CN202844880U - Processing system for removing hydrogen sulfide from acidic gas - Google Patents
Processing system for removing hydrogen sulfide from acidic gas Download PDFInfo
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- CN202844880U CN202844880U CN 201220505813 CN201220505813U CN202844880U CN 202844880 U CN202844880 U CN 202844880U CN 201220505813 CN201220505813 CN 201220505813 CN 201220505813 U CN201220505813 U CN 201220505813U CN 202844880 U CN202844880 U CN 202844880U
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Abstract
The utility model relates to a processing system for removing hydrogen sulfide from acidic gas. The processing system comprises an absorption reaction unit, a sulfur filtering unit, a solution regeneration unit, a temperature control unit and a medicament conveying unit, wherein the absorption reaction unit comprises a chelated iron catalyst desulfurization solution which is used for absorbing the hydrogen sulfide in the acidic gas introduced into the absorption reaction unit and oxidizing the hydrogen sulfide to obtain elemental sulfur; the sulfur filtering unit is used for filtering out the elemental sulfur; and the solution regeneration unit is connected with the sulfur filtering unit and used for performing oxidation regeneration on the chelated iron catalyst desulfurization solution after filtration, wherein the sulfur filtering unit is positioned between the absorption reaction unit and the solution regeneration unit. The processing system disclosed by the utility model can prevent the elemental sulfur from being settled at the bottom end of an oxidation regenerator, realize low sulfur concentration in the system, operate stably for a long time and realize good operation elasticity under various working conditions by filtering out the elemental sulfur from the solution before the oxidation regeneration step. The structure of equipment can be simplified, and the investment and construction periods can be reduced.
Description
Technical field
The utility model relates to a kind of gas handling system, relates in particular to a kind of acid gas removal hydrogen sulfide treatment system.
Background technology
In the industrial gasses such as petrochemical industry, natural gas, oil field development, coke-stove gas and semiwater gas, hydrogen sulfide is a kind of very harmful impurity.Its existence not only can cause equipment and corrosion of piping, and can bring quite serious harm to environment, belongs to the pollutant that must eliminate or control.
In hydrogen sulfide stripping technique, large-scale desulphurization system, for example the system of elemental sulfur output more than 5000 ton/years generally adopts CLAUS technique; Most widely used for small-sized desulphurization system is following two kinds of wet method catalytic oxidation techniques, 1) and Complexing Iron catalyst absorbent solution; 2) vanadium metal catalyst absorbent solution.In addition, in addition sulfide (is comprised hydrogen sulfide, SO
2, organic sulfur etc.) all be oxidized to SO
3And the technique of extracting sulfuric acid, sulfide acid-making process applied range, desulfuration efficiency is high, operating cost is low, good in economic efficiency, but owing to relating to management and the cost of transportation of hazardous chemical, generally be applied in the occasion that the sulfuric acid demand is arranged in device scene or the economic radius.
In small-scale sulfur removal technology, complex iron is a kind of hydrogen sulfide that removes from air-flow, be the sulfur removal technology of sulphur with Oxidation of Hydrogen Sulfide, since 20 century 70s begin abroad commercial Application, so far have the history of decades, in common knowledge for everybody, have technique simple, the desulfuration efficiency advantages of higher.
Complex iron uses liquid Complexing Iron catalyst solution, and this solution contacts with the air-flow that comprises hydrogen sulfide, and Oxidation of Hydrogen Sulfide is become elemental sulfur, simultaneously, and the Fe in the Complexing Iron catalyst solution
3+Be reduced into Fe
2+, then, with the gas that contains oxygen, generally be air, with Fe
2+Be oxidized to Fe
3+After reuse.At H
2The key reaction equation is as follows in the absorption process of S:
H
2The S(gaseous state)+H
2O (liquid)=H
2S (liquid state)+H
2O (liquid)
H
2S (liquid state)=H
++ HS
-
HS-=H
++S
2-
HS
-+2Fe
3+--H
++S+2Fe
2+
S
2-+2Fe
3+--H
++S+2Fe
2+
These equations merge, and the result is:
H
2The S(gaseous state)+2Fe
3+--2H
++ S+2Fe
2+
At Fe
2+Oxidative regeneration process in, the key reaction equation is as follows:
O
2(gaseous state)+H
2O (liquid)=O
2(liquid state)+H
2O (liquid)
O
2(liquid state)+2H
2O+4Fe
2+--4OH
-+ 4Fe
3+
These equations merge, and the result is:
O
2(gaseous state)+H
2O+2Fe
2+--2OH
-+ 2Fe
3+
Aspect abroad, 20 century 70s, U.S. air resource company takes the lead in having developed the complex iron technique LO-CAT based on the EDTA association complex, and desulfuration efficiency can be up to 99.99%.And begin commercial Application in the eighties in 20th century.At the beginning of the nineties, air resource company has further released self-loopa LO-CAT II technique.
