comprises for delivery of the exhaust fan of tail gas with for the exhaust gas reheater device with tail gas heating.
According to sour gas flare system of the present utility model, owing to take two-stage Crouse conversion unit and two-stage catalyzed oxidation relieving haperacidity unit, the sulfur recovery rate of a whole set of Acidic Gas Treating system can reach more than 99.99%, is discharged into SO in the tail gas of atmosphere
2Concentration＜100mg/m
3, this transformation efficiency and emission concentration can satisfy industry maximum emission limitation standard, and do not have discharging of waste liquid in the system.
The poor sour gas of low in hydrogen sulphide concentration in the feeding gas, do not need the preconcentration concentrate, directly enter Claus tail gases and poor sour gas incinerator, both provided thermal source for the Claus tail gases incinerator, indirectly improved again the total sour gas concentration that enters the thermal response processing unit, be conducive to improve the transformation efficiency of hydrogen sulfide, guaranteed the steady running of Crouse unit, simultaneously, simplify flow process, saved investment, in addition, when poor acid tolerance is very few, can enter Claus tail gases and poor sour gas burning unit by the rich sour gas of by-passing portions, system does not need postcombustion gas and external heat source.
Very few or concentration is excessively low when the rich sour gas tolerance of charging, when Crouse's processing unit is difficult to steady running, can be stopped transport in the Crouse unit, all sour gas introducing Claus tail gases and poor sour gas burn the unit burning, then in follow-up two-stage catalyzed oxidation relieving haperacidity unit, change into sulfuric acid, still can realize 99.9% sulfur recovery rate.
Owing to do not have the rare gas element of introducing in the hydrogenation process of conventional Claus+tail gas Reducing and absorption technique and the sour gas that after amine absorption regeneration, returns the Crouse unit, therefore, the equipment size of claus reaction device is less more than 10% than conventional Claus+tail gas Reducing and absorption technique.Because poor sour gas does not enter the thermal response processing unit, therefore, the size of thermal response combustion unit and the thermal reactor also Crouse's recovery technology of sulfur than traditional is less.
The utility model technical process is simple, takes up an area littlely, invests lowly, and working cost is low, to Controlling System require low, simple to operate, reliable.
Description of drawings
Fig. 1 is the synoptic diagram of expression the utility model sour gas flare system one embodiment.
Embodiment
Below, by reference to the accompanying drawings the utility model is described in detail.
As shown in Figure 1, among the utility model one embodiment, the sour gas flare system comprises that rich sour gas thermal response processing unit, Crouse's processing unit, Claus tail gases and poor sour gas burn unit, incineration tail gas catalyzed oxidation relieving haperacidity unit, secondary conversion relieving haperacidity unit and exhaust gas reheater unit.In addition, the sour gas flare system also comprises rich sour gas air supply unit, poor sour gas air supply unit and combustion-supporting gas air supply unit.Rich sour gas air supply unit and combustion-supporting gas air supply unit are connected to described rich sour gas thermal response processing unit, and poor sour gas air supply unit is connected in described Claus tail gases and poor sour gas burns the unit.Rich sour gas air supply unit is in order to provide the rich sour gas A of sulfide hydrogen concentration higher (the hydrogen sulfide volumetric concentration is more than 30% usually), poor sour gas air supply unit is used for providing the poor sour gas B of sulfide hydrogen concentration lower (the hydrogen sulfide volumetric concentration is less than 10% usually), and combustion-supporting gas air supply unit is used for providing combustion-supporting gas C.
Rich sour gas thermal response processing unit comprises combustion unit 1, thermal reactor 2, waste heat exchanger 3 and first step sulfur condenser 6.Wherein rich sour gas A and combustion-supporting gas C enter combustion unit 1 and burn, and by controlling the flow of combustion-supporting gas C, guarantee that hydrocarbon polymers all in the feeding gas can fully burn, and the H of control 1/3 under the monitoring of monitoring equipment
2S is oxidized to SO
2Combustion-supporting gas C can be pure oxygen, also can be the air that is provided by air-blaster, or air and pure oxygen mixed oxygen enrichment by a certain percentage.
