CN204746071U - Processing apparatus of sulphur recovery unit tail gas - Google Patents
Processing apparatus of sulphur recovery unit tail gas Download PDFInfo
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- CN204746071U CN204746071U CN201520412748.2U CN201520412748U CN204746071U CN 204746071 U CN204746071 U CN 204746071U CN 201520412748 U CN201520412748 U CN 201520412748U CN 204746071 U CN204746071 U CN 204746071U
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Abstract
The utility model discloses a processing apparatus of sulphur recovery unit tail gas, melt the sulphur ware including oxidation tower, the vertical pipe who connects sulphur recovery unit and oxidation tower lower part, oxidation liquid storage tank, filtration, be equipped with syntropy pipeline nozzle at the vertical pipe top, the vertical pipe bottom is equipped with reverse pipeline nozzle, be equipped with the equipment shower nozzle on oxidation tower upper portion, be equipped with demister and tail gas purification export at the oxidation tower top, the oxidation tower through elemental sulfur export with filter melt the sulphur ware contain sulphur liquid entry linkage, filter and melt sulphur ware bottom and be equipped with and melt the sulphur export, oxidation tower bottom liquid outlet and filter and melt the scavenging solution export of sulphur ware lower part and be connected through the oxidation liquid circulating pump and the equipment shower nozzle of vertical pipe's syntropy pipeline nozzle, reverse pipeline nozzle and oxidation tower, oxidation liquid circulating pump entry is connected with oxidation liquid storage tank. The utility model discloses the device have equipment few, take up an area of to economize, the small investment, characteristics such as easy operation, and the desulfurization by -product is water, can not cause secondary pollution, the desulfurization is efficient, the energy consumption is low.
Description
Technical field
The utility model belongs to sulfur recovery tail gas processing technology field, relates to a kind for the treatment of apparatus of sulfur recovery facility tail gas.
Background technology
Improve since Claus sulphur recovery technology realizes suitability for industrialized production from the thirties in last century, have passed through development and the improvement of nearly 90 years, be tending towards ripe and perfect, but because Claus reaction is reversible reaction, be subject to the restriction of chemical balance, even if arrive the conversion of level Four by three, the overall recovery of sulphur can only reach about 98%, and tail gas index does not still reach " discharge standard of air pollutants " (GB16297-1996).This just requires that sulfur recovery rate is higher than 99.5% and just can carries out device production, develop and realize industrialized technique both at home and abroad at present and have tens kinds, can be divided into by the principles of chemistry: tail gas reduction-absorption process, low temperature Claus technique, direct oxidation process and exhaust combustion ammonia absorption technique.
Present stage, what the vent gas treatment of sulfur recovery facility was conventional is reduction-absorption process, is first namely H sulfur-containing compound Restore All in tail gas
2s, and then removed, finally reclaim with the form of sour gas or elementary sulfur, absorbing liquid recyclable regenerative uses.Tail gas after reduction burns part directly calcination through tail gas, makes sulfur-containing compound finally with SO
2form enter air.Wherein, the sulfur content of reducing in tail gas is to the SO finally draining into air
2affect larger.And the absorbing liquid of present stage adopts the formula solution of N methyldiethanol amine substantially, although to H
2s has selective preferably, but by CO
2impact, can not effectively all absorb, and to organic sulfur COS, CS
2substantially there is no assimilation effect, cause the SO finally draining into air
2be difficult to control at 200mg/Nm
3below.
Along with a large amount of exploitations of global sour crude oil and natural gas resource, and the development of Coal Chemical Industry, sulphur recovery has become indispensable supporting environmental protecting device; And along with the standard increasingly stringent of countries in the world environment protection, require more and more high to the sulfur recovery rate of sulfur recovery facility.Mandatory standard " discharge standard of air pollutants " (GB16297-1996) that China came into effect on January 1st, 1997, not only defines SO in tail gas
2the highest permission rate of discharge, also specify the highest permission concentration of emission, namely 1200mg/Nm be respectively to existing pollution sources and new pollution sources the highest permission discharge quality concentration
3and 960mg/Nm
3.For the sulfur recovery facility in current domestic natural gas purification plant and oil plant, use SCOT method tail gas treatment process can reach the emission request that standard specifies.But " sulfuric acid industry pollutant emission standard " (GB26132-2010) that national environmental protection portion newly promulgates explicitly points out: from 01 day October in 2013, the concentration of emission limit value of existing sulfuric acid industry enterprise sulfur dioxide pollution thing will be adjusted downward to 400mg/Nm
3.From on 03 01st, 2011, newly-built sulfuric acid industry enterprise performed the concentration of emission limit value 400mg/Nm of sulfur dioxide pollution thing
3, sulfuric acid mist must lower than 30mg/Nm
3regulation.