Aspect at home, in recent years, along with raising and industrial expansion that domestic desulfurization requires, the demand of small-sized sulfur recovery increased rapidly, and the LO-CAT technique that is suitable on a small scale sulfur recovery progressively is applied at home.Domestic complex iron is taken off H
2S has carried out for many years research, studies several different methods, but these method and technology poor reliability or economic feasibility are poor and fail commercial Application basically.At home, patent CN1354038 is studied the process conditions of complex iron, according to different unstripped gas, has proposed different desulfurizing agent composition and proportioning, and different gas treatment modes, and improves the equipment corrosion situation by adding corrosion inhibiter.In addition, the user of domestic indivedual LO-CAT techniques has carried out production domesticization to the used import catalyst of LO-CAT system and has substituted exploitation in order to reduce cost.
In existing complex iron common process, hydrogen sulfide containing gas absorbs in absorber, then, has absorbed H
2The solution of S is all delivered to oxidizing chamber and is carried out oxidation regeneration, the elemental sulfur that generates in the technical process is in the cone sedimentation of oxidizing chamber bottom, elemental sulfur after the sedimentation filters, because the elemental sulfur of cone is dense, the elemental sulfur that can prevent cone even take measures stops up because of long-time deposition, but still easily cause the obstruction of equipment and pipeline, and additionally increased complexity and the investment of technique.In order to make elemental sulfur need to keep certain density elemental sulfur concentration in the whole desulphurization system in the cone base sedimentation, in order to form larger drusen.Also need in system, add the surfactant of capacity, prevent elemental sulfur sedimentation separation difficulty.
In existing complex iron self-loopa technique, there is following shortcoming:
1. device structure is complicated, invests highly, and the design-and-build cycle is long;
2. the circulation rate of solution is set by the initial physical dimension of self-loopa reactor, during operation can not be measured, can not be controlled;
3. although in theory self-loopa technique can be moved under 0 ~ 100% load, but, because self-circulation system need to utilize the lifting of sour gas and air to come the circulation of solution in the realization response device, therefore, low or because the low air capacity that causes needs of the load of hydrogen sulfide when hanging down when acid tolerance, solution just can't form self-loopa, and system can't be moved.And if continue to keep high air capacity this moment, will cause again the over oxidation of catalyst and hydrogen sulfide, thereby also will affect the operation of system, so operating flexibility in actual applications is much smaller.Can not give full play to the large advantage of complex iron depriving hydrogen sulphide technological operation elasticity.
Summary of the invention
In view of the problems referred to above that exist in the present both at home and abroad complex iron depriving hydrogen sulphide technique, the purpose of this utility model is, a kind for the treatment of system that can effectively remove the hydrogen sulfide in the sour gas is provided, treatment system of the present utility model can satisfy discharge standard, system can steady in a long-term be moved, and system all have excellent operation elasticity under various operating modes.