In thermal reactor 2,1/3 H in the feeding gas
2Sulfurous gas (the SO that S generates by burning
2) and remain 2/3 H
2S reaction generting element sulphur (S
n) and water (vapour phase), the reactive chemistry equation is as follows:
H
2S+3/2O
2---SO
2+H
2O
2H
2S+SO
2---2H
2O+3/nS
n
Waste gas cooling and the generating steam of the waste heat exchanger 3 that directly links to each other with thermal reactor 2 after with the sour gas burning.Be divided into two bursts of logistics from waste heat exchanger 3 waste gas out, namely treat condensation waste gas 4 and thermal bypass gas 5 again.Treat that condensation waste gas 4 enters into first step sulfur condenser 6, be cooled to about 160 ℃, and be divided into two bursts of logistics, be i.e. waste gas 9 after liquid-state sulfur 43 and the one-level condensation; Liquid-state sulfur 43 relies on actions of gravity to flow in the molten sulfur pond 46 and is degassed in the molten sulfur pond, and the molten sulfur 15 after degassed is sent outside, and molten sulfur degasification tail gas 47 delivers to follow-up Claus tail gases and poor sour gas burns cell processing.In first step sulfur condenser 6, also can generate low-pressure steam.The sulfur recovery rate of rich sour gas thermal response processing unit approximately only has 60～70%.
In order to obtain higher sulfur recovery rate, Crouse's processing unit and then after rich sour gas thermal response processing unit.In general in order to reach the requirement of sulfur recovery rate, need to use two-stage even more Crouse's treatment unit.Crouse's processing unit comprises one-level Crouse treatment unit and secondary Crouse treatment unit in the present embodiment.
One-level Crouse's treatment unit comprises claus reaction device 7 and second stage sulfur condenser 8, in claus reaction device 7, activated alumina and titanium deoxide catalyst is housed, under lower temperature, and remaining SO
2And H
2Continue to occur claus reaction between the S.
Use titanium deoxide catalyst can promote COS and CS
2Partial hydrolysis, and then the whole sulfur recovery rate of Crouse part in the raising system.COS and CS
2The hydrolysis reaction formula as follows:
COS+H
2O---H
2S+CO
2
CS
2+2H
2O---2H
2S+CO
2
Enter second stage sulfur condenser 8 from claus reaction device 7 waste gas out, be cooled and be divided into two bursts of logistics, i.e. waste gas 10 behind liquid-state sulfur 44 and the B-grade condensation; Liquid-state sulfur 44 relies on action of gravity to flow in the molten sulfur pond 46.Waste gas 10 enters secondary Crouse treatment unit behind the B-grade condensation.
Secondary Crouse treatment unit comprises Crouse's reheater 11, secondary claus reaction device 12 and third stage sulfur condenser 13, in secondary claus reaction device 12, activated alumina catalyst is housed, under lower temperature, and remaining SO
2And H
2Continue to occur claus reaction between the S.
Waste gas 10 enters secondary claus reaction device 12 behind the B-grade condensation after secondary Crouse reheater 11 is heated to proper temperature, out enter afterwards third stage sulfur condenser 13 from secondary claus reaction device 12, be cooled and be divided into two bursts of logistics, i.e. liquid-state sulfur 45 and Claus tail gases 14; Liquid-state sulfur 45 relies on action of gravity to flow in the molten sulfur pond 46.Claus tail gases 14 enters follow-up Claus tail gases and poor sour gas burns the unit.
Above-mentioned thermal reactor, waste heat exchanger, sulfur condenser, Crouse's reheater, claus reaction device are not particularly limited, and can adopt any same category of device well known in the art.First step sulfur condenser, second stage sulfur condenser and third stage sulfur condenser can share a housing, to reduce gross investment, also can separately build, and this is not particularly limited.