China Petrochemical Industry actively implements green low-carbon development strategy, the sulfur dioxide emissioning concentration reduced in sulfur recovery facility tail gas is striven for one of important indicator of world-class enterprise as oil refining plate, and " petroleum refining industry pollutant emission standard " exposure draft is issued, wherein specify: existing enterprise from 1 day July in 2014 and newly-built enterprise from 1 day July in 2011, performed sulfur recovery facility sulfur dioxide emissioning concentration be less than 400mg/Nm
3(particular locality is less than 200mg/Nm
3).And " petroleum refining industry pollutant emission standard " Press release is being fermented, wherein specifying: sour gas retracting device sulfur dioxide emissioning concentration is less than 400mg/Nm
3(particular locality is less than 100mg/Nm
3).It is imperative that sulfur dioxide reduces discharging, and China advocates energy-saving and emission-reduction work always, the damage ratio of sulfur dioxide to environment is more serious, and haze is also more and more serious, along with increasingly stringent and the raising of discharge standard, existing recovery technology of sulfur has to pass through the degassed tail gas in transformation sulphur pond, improves the SO that the series of measures such as lyosoption could reduce fume emission
2index, meets strict emission request.
Utility model content
The purpose of this utility model is for prior art Problems existing, a kind for the treatment of apparatus of sulfur recovery facility tail gas is provided, utilize this device to adopt hydrogen peroxide oxidation process from the sulfur-containing tail gas of sulfur recovery facility solvent absorption tower top or sulphur pond tail gas or both mixing, final SO can be reduced
2concentration of emission, the SO of the tail gas after process after burning in final discharge flue gas
2be reduced to 35mg/Nm
3below, acquisition product is sulphur, and byproduct is water, and can not cause secondary pollution, and desulfuration efficiency is high, energy consumption is low.
The purpose of this utility model is realized by following technical approach:
A treating apparatus for sulfur recovery facility tail gas, comprises oxidizing tower, the vertical pipe connecting sulfur recovery facility and oxidizing tower bottom, oxidation solution storage tank, filters molten sulphur device; The bottom being provided with plumbing nozzle, vertical pipe in the same way at the top of described vertical pipe is provided with reverse plumbing nozzle; Described oxidizing tower is hollow-spraying-tower type tower, is provided with equipment shower nozzle on the top of oxidizing tower, is provided with demister and cleaning of off-gas outlet at the top of oxidizing tower; Described oxidizing tower is connected with the sulfur-bearing liquid entrance filtering molten sulphur device through the elemental sulfur outlet of lower side, obtain elemental sulfur for the elemental sulfur offscum on liquid level top, oxidizing tower bottom being sent into the molten sulphur device separating and filtering of filtration, the bottom that sulphur device is melted in described filtration is provided with the outlet of molten sulphur; The scavenging solution outlet that sulphur device bottom is melted in liquid outlet bottom described oxidizing tower and described filtration is connected through the equipment shower nozzle of oxidation solution circulating pump with the plumbing nozzle in the same way of vertical pipe, reverse plumbing nozzle and oxidizing tower; The entrance of described oxidation solution circulating pump is connected with oxidation solution storage tank.
Preferably, oxidation solution delivery pump is also provided with at the export pipeline of described oxidation solution storage tank.
Preferably, be at least provided with one deck plumbing nozzle in the same way on the top of described vertical pipe, be at least provided with the reverse plumbing nozzle of one deck in the bottom of described vertical pipe; Preferred further, be provided with two-layer plumbing nozzle in the same way on the top of described vertical pipe, be provided with the reverse plumbing nozzle of one deck in the bottom of described vertical pipe.