For achieving the above object, the utility model proposes a kind of acid gas removal hydrogen sulfide treatment system, comprise absorption reaction unit, sulfur filtration unit, regeneration of waste liquor unit, temperature control unit and drug delivery unit, described absorption reaction unit has Complexing Iron catalyst desulfurizing solution, is used for absorbing passing into the hydrogen sulfide of sour gas wherein and being oxidized into elemental sulfur; Described sulfur filtration unit is connected in described absorption reaction unit, for the described Complexing Iron catalyst desulfurizing solution behind the filtration absorbing hydrogen sulphide, so that described elemental sulfur is filtered out; Described regeneration of waste liquor unit is connected in described sulfur filtration unit, is used for carrying out oxidation regeneration through the described Complexing Iron catalyst desulfurizing solution after filtering; Described drug delivery unit is connected in described absorption reaction unit, and to described absorption reaction unit, described temperature control unit is used for keeping the reaction temperature of described treatment system for delivery of the required medicament of described treatment system; Wherein, described sulfur filtration unit is between described absorption reaction unit and described regeneration of waste liquor unit, and the described Complexing Iron catalyst desulfurizing solution after the process filtration is back in the described absorption reaction unit.
In the utility model one embodiment, described absorption reaction unit comprises absorption reactor thermally, described sour gas passes into described absorption reactor thermally and described Complexing Iron catalyst desulfurizing solution reaction, reacted described Complexing Iron catalyst desulfurizing solution splits into solution to be filtered and circulation solution, described solution to be filtered passes into described sulfur filtration unit to filter out described elemental sulfur, described circulation solution loops back in the described absorption reactor thermally, and the flow of wherein said solution to be filtered can be regulated by adjusting device.
In the utility model one embodiment, described absorption reactor thermally has the sour gas distributor, and setting has reaction zone in described absorption reactor thermally bottom, and described sour gas distributor is positioned at the top of described reaction zone.
In the utility model one embodiment, described regeneration of waste liquor unit comprises oxidation regeneration device and apparatus of oxygen supply, and described oxidation regeneration device is the vertical flat-bottom tank structure.
In the utility model one embodiment, be provided with air sparger on the base plate of described oxidation regeneration device.
In the utility model one embodiment, described apparatus of oxygen supply is air blast.
In the utility model one embodiment, described oxidation regeneration device can be with the Fe in the described filtrate after filtering
2+Be oxidized to Fe
3+
In the utility model one embodiment, described treatment system also comprises the waste gas pretreatment unit, described waste gas pretreatment unit is connected in described absorption reaction unit, and described waste gas pretreatment unit carries out after the preliminary purification described sour gas being passed into described absorption reaction unit to described sour gas.
In the utility model one embodiment, described treatment system also comprises tail gas treating unit, the described Complexing Iron catalyst desulfurizing solution that described tail gas treating unit is carried secretly for the tail gas of removing the generation of described absorption reaction unit and described regeneration of waste liquor unit.
In the utility model one embodiment, described temperature control unit is solution heat exchanger, and described solution heat exchanger is connected in described absorption reaction unit and described regeneration of waste liquor unit.
The utility model filters out elemental sulfur before the step of oxidation regeneration by taking from solution, elemental sulfur can not be deposited on the bottom of oxidation regeneration device, sulphur concentration is low in the system, system can steady in a long-term be moved, and all have excellent operation elasticity under various operating modes.And can the simplified apparatus structure, reduce investment outlay and the construction period.
Description of drawings
Fig. 1 is the schematic diagram of the acid gas removal hydrogen sulfide treatment system of the utility model one embodiment.
The specific embodiment
Fig. 1 is the schematic diagram of the acid gas removal hydrogen sulfide treatment system of the utility model one embodiment.As shown in Figure 1, among the utility model one embodiment, acid gas removal hydrogen sulfide treatment system comprises waste gas pretreatment unit, absorption reaction unit, sulfur filtration unit, regeneration of waste liquor unit, temperature control unit, drug delivery unit and tail gas treating unit.
The waste gas pretreatment unit is used for the sour gas that passes into is carried out preliminary treatment to remove impurity; The absorption reaction unit has Complexing Iron catalyst desulfurizing solution, be used for passing into wherein sour gas in hydrogen sulfide absorption and be oxidized into elemental sulfur; The elemental sulfur that the sulfur filtration unit is used for oxidation is formed filters; The Complexing Iron catalyst desulfurizing solution that the regeneration of waste liquor unit is used for will participating in reacting carries out oxidation regeneration; The drug delivery unit for delivery of the required medicament for the treatment of system to the absorption reaction unit; Temperature control unit is used for keeping the reaction temperature for the treatment of system; Tail gas treating unit is used for the catalyst solution of the tail gas of removal absorption reaction unit and the generation of regeneration of waste liquor unit.Below be introduced respectively with regard to above-mentioned each unit.