After rich sour gas thermal response processing unit, one-level Crouse's treatment unit, the processing of secondary Crouse treatment unit, sulfur recovery rate can reach 93%～95%.
Claus tail gases and poor sour gas burn the unit and comprise incinerator 16, incinerator waste heat exchanger 17 and fume extractor 20.
Relevant reaction formula is as follows:
H
2S+3/2O
2-->SO
2+H
2O
COS+3/2O
2-->CO
2+SO
2
S+O
2-->SO
2
CO+1/2O
2-->CO
2
All hydro carbons all are oxidized to CO
2
Temperature control in the above-mentioned incinerator realizes by the amount of blasting of regulating combustion air.Simultaneously, the oxygen concentration in the waste gas of incinerator outlet is measured and controlled, be not less than 2% to guarantee oxygen concentration, reach the standard of oxygen-excess combustion.
Only contain SO in the waste gas that produces after burning
2, CO
2And H
2Then O lowers the temperature with 17 heat exchange of incinerator waste heat exchanger.The temperature of the waste gas 18 that flows out from incinerator is reduced to 350～400 degrees centigrade, enters the incineration tail gas catalyzed oxidation relieving haperacidity unit in downstream.Incinerator 16 also is connected with the fuel gas feeding unit, and when follow-up producing acid by oxidation cell failure or maintenance stoppage in transit, incinerator uses fuel gas D heating, and tail gas directly is discharged into atmosphere from bypass F by fume extractor 20, and wherein fume extractor 20 is generally chimney.
Above-mentioned incinerator is not had special restriction, can adopt incinerator well known in the art.Tail gas burning furnace furnace temperature in the Conventional Claus technique is traditionally arranged to be 540～800 ℃, and the incinerator temperature control scope of this technique is about 800～1000 ℃, and simultaneously, incinerator should provide the sufficient residence time, so that can be the H of remnants
2S, COS, CS
2And sulphur burns into SO
2, the incendivity thing other burns into CO such as hydrocarbon polymer, hydrogen and CO
2And water.
If it is very few to advance the poor sour gas of incinerator, when being not enough to still that by the amount of blasting of regulating combustion air temperature maintained 800 ℃, can from the rich sour gas A of charging, shunt a part of sour gas, without rich sour gas thermal response unit and Crouse's processing unit, directly enter incinerator 16.The flow that directly enters the rich sour gas E of incinerator 16 can be regulated by setting device E1, and setting device E1 is variable valve in the present embodiment, and total principle is just to keep the minimum temperature of incinerator when not needing postcombustion gas.Postcombustion gas does not cause water excess in the system except the energy-conservation water that can also prevent that fuel gas when burning from producing.But the maximum that enters total sulfur in the gas of incinerator should limit to some extent, depends on the transformation efficiency of discharge index and follow-up catalyzed oxidation relieving haperacidity unit, for example, if require SO
2Emission concentration is less than 100mg/m
3, the concentration that then enters total sulfur in the gas of incinerator should be not more than 30000ppm.
Under extreme case, very few or concentration is excessively low when the rich sour gas tolerance of charging, when front end Crouse processing unit also is difficult to steady running, can be stopped transport in the Crouse unit, whole rich sour gas are introduced incinerator, in follow-up two-stage catalyzed oxidation relieving haperacidity unit, change into sulfuric acid after the burning, still can realize 99.9% sulfur recovery rate.
Incineration tail gas catalyzed oxidation relieving haperacidity unit comprises convertor 19 and condenser 23.Waste gas 18 enters in the convertor 19, and convertor 19 is comprised of catalyst bed 21 and convertor water cooler 22, and catalyst bed 21 has catalyzer, SO on catalyst bed 21
2Change into SO
3And release reaction heat, convertor interchanger 22 is used for reaction heat is taken out, and plays cooling effect.
