CN204412040U - A kind of combined type Gas Purification Factory low concentration acid gas processing device - Google Patents
A kind of combined type Gas Purification Factory low concentration acid gas processing device Download PDFInfo
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- CN204412040U CN204412040U CN201420710263.7U CN201420710263U CN204412040U CN 204412040 U CN204412040 U CN 204412040U CN 201420710263 U CN201420710263 U CN 201420710263U CN 204412040 U CN204412040 U CN 204412040U
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Abstract
A kind of combined type Gas Purification Factory low concentration acid gas processing device provided by the utility model, comprise solid phase direct oxidation reaction and liquid phase oxidation reaction, described solid phase direct oxidation reaction and liquid phase oxidation reaction are connected in series, and the secondary sulphur condensation separator of described solid phase direct oxidation reaction is connected with the tail gas condenser in described liquid phase oxidation reaction.Solve the problem that Gas Purification Factory process low concentration acid gas process sulfur recovery rate is low and operating cost is high, total sulfur recovery reaches 99.9%, makes full use of novel oxidized catalyst choice, improves sulfur recovery rate, reclaims high-quality sulphur; Low Sulfur capacity acid gas ensures discharge gas reduction operating cost up to standard by liquid phase oxidation technique.
Description
technical field:
The utility model relates to a kind of combined type Gas Purification Factory low concentration acid gas processing device.
background technology:
Acid gas refers to the acid gas mixture of deviating from from sour natural gas, and its main component is H
2s and CO
2, and containing a small amount of hydro carbons.
H
2the low concentration acid gas that S content is less than 15% can not use Claus method sulphur recovery and extension process process, current low concentration acid gas Gas Purification Factory many employings conventional solid catalyst direct oxidation method or liquid-phase catalyst direct oxidation method.Conventional solid catalyst Crouse activity is good, poor selectivity, generates SO
2side reaction, sulfur recovery rate is the highest by about 90%, is difficult to reach current discharge standard.Liquid-phase catalyst direct oxidation method sulfur recovery rate can reach 99.9%, but product is water and impurity 60.0% (wt) sulphur cake, sulphur poor quality, is difficult to sell, and whole plant running cost is high.Because traditional low concentration acid gas treatment technology exists, exhaust emissions is not up to standard or sulfur product is defective and plant running high in cost of production problem, and the process of current Gas Purification Factory low concentration acid gas is a difficult point.
Along with the increasingly stringent of national requirements for environmental protection, industry-by-industry is corresponding has formulated stricter atmosphere pollutants emission standards.The SO of current Gas Purification Factory
2emission control is mainly by production technology measure, and raising sulfur recovery rate realizes, and this is also the common practice of foreign natural gas purification industry.At present both at home and abroad Gas Purification Factory high concentration acid gas adopts Claus method Recovered sulphur usually, improving sulfur recovery rate further and adds tail gas treatment process, mainly containing and extending Claus method, reducing absorping method and catalyst direct oxidation method to meet discharge standard.
Conventional Claus method recovery technology of sulfur and extension claus process thereof are subject to the restriction of reaction temperature generally with processing H
2the acid gas that S content is greater than 15%, the method has been very ripe technology.Claus reaction is micro-exothermic reaction, less from the equilibrium constant be reversible reaction, the highest sulfur recovery rate of such technique is only 99.2%.Restriction due to conversion ratio has stopped introducing at present, or built device has carried out transforming the new environment protection emission requirement of adaptation.
Reducing absorping method tail gas treatment process method is ripe, and total sulfur recovery rate can reach more than 99.8%.But because its technological process is more complicated, investment is high with operating cost, is generally used for the vent gas treatment of fairly large Claus device.
H
2the acid gas that S content is less than 15% does not domesticly at present have effective processing mode, and processing mode many employings catalyst direct oxidation method traditional at present, is divided into liquid phase oxidation and solid oxidation technique.Under the effect of catalyst, directly H
2s is oxidized to elemental sulfur.