Preferably, one deck equipment shower nozzle is at least provided with on the top of described oxidizing tower; Preferred further, be provided with two to three-layer equipment shower nozzle on the top of described oxidizing tower.
Preferably, the treating apparatus of described sulfur recovery facility tail gas also comprises oxidation solution filter Sum decomposition device; Arrange bypass at the outlet line of described oxidation solution circulating pump, described bypass is connected with the liquid-inlet of oxidation solution filter, and the liquid outlet of described oxidation solution filter is connected with decomposer, oxidation solution storage tank respectively through two pipelines in parallel.
Preferably, described filtration melts the number of sulphur device for two or more.Described filtration is melted sulphur device and is comprised the tank body be made up of cylindrical shell and upper cover, low head; Described upper cover is provided with steam companions; Described cylindrical shell top is provided with sulfur-bearing liquid entrance, and bottom is provided with scavenging solution outlet; Described low head is provided with the outlet of molten sulphur and discharge opeing outlet; Steam jacket is provided with outside described cylindrical shell and low head; At least two-layer filter arranged in staggered floor is provided with in described cylindrical shell, described filter comprises Rose Box, described Rose Box comprises extraction plate and sidewall spacer, sidewall spacer top is provided with oblique slide carriage, in Rose Box, be provided with the first filter course, in the first filter course, be provided with steam pipe coil; Be provided with the second filter course at described cylinder body bottom, in the second filter course, be provided with steam pipe coil; The 3rd filter course is provided with in described low head; Be provided with downflow weir in described scavenging solution exit, be provided with the 4th filter course in the bottom of downflow weir, in the 4th filter course, be provided with steam pipe coil, above the 4th filter course, be provided with at least one deck sieves plate.
It is that upper and lower staggered floor is arranged that filter in sulphur device is melted in described filtration, can adjust the number of filter according to the actual requirements.When the number of filter is even numbers, neighbouring filter forms a filtration group.
Preferably, adjacent two layers filter is arranged in half-and-half type in cylindrical shell.
Preferably, described sidewall spacer exceeds 200 ~ 300mm than the first filter course.Described oblique slide carriage becomes the angle of 20 ~ 60 ° with sidewall spacer, also improve filter and discharging efficiency in order to water conservancy diversion.Preferably, described downflow weir is made up of sidewall baffle plate and top flap, and described sidewall baffle plate and top flap are solid barrier.Above the 4th filter course, be provided with two-layer filtration sieve plate, the sieve aperture of upper level filter sieve plate is less than the sieve aperture that sieve plate filters in lower floor.Scavenging solution after filtration enters downflow weir by low head, come through in the double medium filtration sieve plate overflow after the 4th filter course in the middle part of downflow weir, the sidewall baffle plate of downflow weir and top flap are solid barrier, prevent from not filtering suspension completely and export discharge by scavenging solution.
Preferably, described steam companions is provided with steam inlet and steam (vapor) outlet; The top of described steam jacket is provided with steam inlet, and the bottom of steam jacket is provided with steam (vapor) outlet.
Preferably, described upper cover is provided with gas phase connected entrance and at least one observation panel.Preferred further, described upper cover is provided with two observation panels, and the both sides being arranged on upper cover of described observation panel symmetry are so that observe the filtration of filtering in molten sulphur device, molten sulphur situation.
Preferably, described filtration is melted sulphur device and is also provided with at least one manhole; Preferred further, described filtration is melted sulphur device and is provided with two manholes, and wherein, a manhole is arranged on upper cover, and another manhole is arranged on cylindrical shell bottom.
Described upper cover is ellipsoidal head, and described low head is ellipsoidal head or conical head.
The filler of the first described filter course, the second filter course, the 3rd filter course and the 4th filter course is SNGLA type or Type B filler, or porcelain ball and metal packing etc., and the particle of elemental sulfur and foam can be adsorbed on the surface of above-mentioned filler.