In one embodiment, the waste gas pretreatment unit comprises that sour gas divides flow container 1, and the inlet channel for the treatment of system is communicated in acid gas-liquid separatory tank 1.Sour gas divides flow container 1 with removals such as the trace acidic drop carried secretly in the sour gas that passes into wherein, oil, hydro carbons, to carry out preliminary purification to sour gas.Sour gas divides flow container 1 can adopt the normally used minute flow container in this area, the utility model is particular determination not, and for example, acid gas-liquid separatory tank can adopt vertical, acid gas-liquid separatory tank top can arrange this area demister commonly used, for separating of the drop of carrying secretly in the sour gas.If the use demister need to arrange necessary water flushing facility equally.
It should be noted that if sour gas is comparatively pure, contained acid drop, oil, hydro carbons etc. are less, then can not carry out preliminary purification, also are that this treatment system can not arrange the waste gas pretreatment unit.
Hydrogen sulfide containing sour gas is divided into two bursts of logistics after sour gas divides flow container 1, minute flow container lime set 3 and the sour gas logistics 2 from dividing flow container top to discharge that namely divide flow container 1 bottom to discharge from sour gas.Divide flow container lime set 3 to be discharged into the local further processing of external security.And sour gas logistics 2 enters follow-up processing flow.
The absorption reaction unit comprises absorption reactor thermally 4.Absorption reactor thermally 4 is connected with acid gas-liquid separatory tank 1.Has Complexing Iron catalyst desulfurizing solution in the absorption reactor thermally 4.Sour gas passes in the absorption reactor thermally 4 and contacts with Complexing Iron catalyst desulfurizing solution, and the hydrogen sulfide (H in the sour gas
2S) be desulfurized solution absorption, and further by the ferric ion (Fe in the solution
3+) be oxidized to elemental sulfur (S).In the present embodiment, to pass in the reacting sucting collector 4 through the sour gas logistics 2 that acid gas-liquid separatory tank 1 separates, the appropriate location arranges sour gas distributor (not shown) in absorption reactor thermally 4, the sour gas distributor can make sour gas logistics 2 become less bubble evenly to distribute, and contacts with the Complexing Iron catalyst desulfurizing solution of reverse flow in absorption reactor thermally 4.Hydrogen sulfide in the sour gas logistics 2 is desulfurized solution absorption, and further is desulfurized the ferric ion (Fe in the solution
3+) be oxidized to elemental sulfur.Above-mentioned sour gas distributor does not have special restriction, can adopt sour gas distributor well known in the art, only needs and sour gas logistics 2 homogenising that pass into can be got final product.The emission concentration of hydrogen sulfide that allow after according to the concentration of hydrogen sulfide in the sour gas logistics 2 and absorption reaction the time of contact of sour gas logistics 2 and Complexing Iron catalyst desulfurizing solution is determined.The preferred bubble towers that adopt of absorption reactor thermally 4 should have certain volume space as reaction zone in the bottom of sour gas distributor, so that the HS that forms when making hydrogen sulfide be dissolved in the aqueous solution
-And S
2-Ion can with Complexing Iron catalyst desulfurizing solution in Fe
3+Fully reaction forms elemental sulfur.The time of staying of Complexing Iron catalyst desulfurizing solution in reaction zone is preferably 10 ~ 60 seconds.Absorption reactor thermally tail gas 5 after absorption reactor thermally 4 removes hydrogen sulfide enters follow-up processing flow.In the utility model embodiment, absorption reactor thermally tail gas 5 enters absorption reactor thermally tail gas water washing tank 6, in the absorption reactor thermally tail gas water washing tank 6 water 6a is housed, utilize washing to remove a small amount of catalyst solution drop and the sulfur granules of carrying secretly in the absorption reactor thermally tail gas 5, with the loss of minimizing catalyst, and prevent that the Complexing Iron catalyst solution is to the corrosion of downstream line and equipment.Comprise two bursts of logistics, i.e. discharging waste gas 7 and tail gas water washing tank raffinate 25 from what absorption reactor thermally tail gas water washing tank 6 was discharged.Hydrogen sulfide in the discharging waste gas 7 reaches discharge standard, directly is emitted in the air or again discharging after downstream unit is further processed other impurity.Tail gas water washing tank raffinate 25 turns back to absorption reactor thermally 4 to be continued to use.