Liquid phase oxidation technique is Complexing Iron liquid phase oxidation technology (LO-CAT technique) mainly, and Complexing Iron liquid phase oxidation technique utilizes ferrum-based catalyst to complete oxidation reaction, carries out the process of sulphur recovery.Its nucleus equipment is absorption/oxidation reactor.Mainly be applicable to the process of the relatively little acid gas of sulfur content or waste gas.LO-CAT device can reach the sulphur eliminating efficiency of more than 99.9%.Complexing Iron liquid phase oxidation technology needs interpolation 5 kinds of chemicals solvents, and solvent-oil ratio is large; Solvent feed system is complicated, and operating cost is high, produces sulphur medicament per ton and energy consumption consumes about 3500-4000 unit.Liquid phase oxidation technique product is moisture and impurity 60.0% (wt) sulphur cake, sulphur poor quality, is difficult to sell.
Solid-phase catalyst direct oxidation method, catalyst more options have the catalyst of Crouse's activity, due to this catalyst low-temperature activity, selective poor, catalyst existing catalysis H
2the reaction of S oxygen generates simple substance S, also has catalysis to generate SO
2side reaction, reduce sulphur yield, Recovery ratio is less than 90%, is difficult to meet more and more stricter emission request, and current built equipment carries out plant modification.
Utility model content
The utility model is the problem that sulfur recovery rate is low, operating cost is high existed for current Gas Purification Factory process low concentration acid gas and a kind of combined type Gas Purification Factory low concentration acid gas processing device developed.The solid-phase catalyst oxidation technology series connection liquid phase oxidation technique that it adopts new selective high, successfully solves the problem that Gas Purification Factory process low concentration acid gas process sulfur recovery rate is low and operating cost is high.
The technical solution adopted in the utility model:
A kind of combined type Gas Purification Factory low concentration acid gas processing device, comprise solid-phase redox reaction device and liquid phase oxidation reaction device, solid-phase redox reaction device and liquid phase oxidation reaction device are connected in series;
Described solid-phase redox reaction device comprises isothermal reactor, the upper end import of described isothermal reactor is connected with acid gas separator by pipeline, the upper end entrance of described acid gas separator is connected with acid gas pipeline, acid gas booster fan and acid gas preheater is connected with in turn between described acid gas separator and described isothermal reactor, the upper end import of described isothermal reactor is in series with air preheater successively, air-blaster, the upper inlet of described air-blaster is connected with air duct, the lower end outlet of described isothermal reactor is connected with one-level sulfur condenser, described one-level sulfur condenser outlet is connected with one-level sulphur condensation separator,
Described liquid phase oxidation reaction device comprises absorption oxidizing tower, and the arrival end of described absorption oxidizing tower is connected with gas-liquid separator, and the arrival end of gas-liquid separator is connected with tail gas condenser;
The upper end outlet of one-level sulphur condensation separator of described solid-phase redox reaction device is connected with the tail gas condenser entrance of liquid phase oxidation reaction device.
Be connected with adiabatic reactor and secondary sulphur condensation separator between described one-level sulphur condensation separator and described tail gas condenser in turn, between described adiabatic reactor and described secondary sulphur condensation separator, be connected with secondary sulfur condenser.
The upper end entrance of described isothermal reactor is connected with gas bag, and the outlet at bottom of described gas bag and the lower end outlet of warm reactor, the entrance of gas bag is connected with boiler replenishing water pipeline.
The upper outlet of described absorption oxidizing tower is connected with filter, is provided with air-blaster between described filter and described absorption oxidizing tower.
Described absorption oxidizing tower is taper, and described absorption oxidizing tower conical lower portion outlet is connected with sulphur stock pump.
Also comprise heat exchanger, the two ends of described heat exchanger are connected with absorption oxidizing tower, are provided with solution circulation pump between described heat exchanger and absorption oxidizing tower.
The beneficial effects of the utility model:
To low H
2s concentration (H
2s < 15%) acid gas treating process, meet now more and more stricter discharge standard.By adopting solid phase direct oxidation series connection liquid phase oxidation technology, solid phase direct oxidation catalyst selects low temperature active good, selective high Domestic New catalyst, selects the H of direct selective oxidation and direct oxidation two-stage reactor or direct selective oxidation A reactor 99.6% by the height of acid gas concentration
2s is converted into high-quality sulphur.