The reaction formula of convertor 19 internal reactions is as follows:
SO
2+1/2O
2-->SO
3
SO
3+H
2O-->H
2SO
4
According to the content of sulfurous gas in the waste gas 18, convertor 19 is interior can to arrange multi-layer catalyst bed and convertor interchanger.Catalyzer wherein is not particularly limited, and for example can select Pt or V
2O
5Deng, but preferred honeycomb Pt coated catalysts, it is advantageous that it can move in the temperature range of 250 ° of C to 500 ° of C, higher transformation efficiency is provided, honeycomb structure is conducive to provide larger surface in contact and the less pressure-losses.If use V
2O
5As catalyzer, then the temperature in the convertor should be controlled at 450～550 degrees centigrade.Also without particular determination, can adopt any interchanger well known in the art to above-mentioned convertor interchanger.
Behind the waste gas process convertor 19, SO
2To SO
3Transformation efficiency greatly between 95%-97%.The spent air temperture that flows out from convertor 19 is controlled at about about 280 ° of C, enters subsequently condenser 23; Condenser 23 is by condenser heat exchanger 24,25, and mist eliminator 26 and blower fan 27,28 form.Waste gas temperature after condenser heat exchanger 24 and 25 coolings is down to about 80 ° of C, and sulfuric acid gets off in the upper condensation of the shell side (or tube side) of condenser heat exchanger 24 and 25, flows out afterwards condenser 23 under action of gravity, enters the sulfuric acid storage and handling facility with logistics 42.Residue acid mist in the Process Gas is removed by electrostatic precipitator 26, then enter the tube side (or shell side) of condenser heat exchanger 24 through blower fan 27 pressurizations, and with the hot waste gas heat exchange of shell side (or tube side), to improve heat utilization rate, then enter secondary and transform the relieving haperacidity unit.Condenser heat exchanger 24 adopts cold waste gas and hot waste gas heat exchange to improve heat utilization rate, and condenser heat exchanger 25 used cooling airs are provided by blower fan 28.
Secondary transforms the relieving haperacidity unit and comprises second stage convertor 29 and second stage condenser 33, and the principle that secondary transforms the relieving haperacidity unit is the same with the principle of incineration tail gas catalyzed oxidation relieving haperacidity unit.With unoxidized SO in the incineration tail gas catalyzed oxidation relieving haperacidity unit
2Continue to change into sulfuric acid.
The exhaust gas reheater unit comprises exhaust fan 39 and exhaust gas reheater device 48.After exhaust fan 39 is extracted out, deliver to exhaust gas reheater device 48 from second stage condenser 33 waste gas out, be heated to about 125 ° of C through the exhaust gas reheater device, then be discharged into atmosphere by fume extractor 20.Another effect of exhaust fan 39 is second stage condenser 33 can be maintained negative pressure state, can guarantee that second stage condenser does not have the gas leakage phenomenon and occurs.The exhaust gas reheater device there is not special restriction, can adopt any type of interchanger well known in the art, for example can the multilayer fin be installed in exhaust gas channel, leave the gap between the fin, tail gas can clog-freely pass through, heating medium by fin with tail gas heating.The thermal source of exhaust gas reheater device 48 also comes from incinerator waste heat exchanger 17, also namely by pipeline etc. heat is passed to exhaust gas reheater device 48 by incinerator waste heat exchanger 17, does not need the external complement from system.The purpose of exhaust gas reheater is that the hydrogen sulfide in the rich sour gas can generate the water of equal volume in the claus reaction process, the burnings such as the hydrocarbon polymer in the sour gas, ammonia also can produce water, this causes the content of water in the Claus tail gases usually higher, these water parts in the relieving haperacidity unit with SO
3In conjunction with having generated sulfuric acid, major part is discharged with tail gas, is not discharged into suitable height if be not heated to proper temperature, will cause the lime set of trace acidic impurity in the tail gas that fume extractor is caused corrosion, and perhaps a large amount of lime sets are landed near emission-control equipment.
In secondary transforms the relieving haperacidity unit, residual SO
2To SO
3And then to H
2SO
4The efficient that transforms surpasses 98%, the transformation efficiency in the comprehensive before incineration tail gas catalyzed oxidation relieving haperacidity unit more than 95%, and the two-stage transformation efficiency will be up to 99.9%.