The suspension that sulphur device can filter sulfur-bearing foam is melted in described filtration, and elemental sulfur is attracted in filter, and the solution after purification is gone out by equipment side surface current, can be recycled; Elemental sulfur in filter is discharged by filter bottom after heating and melting, Recovered sulphur.It is operating as intermittently operated, and during normal operating, being divided into filtration and two operating process of molten sulphur, is atmospheric operation during filtration, is pressurized operation during molten sulphur.During filtration, sulfur-bearing liquid is entered by sulfur-bearing liquid entrance and filters in molten sulphur device, to the filter being arranged on top layer, sulfur-bearing liquid by the first filter course in filter gap flow automatically and under, the particle of part elemental sulfur and foam are filtered layer absorption, after the extraction plate of the filter of top layer, arrive lower one deck filter, after all filters, cylinder body bottom is arrived until liquid, after the second filter course and the 3rd filter course filter absorption, overflow launder is entered from low head, exported to scavenging solution by the two-layer sieve plate overflow in the middle part of downflow weir again through after the 4th filter course, obtain the scavenging solution after filtering.The sulfur-bearing liquid entrance of molten sulphur device to be filtered and scavenging solution outlet pressure reduction larger time, stop passing into sulfur-bearing liquid, when liquid outlet to be clean and discharge opeing outlet are all flowed out without scavenging solution, enter molten sulphur process, open all tracing steams (comprising steam companions, steam jacket and steam pipe coil), heating and melting is filtered the elemental sulfur of the first filter course in device, the second filter course, the 3rd filter course and the 4th filter course absorption, and molten sulfur exports discharge by melting sulphur.After molten sulfur emptying, filter process can be reentered.
Utilize the method for the utility model device sulfur recovery facility process tail gas, step is as follows:
(1) tail gas, from sulfur recovery facility passes into vertical pipe from top, oxidation solution in oxidation solution storage tank is delivered to top and the bottom spray of vertical pipe, sulfur-bearing thing in tail gas contacts with oxidation solution co-current flow and counter-current flow in vertical pipe, there is oxidation reaction and generate elemental sulfur and water, complete the first order oxidation, through the first order oxidation tail gas, with generate elemental sulfur enter oxidizing tower with water together with oxidation solution;
(2) tail gas, through first order oxidation rises in oxidizing tower, the oxidation solution counter current contacting that sulfur-bearing thing in tail gas and oxidizing tower top spray, complete second level oxidation, the tail gas again after oxidation sweetening drains into sulfur recovery unit burning part by oxidation tower top and continues process after foam removal; The elemental sulfur that oxidation generates, water enter bottom oxidizing tower together with oxidation solution, and bottom oxidizing tower, the elemental sulfur offscum of ullage enters the molten sulphur device separating and filtering of filtration and obtains elemental sulfur; Oxidation solution bottom oxidizing tower with filter the oxidation solution after filtering in molten sulphur device and fresh oxidation solution converges, be delivered to the top of vertical pipe by oxidation solution circulating pump, the top of bottom and oxidizing tower recycle.
The utility model method is applicable to the sulfur-containing tail gas processing any concentration, be specially adapted to the process of the sulfur-containing tail gas of sulfur recovery facility solvent absorption tower top tail gas or sulphur pond tail gas or both mixing, be mainly H from sulfur-bearing thing in the tail gas of sulfur recovery facility solvent absorption tower top
2s, COS, CS
2, in the tail gas of sulphur pond, sulfur-bearing thing is mainly H
2s and S simple substance, and in tail gas hydrogen sulfide and organic sulfur concentration lower, be in ppm rank.Tail gas from sulfur recovery facility described in the utility model is the sulfur-containing tail gas from the tail gas of sulfur recovery facility solvent absorption tower top or sulphur pond tail gas or both mixing, H in the sulfur-containing tail gas of the described tail gas from sulfur recovery facility solvent absorption tower top or sulphur pond tail gas or both mixing
2the volume content of S is not higher than 0.05%.
Described oxidation solution to be concentration be 1% ~ 35% hydrogen peroxide, being preferably concentration is the hydrogen peroxide of 1% ~ 10%.Hydrogen peroxide is a kind of strong oxidizer, and oxidisability is better than chlorine, chlorine dioxide, potassium permanganate, and can be converted into by catalysis the hydroxy that activity is only second to fluorine, its catabolite is harmless oxygen and water.Adopt hydrogen peroxide can reach the object of desulfurization as oxidant, operating condition is gentleer, selective height, can effectively remove sulphur and organic sulfur, can not cause secondary pollution.Can by H
2s is oxidized to elemental sulfur and water, and Recovered sulphur produces without the three wastes simultaneously.