In process acid gas through supercooling laggard enter Complexing Iron liquid-phase oxidation reactor, by liquid phase oxidation remaining H
2s is direct oxidation into sulphur slurry, and total sulfur recovery reaches 99.9%.Reclaim most of sulphur by solid catalysis oxidizing process, greatly reduce into the total Sulfur capacity of liquid-phase oxidation reactor, reduce liquid phase oxidation technical operation cost.
By choice oxidation process and liquid phase oxidation process combination, make full use of novel oxidized catalyst choice, improve sulfur recovery rate, reclaim high-quality sulphur; Low Sulfur capacity acid gas ensures exhaust emissions reduction operating cost up to standard by liquid phase oxidation technique.
Be described further below in conjunction with accompanying drawing.
accompanying drawing illustrates:
Fig. 1 is the process schematic representation of combined type Gas Purification Factory low concentration acid gas processing device.
In figure: 1, acid gas separator; 2, acid gas booster fan; 3, acid gas preheater; 4, air-blaster; 5, air preheater; 6, isothermal reactor; 7, one-level sulfur condenser; 8, one-level sulphur condensation separator; 9, second order reaction preheater; 10, adiabatic reactor; 11, secondary sulfur condenser; 12, secondary sulphur condensation separator; 13, gas bag; 14, exhaust gas cooler; 15, gas-liquid separator; 16, oxidizing tower is absorbed; 17, filter; 18, air-blaster; 19, sulphur stock pump; 20, solution circulation pump; 21, heat exchanger.
A, acid gas pipeline; B, air duct; C, boiler replenishing water pipeline; D, Medium Pressure Steam Pipeline; E, acid lime set are to sewage treatment pipeline; F, exhaust pipe; G, defoamer pipeline; H, KOH solution pipeline; I, chemical solution pipeline; J, demineralized water pipeline; K, vacuum belt filter; M, storage tank.
detailed description of the invention:
Embodiment 1:
The utility model is the problem that sulfur recovery rate is low, operating cost is high existed for current Gas Purification Factory process low concentration acid gas and a kind of combined type Gas Purification Factory low concentration acid gas processing device developed.The solid-phase catalyst oxidation technology series connection liquid phase oxidation technique that it adopts new selective high, successfully solves the problem that Gas Purification Factory process low concentration acid gas process sulfur recovery rate is low and operating cost is high.
The utility model provide as shown in Figure 1 a kind of combined type Gas Purification Factory low concentration acid gas processing device and method to low H
2s concentration (H
2s < 15%) acid gas treating process, meet now more and more stricter discharge standard.
As shown in Figure 1, comprise solid-phase redox reaction device and liquid phase oxidation reaction device, solid-phase redox reaction device and liquid phase oxidation reaction device are connected in series;
Described solid-phase redox reaction device comprises isothermal reactor 6, the upper end import of described isothermal reactor 6 is connected with acid gas separator 1 by pipeline, the upper end entrance of described acid gas separator 1 is connected with acid gas pipeline a, acid gas booster fan 2 and acid gas preheater 3 is connected with in turn between described acid gas separator 1 and described isothermal reactor 6, the upper end import of described isothermal reactor 6 is in series with air preheater 5 successively, air-blaster 4, the upper inlet of described air-blaster 4 is connected with air duct b, the lower end outlet of described isothermal reactor 6 is connected with one-level sulfur condenser 7, described one-level sulfur condenser 7 outlet is connected with one-level sulphur condensation separator 8,
Described liquid phase oxidation reaction device comprises absorption oxidizing tower 16, and the arrival end of described absorption oxidizing tower 16 is connected with gas-liquid separator 15, and the arrival end of gas-liquid separator 15 is connected with tail gas condenser 14;
The upper end outlet of the one-level sulphur condensation separator 8 of described solid-phase redox reaction device is connected with tail gas condenser 14 entrance of liquid phase oxidation reaction device.