From whole Acidic Gas Treating system, sulfur recovery rate after thermal response processing unit, one-level Crouse's treatment unit and secondary Crouse treatment unit are processed is 93%～95%, and the rate of recovery of sulphur reaches 99.9% in incineration tail gas catalyzed oxidation relieving haperacidity unit and secondary conversion relieving haperacidity unit, the sulfur recovery rate of a whole set of Acidic Gas Treating system can reach more than 99.99%, is discharged into SO in the tail gas of atmosphere
2Concentration＜100mg/m
3, this transformation efficiency and emission concentration can satisfy industry maximum emission limitation standard.
In the system of the present utility model, the poor sour gas of low in hydrogen sulphide concentration does not need the laggard Cross unit of preconcentration concentrate, but directly enter Claus tail gases and poor sour gas incinerator, both provided thermal source for the Claus tail gases incinerator, indirectly improved again the total sour gas concentration that enters the thermal response processing unit, be conducive to improve the transformation efficiency of hydrogen sulfide, guaranteed the steady running of Cross unit.Simultaneously, simplify flow process, saved investment.In addition, because the rich sour gas of the part of poor sour gas and in case of necessity shunting directly enters follow-up relieving haperacidity unit, without the thermal response processing unit, therefore, the size of thermal response combustion unit and thermal reactor is less than traditional Crouse's recovery technology of sulfur.
Owing to do not have the rare gas element of introducing in the hydrogenation process of conventional Claus+tail gas Reducing and absorption technique and the sour gas that after amine absorption regeneration, returns the Crouse unit, therefore, the equipment size of claus reaction device is less in the system of the present utility model, and is less more than 10% than conventional Claus+tail gas Reducing and absorption technique.
Reaction produces in the Acidic Gas Treating of the present utility model system a water part and SO
3In conjunction with having generated sulfuric acid, a part does not have discharging of waste liquid with exhaust emissions.
Technical process is simple, take up an area less than conventional Claus+tail gas Reducing and absorption technique, invest low, to Controlling System require low, simple to operate, reliable.In addition, except the driving stage, system does not need postcombustion gas, and working cost is low.
Below, by test example, further describe present embodiment.
Test example 1
Carry out the sour gas off gas treatment according to following step.
A, raw material sour gas have the sour gas of 3 strands of different concns, and the component of sour gas 1 and character are: H
2S content 37%(V), COS content 4.8% (V), CO
2Content 54.8% (V), N
2Content 3.4% (V), 25 ℃ of temperature, pressure 100Kpa; The component of sour gas 2 and character are: H
2S content 1.9%(V), COS content 0.25% (V), CO
2Content 26.0% (V), CO content 43% (V), H
2Content 24% (V), H
2O content 4% (V), N
2Content 0.75% (V), temperature 60 C, pressure 300KPa; The component of sour gas 3 and character are: H
2S content 5%(V), COS content 0.02% (V), CO
2Content 71.98% (V), CO content 6% (V), H
2Content 5% (V), H
2O content 12% (V), (V) temperature is 55 ℃, pressure 200KPa.
B, sour gas 1 enter the thermal reactor burner, adopt pure oxygen burning, by monitoring H
2S/SO
2Ratio, the flow of control oxygen guarantees that hydrocarbon polymers all in the feeding gas can fully burn, and with 1/3rd H
2S is oxidized to SO
2Waste heat exchanger is cooled to 340 ℃ with process gas, and generates saturated middle pressure steam.
C, enter one-level claus reaction device from a waste heat exchanger waste gas part out, rest part enters into first step sulfur condenser, be cooled to 160 ℃, cooled gas mixes with the waste gas that directly enters one-level claus reaction device without cooling, enters one-level claus reaction device.Liquid-state sulfur in the condensation of first step sulfur condenser enters the molten sulfur storage tank according to liquid level.