In step (1), the oxidation solution being delivered to the top of vertical pipe sprays downwards, the oxidation solution of downward ejection and tail gas co-current contact, be delivered to the oxidation solution upward spraying of the bottom of vertical pipe, the oxidation solution upwards sprayed and tail gas counter current contacting, there is oxidation reaction and generate elemental sulfur and water, complete first order oxidation.The oxidation solution of spray is excessive, ensures to complete oxidation reaction to greatest extent, and the absorptivity making sulfur-bearing thing in tail gas in described first order oxidation is 50 ~ 65%.
In step (2), on the basis of first order oxidation, sulfur-bearing thing residual lower than 20ppmV in tail gas after the oxidation of the second level.The sulfur recovery unit burning part that drains into the tail gas that autoxidation top of tower is discharged continues process, the SO in final discharge flue gas
2lower than 35mg/Nm
3.
There is oxidation reaction in the sulfur-bearing thing in step (1), (2) in tail gas and oxidation solution, temperature is 10 ~ 40 DEG C at normal temperatures.
In step (2), in the bypass of the outlet line of oxidation solution circulating pump, oxidation solution filter is set, by oxidation solution circulating pump be delivered to the top of vertical pipe, bottom and oxidizing tower the oxidation solution at top excessive time, excessive oxidation solution is delivered to oxidation solution filter, after filtering oxidation solution, entering decomposer, is the discharge of free of contamination water through heat resolve.
The beneficial effects of the utility model:
The treating apparatus of the utility model sulfur recovery facility tail gas has the features such as equipment is few, occupation of land economizes, small investment, simple to operate, and desulfuration byproduct is water, can not cause secondary pollution, and desulfuration efficiency is high, energy consumption is low.Utilize this device, adopt hydrogen peroxide oxidation process from the method for the sulfur-containing tail gas of sulfur recovery facility tail gas solvent absorption tower top sulfur-containing tail gas or sulphur pond tail gas or both mixing, the sulfur-containing tail gas of any concentration can be processed, and the SO of the tail gas after process after burning in final discharge flue gas
2be reduced to 35mg/Nm
3below.Reach present stage the strictest emission request.
Accompanying drawing explanation
Fig. 1 is the structural representation of the treating apparatus of the utility model sulfur recovery facility tail gas;
Fig. 2 is the structural representation filtering molten sulphur device.
In Fig. 1,1-oxidizing tower, 2-vertical pipe, 3-is plumbing nozzle in the same way, the reverse plumbing nozzle of 4-, 5-equipment shower nozzle, 6-oxidation solution storage tank, 7-oxidation solution delivery pump, and 8-filters molten sulphur device, 9-oxidation solution circulating pump, 10-oxidation solution filter, 11-decomposer;
In Fig. 2, 801-cylindrical shell, 802-upper cover, 803-low head, 804-steam companions, 805-sulfur-bearing liquid entrance, 806-scavenging solution exports, 807-melts sulphur outlet, 808-discharge opeing exports, 809-steam jacket, 810-filter, 811-extraction plate, 812-sidewall spacer, the oblique slide carriage of 813-, 814-first filter course, 815-steam pipe coil, 816-downflow weir, 817-second filter course, 818-the 3rd filter course, 819-the 4th filter course, 820-upper level filter sieve plate, sieve plate filters in 821-lower floor, 822-gas phase connected entrance, 823-observation panel, 824-manhole, 825-steam inlet, 826-steam (vapor) outlet.
Detailed description of the invention
With embodiment, the technical solution of the utility model is further described by reference to the accompanying drawings.