After mixing, gas enters isothermal reactor 6, carries out selective oxidation reaction, by most H in isothermal reactor 6
2s is direct oxidation into sulphur steam, sulphur steam after isothermal reaction enters one-level sulfur condenser 7, be cooled to 125 DEG C to enter one-level sulphur condensation separator 8 and isolate molten sulfur, molten sulfur enters storage tank m, the tail gas going out one-level sulphur condensation separator 8 enters adiabatic reactor 10 and carries out direct oxidation reaction after second order reaction preheater 9 is heated to 160 DEG C, reacted sulphur steam enters secondary sulfur condenser 11 and is cooled to 125 DEG C and enters secondary sulphur condensation separator 12 and isolate molten sulfur, and molten sulfur enters storage tank m; Heat exchange coil is established to be taken away by the heat that chemical reaction produces in isothermal reactor 6, the steam that heat exchange coil produces and water isolate steam and water in gas bag 13, produce a steam part as acid gas preheater 3 and air preheater 5 thermal source, remainder middle pressure steam goes out device, and the water of generation enters the circulation of isothermal reactor 6 heat exchange coil.
Be connected with in turn between described one-level sulphur condensation separator 8 and described tail gas condenser 14, adiabatic reactor 10, secondary sulfur condenser 11, secondary sulphur condensation separator 12.
The upper end entrance of described isothermal reactor 6 is connected with gas bag 13, the outlet at bottom of described gas bag 13 and the lower end outlet of warm reactor 6, and the entrance of gas bag 13 is connected with boiler replenishing water pipeline c.
Embodiment 2:
The upper outlet of described absorption oxidizing tower 16 is connected with filter 17, is provided with air-blaster 18 between described filter 17 and described absorption oxidizing tower 16.
The tail gas going out secondary sulphur condensation separator 12 is cooled to 50 DEG C through exhaust gas cooler 14 and enters absorption oxidizing tower 16 by gas-liquid separator 15, the H in tail gas
2s gas carries out reactive absorption with the alkaline solution absorbed in oxidizing tower 16, generates sulphur simple substance with the chelated iron oxidation reaction absorbed in oxidizing tower 16; Air enters after air-blaster 18 supercharging through filter 17 and enters absorption oxidizing tower 16 ferrous ions oxidation recycling utilization.
Embodiment 3:
Described absorption oxidizing tower 16 is taper, and described absorption oxidizing tower 16 conical lower portion outlet is connected with sulphur stock pump 19.
Also comprise heat exchanger 21, the two ends of described heat exchanger 21 are connected with absorption oxidizing tower 16, are provided with solution circulation pump 20 between described heat exchanger 21 and absorption oxidizing tower 16.
When absorbing the slurry of the sulphur bottom oxidizing tower 16 centrum concentration and reaching more than 5%, pumped by sulphur stock pump 19 and remove moisture to band filter, obtain 60.0% (wt) sulphur cake.Go out to absorb SO in the tail gas up to standard of oxidizing tower 16 discharge
2and H
2s concentration is less than 10ppm(v).Absorb solution in oxidizing tower and enter temperature constant in heat exchanger 21 maintenance absorption oxidizing tower by solution circulation pump 20.The KOH solution and chemical solution that absorb oxidizing tower 16 postreaction consumption is given by solution reservoir.