About 230 ℃ of the inlet air temperature of d, one-level claus reaction device, about 320 ℃ of reaction bed temperature.Enter into second stage sulfur condenser from one-level claus reaction device Process Gas out, be cooled to 160 ℃, cooled gas is heated to 205 ~ 220 ℃ by interchanger with middle pressure steam, enters secondary claus reaction device.Liquid-state sulfur in second stage sulfur condenser condensation enters the molten sulfur storage tank according to liquid level equally.
About 235 ℃ of the reaction bed temperature of e, secondary claus reaction device.Enter into third stage sulfur condenser from secondary claus reaction device waste gas out, be cooled to 160 ℃, enter the Claus tail gases incinerator.Liquid-state sulfur in the condensation of third stage sulfur condenser enters the molten sulfur storage tank according to liquid level equally.
F, Claus tail gases enter incinerator with the molten sulfur degasification tail gas that sour gas 2, sour gas 3, molten sulfur storage tank come, and with the combustion air burning that is preheating to 220 ℃, the incinerator temperature is controlled at 800～1000 ℃.Combustion air comes from the cooling blower that follow-up secondary transforms the relieving haperacidity unit.Temperature control in the incinerator realizes by the amount of blasting of regulating combustion air, simultaneously, system measures and controls the oxygen concentration in the Process Gas of incinerator outlet, is not less than 2% to guarantee oxygen concentration, if oxygen concentration is excessively low, then improve the amount of blasting of combustion air.When excess Temperature, will blast more combustion air.When normal operation, do not need aftercombustion gas just the temperature of incinerator can be maintained more than 800 ℃.When the poor sour gas underload of incinerator charging, a part of sour gas of shunting without rich sour gas thermal response unit and Crouse's processing unit, directly enters incinerator from sour gas 1, keeps the incinerator temperature more than 800 ℃.
The heat of high-temp waste gas takes out by finned heat exchanger in g, the incinerator, and heat transferring medium adopts hot melt salt.The spent air temperture that flows out from incinerator is reduced to 350～400 ℃, enters one-level catalyzed oxidation convertor.Adopt two-layer catalyzer in this convertor, and an interchanger is set behind every layer of catalyzer, to take out reaction heat, keep the temperature of reaction in the convertor.Catalyzer adopts honeycomb Pt coated catalysts, and interchanger adopts finned heat exchanger, and heat transferring medium adopts hot melt salt.
H, waste gas flow out from one-level catalyzed oxidation convertor, and temperature is controlled at about about 280 ° of C, enters subsequently first-stage condenser; Adopt the Glass tubing interchanger to be cooled to 80 ℃, sulfuric acid flows out from the condenser bottom, and waste gas is removed acid mist with electrostatic precipitator, then with the waste gas heat exchange of the heat that enters first-stage condenser, is heated to 230 ℃, enters the secondary convertor.
Be provided with a heating heat exchanger, one deck catalyzer and a cooling heat exchanger in i, the secondary convertor, then the waste heat that heating heat exchanger uses the incinerator waste heat exchanger will remain SO with waste gas heating to 400 ℃ on catalyzer
2Continue to be oxidized to SO
3, take out reaction heat with cooling heat exchanger, the type in catalyzer and interchanger and the one-level convertor is identical.
J, the spent air temperture that flows out from secondary catalyzed oxidation convertor are controlled at about about 280 ° of C, enter secondary condenser, cool off and demist, and sulfuric acid flows out from the condenser bottom, discharges behind tail gas heating to the 125 ° C.Sulfuric acid concentration is 96%, SO in the emission
2Concentration is 50mg/m
3
By test example 1 as can be known, owing to take two-stage Crouse conversion unit and two-stage catalyzed oxidation relieving haperacidity unit, the sulfur recovery rate of a whole set of Acidic Gas Treating system reaches more than 99.99%, is discharged into SO in the tail gas of atmosphere
2Concentration＜100mg/m
3
And, the poor sour gas of low in hydrogen sulphide concentration in the feeding gas, do not need the preconcentration concentrate, directly enter catalyzed oxidation relieving haperacidity unit, both for the Claus tail gases incinerator provides thermal source, indirectly improved again the total sour gas concentration that enters the thermal response processing unit, be conducive to improve the transformation efficiency of hydrogen sulfide, guarantee the steady running of Crouse unit, simultaneously, simplified flow process.