After Complexing Iron catalyst desulfurizing solution in the absorption reactor thermally 4 and the sour gas reaction, reaction solution 8 flows out from absorption reactor thermally 4 bottoms, is divided into two bursts of logistics after pump 9 pressurizations, i.e. solution 10 to be filtered and circulation solution 11.Solution 10 to be filtered passes in the follow-up sulphur filter element, and circulation solution 11 is back in the absorption reactor thermally 4.The sulfur filtration unit comprises sulphur filter 12, and solution 10 to be filtered passes into sulphur filter 12 and filters, and wherein elemental sulfur is separated with other components.The flow of solution 10 to be filtered can be regulated by adjusting device, and adjusting device 10a is control valve in the present embodiment, and this flow is determined according to concentration and the hydrogen sulfide content in the sulfide hydrogen sour gas of the elemental sulfur in the reaction solution 8.The elemental sulfur that guarantee to need filters is less than the peak load of sulphur filter 12, and guarantees simultaneously to return the Fe that capacity is arranged in the solution 20 after the circulation solution 11 of absorption reactor thermally 4 and the regeneration
3+
The regeneration of waste liquor unit comprises oxidation regeneration device 16 and apparatus of oxygen supply.Apparatus of oxygen supply is air blast 17 in the present embodiment.Filtrate 13 enters in the oxidation regeneration device 16, adopts air that filtrate 13 is carried out oxidation regeneration in oxidation regeneration device 16, with the Fe in the filtrate 13
2+Be oxidized to Fe
3+In filter process, need regularly to use backwash logistics 15 blowbacks, to keep the stable operation of sulphur filter 14.Wherein backwash logistics 15 can be for filtering rear solution.Above-mentioned sulphur filter 14 is not particularly limited, and can adopt sulphur filter well known in the art, preferably adopts membrane filter, and filtering accuracy is preferably 1 ~ 2mm.Air blast 17 is for the preparation of regeneration air 18.Except using air blast 17 preparation regeneration airs 18, also can adopt other available oxygen-containing gas to Fe
2+Carry out oxidation.Because elemental sulfur need to be in the 16 interior sedimentations of oxidation regeneration device, therefore, above-mentioned oxidation regeneration device 16 does not need to adopt conical vessel as prior art, the equipment that prevents that elemental sulfur from stopping up need to be set in inside yet, but preferably adopt the vertical flat-bottom storage tank, at storage tank bottom plate the air sparger (not shown) is set, air or other oxygen-containing gas form micro air bubble by air sparger, to improve the contact area of air and solution.The form of above-mentioned air sparger is not particularly limited, so long as the air homogenising can be got final product with the contact area that improves air and solution, can adopt air sparger well known in the art.
Temperature control unit comprises solution heat exchanger 21, is that solution heats or cools off with regenerating afterwards to circulation solution by heating or cooling medium, to keep the unit of reaction temperature.In the present embodiment, solution heat exchanger 21 is connected in absorption reactor thermally 4 and oxidation regeneration device 16, to keep the reaction temperature in absorption reactor thermally 4 and the oxidation regeneration device 16.
Tail gas treating unit comprises absorption reactor thermally tail gas water washing tank 6 and oxidation regeneration device tail gas water washing tank 23, be that the oxidation regeneration device tail gas 22 that absorption reactor thermally tail gas 5 and the oxidation regeneration device 16 of absorption reactor thermally 4 discharges are discharged is washed, remove the catalyst solution of carrying secretly in the tail gas.