Embodiment 4:
A kind of combined type Gas Purification Factory low concentration acid gas processing method, its concrete steps are as follows,
(1) in described solid phase direct oxidation separator, from the external acid gas of device by acid gas passage a enter acid gas separator 1 be separated after through acid gas booster fan 2 supercharging, be heated to 180 DEG C through acid gas preheater 3 after supercharging; Meanwhile, air enters air-blaster 4 supercharging by air duct b, with acid gas by acid gas preheater 3 mixes after being heated to 180 DEG C after supercharging by air preheater 5;
(2) when gas after mixing enters isothermal reactor 6, in isothermal reactor 6, selective oxidation reaction is carried out, by H
2s is direct oxidation into sulphur steam, and the sulphur steam after isothermal reaction enters one-level sulfur condenser 7, and be cooled to 125 DEG C and enter one-level sulphur condensation separator 8 and isolate molten sulfur, molten sulfur enters storage tank m;
(3) tail gas going out one-level sulphur condensation separator 8 enters adiabatic reactor 10 and carries out direct oxidation reaction after second order reaction preheater 9 is heated to 160 DEG C, reacted sulphur steam enters secondary sulfur condenser 11 and is cooled to 125 DEG C and enters secondary sulphur condensation separator 12 and isolate molten sulfur, and molten sulfur enters storage tank m;
(4) heat exchange coil is established to be taken away by the heat that chemical reaction produces in isothermal reactor 6, the steam that heat exchange coil produces and water isolate steam and water in gas bag 13, produce a steam part as acid gas preheater 3 and air preheater 5 thermal source, remainder middle pressure steam goes out device, and the water of generation enters the circulation of isothermal reactor 6 heat exchange coil;
(5) tail gas going out secondary sulphur condensation separator 12 is cooled to 50 DEG C through exhaust gas cooler 14 and enters absorption oxidizing tower 16 by gas-liquid separator 15, the H in tail gas
2s gas carries out reactive absorption with the alkaline solution absorbed in oxidizing tower 16, generates sulphur simple substance with the chelated iron oxidation reaction absorbed in oxidizing tower 16;
(6) in described liquid phase oxidation separator, air enters to enter after air-blaster 18 supercharging through filter 17 by air duct b and absorbs oxidizing tower 16 ferrous ions oxidation recycling utilization;
(7) when absorbing the slurry of the sulphur bottom oxidizing tower 16 centrum concentration and reaching more than 5%, pumped by sulphur stock pump 19 and remove moisture to band filter, obtain 60.0% (wt) sulphur cake, go out to absorb SO in the tail gas up to standard that oxidizing tower 16 discharged by exhaust pipe f
2and H
2s concentration is less than 10ppm(v);
(8) in absorption oxidizing tower, solution enters temperature constant in heat exchanger 21 maintenance absorption oxidizing tower 16 by solution circulation pump 20, is given absorb KOH solution and the chemical solution that oxidizing tower 9 passes through KOH solution pipeline h and chemical solution pipeline i postreaction consumption by solution reservoir.
Out all pass through sewage treatment pipeline e to sewage disposal system process by acid lime set from acid gas separator and 15 gas-liquid separators, boiler replenishing water pipeline c is connected with gas bag 13 with Medium Pressure Steam Pipeline d, ensures to have abundant water resources.Defoamer pipeline g is connected with solution circulation pump 20, ensures solution smoothly by solution circulation pump 20.
As shown in Figure 1, the sour gas external from device carries out supercharging after sour gas knockout drum 1 initial gross separation, after acid preheater 3 is heated to 180 DEG C, mix with the air b being heated to 180 DEG C through air-blaster 4 supercharging and air preheater 5, and gas O after ensureing mixing
2/ H
2s=0.6-0.8, after mixing, gas enters isothermal reactor 6.Sour gas carries out selective oxidation reaction at isothermal reactor 6 by new selective oxidation catalyst, by most H
2s is oxidized to sulphur, and during isothermal reaction, heat exchanger tube 21, interior generation steam, takes away the heat that reaction produces, and a steam part is as reactor inlet heater thermal source, and remainder goes out device.Gas after isothermal reaction enters one-level sulfur condenser 7, is cooled to 125 DEG C, isolates molten sulfur.Tail gas after isolating molten sulfur also has a small amount of H
2s gas, also needs the adiabatic reaction carrying out the degree of depth.This gas enters adiabatic reactor 10 and carries out direct oxidation reaction after second order reaction preheater 9 is heated to 160 DEG C.Reacted gas is cooled to 125 DEG C through secondary sulfur condenser 11, is separated molten sulfur afterwards at secondary sulphur condensation separator 12.H in acid gas
2one-level isothermal reaction can be directly adopted when S concentration is lower.