Although described the utility model with reference to several exemplary embodiments, should be appreciated that used term is explanation and exemplary and nonrestrictive term.Because the utility model is implementation and do not break away from spirit of the present utility model or essence in a variety of forms, so be to be understood that, above-described embodiment is not limited to any aforesaid details, and should be in the spirit and scope that claims limit explain widely, therefore fall into whole variations in claim or its equivalent scope and remodeling and all should be claims and contain.
Claims (9)
1. a sour gas flare system is characterized in that, comprising:
Rich sour gas air supply unit is used for providing rich sour gas;
Combustion-supporting gas air supply unit is used for providing combustion-supporting gas (C);
Poor sour gas air supply unit is used for providing poor sour gas (B);
Rich sour gas thermal response processing unit, be connected in the downstream of described rich sour gas air supply unit and described combustion-supporting gas air supply unit, be used for carrying out the desulfurization processing by the combustion-supporting described rich sour gas (A) that will pass into described rich sour gas thermal response processing unit of described combustion-supporting gas (C);
Crouse's processing unit is connected in the downstream of described rich sour gas thermal response processing unit, and the gas after being used for described rich sour gas thermal response processing unit desulfurization processed further carries out desulfurization and processes and produce Claus tail gases (14);
Claus tail gases and poor sour gas burn the unit, be connected in the downstream of described Crouse's processing unit and the downstream of described poor sour gas air supply unit, be used for burning the molten sulfur degasification tail gas (47) that produces after described poor sour gas (B), described Claus tail gases (14) and the described rich sour gas thermal response processing unit of process and the described Crouse's processing unit desulfurization processing and producing waste gas from incinerator (18);
Incineration tail gas catalyzed oxidation relieving haperacidity unit is connected in the downstream that described Claus tail gases and poor sour gas burn the unit, is used for the SO with described waste gas from incinerator (18)
2Change into SO
3, and be combined with water and be condensed into sulfuric acid;
Secondary transforms the relieving haperacidity unit, is connected in the downstream of described incineration tail gas catalyzed oxidation relieving haperacidity unit, is used for further with SO
2Change into SO
3, and be combined with water and be condensed into sulfuric acid; And
The exhaust gas reheater unit is connected in the downstream that described secondary transforms the relieving haperacidity unit, is used for described secondary is transformed the waste gas heating that the relieving haperacidity unit produces;
Described rich sour gas air supply unit and described Claus tail gases and poor sour gas burn between the unit and are provided with: can make at least part of described rich sour gas enter described Claus tail gases and poor sour gas burns the connection line of unit, and the flow regulation device (E1) that is used for regulating described rich sour gas (E) flow of described connection line.
2. sour gas flare system as claimed in claim 1 is characterized in that, described rich sour gas thermal response processing unit comprises for the H with described rich sour gas (A) 1/3rd
2S burns into SO
2Combustion unit (1), the SO that generates for described burning
2With remaining described H
2S reacts thermal reactor (2), the waste heat exchanger (3) that is used for heat exchange that generates sulphur and the first step sulfur condenser (6) that is used for condensation sulphur therein.
3. sour gas flare system as claimed in claim 2 is characterized in that, described Crouse's processing unit comprises one-level Crouse treatment unit and secondary Crouse treatment unit, and described one-level Crouse's treatment unit comprises makes remaining SO
2And H
2Claus reaction occurs with the one-level claus reaction device (7) that generates sulphur and is used for the second stage sulfur condenser (8) of the sulphur that the described one-level claus reaction of condensation device (7) produces in S, is used to described one-level claus reaction device (7) that heat is provided from the again thermal bypass gas (5) of the described waste heat exchanger (3) of described rich sour gas thermal response processing unit.