Absorption reactor thermally tail gas 5 enters absorption reactor thermally tail gas water washing tank 6, utilize washing to remove a small amount of catalyst solution drop and the sulfur granules of carrying secretly in the absorption reactor thermally tail gas 5, with the loss of minimizing catalyst, and prevent that the Complexing Iron catalyst solution is to the corrosion of downstream line and equipment.The two bursts of logistics that comprise from 6 discharges of absorption reactor thermally tail gas water washing tank, be discharging waste gas 7 and tail gas water washing tank raffinate 25, hydrogen sulfide in the discharging waste gas 7 reaches discharge standard, directly is emitted in the air or again discharging after downstream unit is further processed other impurity.Tail gas water washing tank raffinate 25 turns back to absorption reactor thermally 4 to be continued to use.Oxidation regeneration device tail gas 22 enters oxidation regeneration device tail gas water washing tank 23, oxidation regeneration device tail gas water washing tank 23 is equipped with water 23a, utilize washing to remove a small amount of catalyst solution drop and the sulfur granules of carrying secretly in the oxidation regeneration device tail gas 22, with the loss of minimizing catalyst, and prevent that the Complexing Iron catalyst solution is to the corrosion of downstream line and equipment.Comprise two bursts of logistics from what oxidation regeneration device tail gas water washing tank 23 was discharged, i.e. discharging waste gas 24 and tail gas water washing tank raffinate 32, hydrogen sulfide content satisfies discharge standard in the discharging waste gas 24, directly emptying or discharge after downstream unit is further processed other impurity.Tail gas water washing tank raffinate 32 turns back to absorption reactor thermally 4 to be continued to use.
In above-mentioned tail gas treating unit, if absorption reactor thermally tail gas 5 is the same with the subsequent treatment mode of oxidation regeneration device tail gas 22, then absorption reactor thermally tail gas water washing tank 23 can be merged into one with oxidation regeneration device tail gas water washing tank 6.In other embodiments, if absorption reactor thermally tail gas 5 and oxidation regeneration device tail gas 22 are enough pure, then this treatment system does not need to arrange tail gas treating unit.
The drug delivery unit comprises medicament storage tank 26,27,28 and delivery pump 29,30,31, is that the required medicament of system is stored and is transported in the absorption reactor thermally 4.Required medicament comprises iron catalyst, complexing agent, pH value conditioning agent etc. in the course of reaction, and these several medicaments adopt storage tank 26 ~ 28 to store, and are transported to absorption reactor thermally by pump 29 ~ 31.The effect of iron catalyst is to provide Fe for system
3+, the effect of complexing agent is and Fe
3+ form complex compound, form precipitation to prevent it, the effect of pH value conditioning agent is to keep suitable pH value in system.As everyone knows, the absorption rate of hydrogen sulfide in solution significantly descends with the reduction of PH, and remove in the process of hydrogen sulfide at complex iron, be accompanied by the formation of the water soluble salt of accessory substance sulphur and oxygen, pH value is tending towards descending, therefore, need regularly to add alkali, to keep the absorption efficiency of pH value to obtain of appropriateness.The preferable range of pH value is 7.0 ~ 9.5, more preferably 7.5 ~ 8.5.Kind to above-mentioned iron catalyst, complexing agent, PH conditioning agent does not have special restriction, for example can adopt the EDTA-molysite as iron catalyst, adopt aminocarboxylic acids complexing agent, as complexing agent, adopt KOH, NaOH, NH3 as the pH value conditioning agent such as NTA, EDTA etc.
Below by a test case, further describe present embodiment.
Test 1
Carry out the sulfide hydrogen Acidic Gas Treating according to following step.
A, raw material sour gas are transported to system by exterior tubing, enter sour gas and divide flow container after temperature, pressure, flow measurement, the temperature 45 C of sour gas, flow 800Nm3/h, pressure 70KPa, H
2S content 15.5% (V), NH3 content 10.5%(V), CO
2Content 4%(V), other component is N
2And water.It is vertical that sour gas divides flow container, and demister is established on top, and demister is with a small amount of fresh water periodic flushing.Sour gas divides the lime set Closed Drain of flow container to process to the sewage-farm, and the sour gas logistics enters absorption reactor thermally and processes.
B, absorption reactor thermally adopt bubble tower, 4 meters of diameters, and 10 meters of height, wherein the sour gas distributor is positioned at above 2 meters, bottom, and liquid level is 6 meters in the absorption reactor thermally.Fe in the solution
3+Concentration 1000ppm, complexing agent adopts NTA, reaction solution pH value 8 ~ 9.