Adopt new selective direct oxidation catalyst, this reactional equation is as follows:
Selective oxidation sulfur removal technology core technology is its selective oxidation catalyst, and its selective oxidation catalyst is HS-35, and its outward appearance, shape are cylindrical, and Main Ingredients and Appearance is TiO
2, Fe
2o
3, Al
2o
3, specification mm Φ 4 × 5 ~ 15(L), breaking strength N/cm>=120, bulk density kg/m
3900 ~ 1100, specific surface m
2/ g 100 ~ 120, Recovery ratio %>=95.0, service life year>=3.0.
Deep oxidation catalyst is HS-38, and its shape is cylindrical, and Main Ingredients and Appearance is TiO
2, MoO, Fe
2o
3, specification mm Φ 4 × 5 ~ 15(L), breaking strength N/cm>=120, bulk density kg/m
3950 ~ 1050, Recovery ratio %>=95.0, service life year>=3.0.
This catalyst has good low temperature active and selective, can use at 130 DEG C, active without claus reaction, activity stabilized, and its selective oxidation is irreversible reaction.This reaction is non-equilibrium reaction, therefore its outlet H
2s concentration does not affect by thermodynamical equilibrium, and total sulfur recovery is high.
Tail gas after separation is cooled to 50 DEG C and enters liquid-phase oxidation reactor (LO-CAT device).Acid gas enters bottom absorption oxidizing tower 16 absorption chamber of main reactor, and air is passed into bottom the absorption oxidizing tower 16 of main reactor by air-blaster 18.Reactor absorbs the solution in oxidizing tower 16, is mainly demineralized water j, chelate, iron ion, KOH solution h, chemical solution i.
By density contrast at inside reactor shuttling movement voluntarily, ionization after the hydrogen sulfide in acid gas dissolves, react with the chelated iron in reactor and generate sulphur simple substance, the iron ion be reduced is regenerated under the oxidation of air.When sulphur slurry concentration bottom reactor centrum reaches more than 5%, pumped by sulphur stock pump 19 and remove moisture to vacuum belt filter k, obtain 60.0% (wt) sulphur cake.
Lo-cat technique is a kind of sulfur recovery technology carried out under normal temperature, lower pressure, is to carry out in the liquid phase, usually uses alkaline aqueous solution, catalyst adopts water-soluble chelates ferric ions, whole reaction can be divided into absorption reaction, regenerative response, also has side reaction to occur simultaneously.Alkaline solution can suppress the generation of side reaction.Chemical equation is as follows:
Absorption chamber: H
2s (g)+H
2o → H
2s (aq)+H
2o (H
2the dissolving of S gas)
H
2s (aq) → H
++ HS
-(cell reaction)
HS
-+ 2Fe
3+→ S (s)+H
++ 2Fe
2+(sulphur forming reactions)
Oxidizing chamber: O
2(g)+2H
2o → O
2(aq)+2H
2o (dissolving of oxygen)
O
2(aq)+4H
++ 4Fe
2+→ 2H
2o+4Fe
3+(dissolved oxygen Oxidation of Fe
3+)
By adopting solid phase direct oxidation and liquid phase oxidation (LO-CAT device) composite acid gas disposal technology, ensure SO in emission
2and H
2s concentration is less than 10ppm(v).Overcome traditional Crouse and extension process can not process low H
2s concentration (H
2s < 15%) acid gas, solve direct oxidation method process low concentration acid gas sulfur recovery rate low, reduce Sulfur capacity and reduce liquid phase oxidation (LO-CAT device) operating cost.
Claims (6)
1. a combined type Gas Purification Factory low concentration acid gas processing device, is characterized in that: comprise solid-phase redox reaction device and liquid phase oxidation reaction device, and solid-phase redox reaction device and liquid phase oxidation reaction device are connected in series;
Described solid-phase redox reaction device comprises isothermal reactor (6), the upper end import of described isothermal reactor (6) is connected with acid gas separator (1) by pipeline, the upper end entrance of described acid gas separator (1) is connected with acid gas pipeline (a), acid gas booster fan (2) and acid gas preheater (3) is connected with in turn between described acid gas separator (1) and described isothermal reactor (6), the upper end import of described isothermal reactor (6) is in series with air preheater (5) successively, air-blaster (4), the upper inlet of described air-blaster (4) is connected with air duct (b), the lower end outlet of described isothermal reactor (6) is connected with one-level sulfur condenser (7), described one-level sulfur condenser (7) outlet is connected with one-level sulphur condensation separator (8),
Described liquid phase oxidation reaction device comprises absorption oxidizing tower (16), and the arrival end of described absorption oxidizing tower (16) is connected with gas-liquid separator (15), and the arrival end of gas-liquid separator (15) is connected with tail gas condenser (14);
The upper end outlet of the one-level sulphur condensation separator (8) of described solid-phase redox reaction device is connected with tail gas condenser (14) entrance of liquid phase oxidation reaction device.