4. sour gas flare system as claimed in claim 3 is characterized in that, described secondary Crouse treatment unit comprises to be made through remaining SO after described one-level Crouse's treatment unit
2And H
2Continue to occur between the S claus reaction with the secondary claus reaction device (12) that generates sulphur, be used to described secondary claus reaction device (12) that Crouse's reheater (11) of heat is provided and be used for the third stage sulfur condenser (13) of the sulphur that the described secondary claus reaction of condensation device (12) produces.
5. sour gas flare system as claimed in claim 4, it is characterized in that described Claus tail gases and poor sour gas burn the unit and comprise be used to the incinerator (16) that burns described Claus tail gases (14), described poor sour gas (B) and described molten sulfur degasification tail gas (47), be used for burning the SO of rear generation
2, CO
2And H
2O carries out the incinerator waste heat exchanger (17) of heat exchange cooling and is used for the fume extractor (20) of combustion gas.
6. sour gas flare system as claimed in claim 5 is characterized in that, described incineration tail gas catalyzed oxidation relieving haperacidity unit comprises the SO in the waste gas from incinerator (18) that described incinerator (16) is produced
2Change into SO
3And be combined into the first step convertor (19) of sulfuric acid with water and with the first step condenser (23) of described condensation of sulfuric acid.
7. sour gas flare system as claimed in claim 6 is characterized in that, described secondary conversion relieving haperacidity unit comprises further will be from the SO of described first step condenser (23)
2Change into SO
3And be combined into the second stage convertor (29) of sulfuric acid with water and with the second stage condenser (33) of described condensation of sulfuric acid.
8. sour gas flare system as claimed in claim 7, it is characterized in that, described second stage convertor (29) also comprises second stage convertor well heater (30), and described incinerator waste heat exchanger (17) is passed to described second stage convertor well heater (30) with heat.
9. sour gas flare system as claimed in claim 8 is characterized in that, described exhaust gas reheater unit comprises the exhaust fan (39) for delivery of tail gas and is used for exhaust gas reheater device (48) with tail gas heating.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220564443 CN202864918U (en) | 2012-10-30 | 2012-10-30 | Waste gas treatment system of acid gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220564443 CN202864918U (en) | 2012-10-30 | 2012-10-30 | Waste gas treatment system of acid gas |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102910593A (en) * | 2012-10-30 | 2013-02-06 | 美景（北京）环保科技有限公司 | System and method for treating waste acid gas |
| CN108298505A (en) * | 2018-01-29 | 2018-07-20 | 华陆工程科技有限责任公司 | Processing contains H2The process integration of S sour gas while extracting sulfuric acid and sulphur |
| CN110713175A (en) * | 2019-10-17 | 2020-01-21 | 山西潞安煤基清洁能源有限责任公司 | Method and device for improving sulfur recovery efficiency |
| CN113697774A (en) * | 2021-09-17 | 2021-11-26 | 洛阳瑞昌环境工程有限公司 | Ultra-low load sulfur recovery system and process |
-
2012
- 2012-10-30 CN CN 201220564443 patent/CN202864918U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102910593A (en) * | 2012-10-30 | 2013-02-06 | 美景（北京）环保科技有限公司 | System and method for treating waste acid gas |
| CN108298505A (en) * | 2018-01-29 | 2018-07-20 | 华陆工程科技有限责任公司 | Processing contains H2The process integration of S sour gas while extracting sulfuric acid and sulphur |
| CN108298505B (en) * | 2018-01-29 | 2021-07-06 | 华陆工程科技有限责任公司 | Treatment of a gas containing H2Combined process for preparing sulfuric acid and sulfur simultaneously from S acid gas |
| CN110713175A (en) * | 2019-10-17 | 2020-01-21 | 山西潞安煤基清洁能源有限责任公司 | Method and device for improving sulfur recovery efficiency |
| CN113697774A (en) * | 2021-09-17 | 2021-11-26 | 洛阳瑞昌环境工程有限公司 | Ultra-low load sulfur recovery system and process |
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