C, solution circulation flow 650m
3/ h.Adopt 90 ℃ of hot water heatings, keep 48 ℃ of system temperatures.
D, employing membrane filter filter reaction solution, filtering accuracy 1mm, the elemental sulfur slurries sulfur content 10 ~ 20%(W/V) that filter is discharged.
E, oxidation regeneration device adopt the vertical flat-bottom tank, and the bottom arranges the diaphragm-type air compartment system, 6 meters of oxidation regeneration device diameters, the air that oxidation regeneration adopts air blast to provide, air mass flow 3800m
3/ h, blower air quantity adopts variable frequency adjustment.The deposition that in the oxidation regeneration device, does not have elemental sulfur.
The tail gas of f, absorption reactor thermally and oxidation regeneration device is sent into the tail gas water washing tank together, the raffinate of tail gas water washing tank turns back to absorption reactor thermally, the emission of tail gas water washing tank adopts the method for GB/T14678-93 defined to measure, hydrogen sulfide content in the emission is 3 ~ 8ppm, meet discharge standard, owing to containing ammonia in the tail gas, discharge after delivering to follow-up burning disposal.
Seen from the above description, the utility model filters out elemental sulfur before the step of oxidation regeneration by taking from solution, and elemental sulfur can not be deposited on the bottom of oxidation regeneration device, and the oxidation regeneration device only need to adopt common flat tank structure.Simultaneously, because elemental sulfur concentration is low in the system, can not stop up the system that guaranteed operation steady in a long-term.
And, because passing into the flow of the solution to be filtered of sulfur filtration unit can regulate, according to the hydrogen sulfide content in the charging sour gas and the elemental sulfur content in the reaction solution, adjusting is transported to that the sulfur filtration unit filters and the flow of the reaction solution of follow-up oxidation regeneration in-situ regeneration, satisfied the operating flexibility under the various operating modes, guaranteed the regeneration of solution, and remaining solution circulation resorption is received reactor continuation absorption, both guarantee assimilation effect, also saved energy consumption.Concentration of hydrogen sulfide reaches discharge standard in the gas after the processing.
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 (8)
1. acid gas removal hydrogen sulfide treatment system, it is characterized in that, comprise absorption reaction unit, sulfur filtration unit, regeneration of waste liquor unit, temperature control unit and drug delivery unit, described absorption reaction unit has Complexing Iron catalyst desulfurizing solution, is used for absorbing passing into the hydrogen sulfide of sour gas wherein and being oxidized into elemental sulfur; Described sulfur filtration unit is connected in described absorption reaction unit, for the described Complexing Iron catalyst desulfurizing solution behind the filtration absorbing hydrogen sulphide, so that described elemental sulfur is filtered out; Described regeneration of waste liquor unit is connected in described sulfur filtration unit, is used for carrying out oxidation regeneration through the described Complexing Iron catalyst desulfurizing solution after filtering; Described drug delivery unit is connected in described absorption reaction unit, for delivery of the required medicament of described treatment system to described absorption reaction unit; Described temperature control unit is used for keeping the reaction temperature of described treatment system; Wherein, described sulfur filtration unit is between described absorption reaction unit and described regeneration of waste liquor unit, and the described Complexing Iron catalyst desulfurizing solution after the process filtration is back in the described absorption reaction unit.
2. acid gas removal hydrogen sulfide treatment as claimed in claim 1 system, it is characterized in that, described absorption reaction unit comprises absorption reactor thermally (4), described sour gas passes into described absorption reactor thermally (4) and described Complexing Iron catalyst desulfurizing solution reaction, reacted described Complexing Iron catalyst desulfurizing solution splits into solution to be filtered (10) and circulation solution (11), described solution to be filtered (10) passes into described sulfur filtration unit to filter out described elemental sulfur, described circulation solution (11) loops back in the described absorption reactor thermally (4), and the flow of wherein said solution to be filtered can pass through adjusting device (10a) to be regulated.
3. acid gas removal hydrogen sulfide treatment as claimed in claim 2 system, it is characterized in that, described absorption reactor thermally (4) has the sour gas distributor, and setting has reaction zone in described absorption reactor thermally (4) bottom, and described sour gas distributor is positioned at the top of described reaction zone.