2. a kind of combined type Gas Purification Factory low concentration acid gas processing device according to claim 1, it is characterized in that: between described one-level sulphur condensation separator (8) and described tail gas condenser (14), be connected with adiabatic reactor (10) and secondary sulphur condensation separator (12) in turn, between described adiabatic reactor (10) and described secondary sulphur condensation separator (12), be connected with secondary sulfur condenser (11).
3. a kind of combined type Gas Purification Factory low concentration acid gas processing device according to claim 1, it is characterized in that: the upper end entrance of described isothermal reactor (6) is connected with gas bag (13), the outlet at bottom of described gas bag (13) and the lower end outlet of warm reactor (6), the entrance of gas bag (13) is connected with boiler replenishing water pipeline (c).
4. a kind of combined type Gas Purification Factory low concentration acid gas processing device according to claim 1, it is characterized in that: the upper outlet of described absorption oxidizing tower (16) is connected with filter (17), is provided with air-blaster (18) between described filter (17) and described absorption oxidizing tower (16).
5. a kind of combined type Gas Purification Factory low concentration acid gas processing device according to claim 1, is characterized in that: described absorption oxidizing tower (16) is taper, and described absorption oxidizing tower (16) conical lower portion outlet is connected with sulphur stock pump (19).
6. a kind of combined type Gas Purification Factory low concentration acid gas processing device according to claim 1, it is characterized in that: also comprise heat exchanger (21), the two ends of described heat exchanger (21) are connected with absorption oxidizing tower (16), are provided with solution circulation pump (20) between described heat exchanger (21) and absorption oxidizing tower (16).
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399362A (en) * | 2014-11-24 | 2015-03-11 | 西安长庆科技工程有限责任公司 | Combination-type low-concentration acid gas processing device and method for natural gas conditioning plant |
| CN111547685A (en) * | 2020-04-10 | 2020-08-18 | 国网河北省电力有限公司电力科学研究院 | Low concentration SF in enclosed space6Gas recovery processing device and method |
| CN111821844A (en) * | 2020-05-11 | 2020-10-27 | 天津市众天科技发展有限公司 | Desulfurization process method combining dry oxidation and wet oxidation |
-
2014
- 2014-11-24 CN CN201420710263.7U patent/CN204412040U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399362A (en) * | 2014-11-24 | 2015-03-11 | 西安长庆科技工程有限责任公司 | Combination-type low-concentration acid gas processing device and method for natural gas conditioning plant |
| CN104399362B (en) * | 2014-11-24 | 2016-08-17 | 西安长庆科技工程有限责任公司 | A kind of combination type Gas Purification Factory low concentration acid gas processing device and method |
| CN111547685A (en) * | 2020-04-10 | 2020-08-18 | 国网河北省电力有限公司电力科学研究院 | Low concentration SF in enclosed space6Gas recovery processing device and method |
| CN111547685B (en) * | 2020-04-10 | 2022-01-25 | 国网河北省电力有限公司电力科学研究院 | Low-concentration SF6 gas recovery processing device and method in closed space |
| CN111821844A (en) * | 2020-05-11 | 2020-10-27 | 天津市众天科技发展有限公司 | Desulfurization process method combining dry oxidation and wet oxidation |
| CN111821844B (en) * | 2020-05-11 | 2022-06-03 | 天津市众天科技发展有限公司 | Desulfurization process method combining dry oxidation and wet oxidation |
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