4. acid gas removal hydrogen sulfide treatment as claimed in claim 1 system is characterized in that, described regeneration of waste liquor unit comprises oxidation regeneration device (16) and apparatus of oxygen supply, and described oxidation regeneration device (16) is the vertical flat-bottom tank structure.
5. acid gas removal hydrogen sulfide treatment as claimed in claim 4 system is characterized in that, is provided with air sparger on the base plate of described oxidation regeneration device (16).
6. acid gas removal hydrogen sulfide treatment as claimed in claim 1 system, it is characterized in that, described treatment system also comprises the waste gas pretreatment unit, described waste gas pretreatment unit is connected in described absorption reaction unit, and described waste gas pretreatment unit carries out after the preliminary purification described sour gas being passed into described absorption reaction unit to described sour gas.
7. acid gas removal hydrogen sulfide treatment as claimed in claim 1 system, it is characterized in that, described treatment system also comprises tail gas treating unit, the described Complexing Iron catalyst desulfurizing solution that described tail gas treating unit is carried secretly for the tail gas of removing the generation of described absorption reaction unit and described regeneration of waste liquor unit.
8. acid gas removal hydrogen sulfide treatment as claimed in claim 1 system is characterized in that, described temperature control unit is solution heat exchanger (21), and described solution heat exchanger (21) is connected in described absorption reaction unit and described regeneration of waste liquor unit.
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| CN105289260A (en) * | 2015-11-20 | 2016-02-03 | 苏州韵蓝环保科技有限公司 | Hydrogen sulfide purifying device |
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| CN109589760A (en) * | 2018-11-07 | 2019-04-09 | 合肥通用机械研究院有限公司 | A kind of use for laboratory hydrogen sulfide quick treatment device and processing method |
| CN112608776A (en) * | 2021-01-15 | 2021-04-06 | 烟台新瑞环保科技有限公司 | Novel process capable of recycling and regenerating wet-process iron complex and special equipment thereof |
| CN116459663A (en) * | 2023-03-13 | 2023-07-21 | 上海安居乐环保科技股份有限公司 | Catalytic desulfurization process and reaction device for removing hydrogen sulfide in sewage and waste gas |
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2012
- 2012-09-28 CN CN 201220505813 patent/CN202844880U/en not_active Expired - Lifetime
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| CN104689698A (en) * | 2015-02-13 | 2015-06-10 | 北京三聚环保新材料股份有限公司 | Method and device for absorbing and purifying hydrogen sulphide by using polymeric ferric sulfate |
| CN104689698B (en) * | 2015-02-13 | 2017-07-25 | 北京三聚环保新材料股份有限公司 | A kind of method and apparatus of use bodied ferric sulfate absorption cleaning hydrogen sulfide |
| CN105289260A (en) * | 2015-11-20 | 2016-02-03 | 苏州韵蓝环保科技有限公司 | Hydrogen sulfide purifying device |
| CN107227185A (en) * | 2017-07-11 | 2017-10-03 | 江苏苏港和顺生物科技有限公司 | A kind of filtration integrated equipment of biogas production wet desulphurization elemental sulfur |
| CN107227185B (en) * | 2017-07-11 | 2023-06-23 | 江苏盐城港盐农循环农业有限公司 | Wet desulfurization elemental sulfur filtering integrated equipment for biogas production |
| CN109589760A (en) * | 2018-11-07 | 2019-04-09 | 合肥通用机械研究院有限公司 | A kind of use for laboratory hydrogen sulfide quick treatment device and processing method |
| CN109589760B (en) * | 2018-11-07 | 2021-04-27 | 合肥通用机械研究院有限公司 | Device and method for rapidly treating hydrogen sulfide for laboratory |
| CN112608776A (en) * | 2021-01-15 | 2021-04-06 | 烟台新瑞环保科技有限公司 | Novel process capable of recycling and regenerating wet-process iron complex and special equipment thereof |
| CN116459663A (en) * | 2023-03-13 | 2023-07-21 | 上海安居乐环保科技股份有限公司 | Catalytic desulfurization process and reaction device for removing hydrogen sulfide in sewage and waste gas |
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