As shown in Figure 1, a kind for the treatment of apparatus of sulfur recovery facility tail gas, comprises oxidizing tower 1, the vertical pipe 2 connecting sulfur recovery facility and oxidizing tower 1 bottom, oxidation solution storage tank 6, filters molten sulphur device 8; The bottom being provided with plumbing nozzle 3, vertical pipe 2 in the same way at the top of described vertical pipe 2 is provided with reverse plumbing nozzle 4; Described oxidizing tower 1 is hollow-spraying-tower type tower, is provided with equipment shower nozzle 5 on the top of oxidizing tower 1, is provided with demister and cleaning of off-gas outlet at the top of oxidizing tower 1; Described oxidizing tower 1 is connected with the sulfur-bearing liquid entrance filtering molten sulphur device 8 through the elemental sulfur outlet of lower side, obtain elemental sulfur for the elemental sulfur offscum on oxidizing tower 1 bottoms level top being sent into molten sulphur device 8 separating and filtering of filtration, the bottom that sulphur device 8 is melted in described filtration is provided with the outlet of molten sulphur; The equipment shower nozzle 5 that the in the same way plumbing nozzle 3 of scavenging solution outlet through oxidation solution circulating pump 9 and vertical pipe 2 of sulphur device 8 bottom, reverse plumbing nozzle 4 and oxidizing tower 1 are melted in liquid outlet bottom described oxidizing tower 1 and described filtration is connected; The entrance of described oxidation solution circulating pump 9 is connected with oxidation solution storage tank 6 through oxidation solution delivery pump 7.
The bypass of valve is provided with at the outlet line of described oxidation solution circulating pump 9, described bypass is connected with the liquid-inlet of oxidation solution filter 10, the liquid outlet of described oxidation solution filter 10 is connected with decomposer 11, oxidation solution storage tank 6 respectively through two pipelines in parallel, connecting the pipeline of oxidation solution filter 10 with decomposer 11, is connected on the pipeline of oxidation solution filter 10 and oxidation solution storage tank 6 and is respectively equipped with valve.
At least be provided with one deck plumbing nozzle 3 in the same way on the top of described vertical pipe 2, be at least provided with the reverse plumbing nozzle 4 of one deck in the bottom of described vertical pipe 2; The number of plies of plumbing nozzle 3 and reverse plumbing nozzle 4 in the same way can be adjusted according to actual needs, in the present embodiment, be provided with two-layer plumbing nozzle in the same way 3 on the top of described vertical pipe 2, be provided with the reverse plumbing nozzle 4 of one deck in the bottom of described vertical pipe 2.
One deck equipment shower nozzle 5 is at least provided with on the top of described oxidizing tower 1; The number of plies of equipment shower nozzle 5 can be adjusted according to actual needs, in the present embodiment, be provided with three-layer equipment shower nozzle 5 on the top of described oxidizing tower 1.
As shown in Figure 2, described molten sulphur filter 8 comprises the tank body be made up of cylindrical shell 801 and upper cover 802, low head 803; Described upper cover 802 is provided with steam companions 804; Described cylindrical shell 801 top is provided with sulfur-bearing liquid entrance 805, and bottom is provided with scavenging solution outlet 806; Described low head 803 is provided with molten sulphur outlet 807 and discharge opeing outlet 808; Be provided with steam jacket 809 outside described cylindrical shell 801 and low head 803, be provided with steam inlet 825 on the top of described steam jacket 809, the bottom of steam jacket 809 is provided with steam (vapor) outlet 826; Be provided with the filter 810 that two faulted layers are arranged in described cylindrical shell 802, described adjacent two layers filter 810 is arranged in half-and-half type in cylindrical shell 801; Described filter 810 comprises Rose Box, described Rose Box comprises extraction plate 811 and sidewall spacer 812, the first filter course 814 is provided with in Rose Box, steam pipe coil 815 is provided with in the first filter course 814, described sidewall spacer 812 to the first filter course 814 exceeds 300mm, oblique slide carriage 813 is provided with, the angle of oblique slide carriage 813 and sidewall spacer 812 one-tenth 20 ~ 60 ° at sidewall spacer 812 top; Bottom described cylindrical shell 1, be provided with the second filter course 817, in the second filter course 817, be provided with steam pipe coil 815; The 3rd filter course 818 is provided with in described low head 803; Export 806 places at described scavenging solution and be provided with downflow weir 816, the 4th filter course 819 is provided with in the bottom of downflow weir 816, steam pipe coil 815 is provided with in the 4th filter course 819, above the 4th filter course 819, be provided with two-layer filtration sieve plate, the sieve aperture of upper level filter sieve plate 820 is less than the sieve aperture that sieve plate 821 filters in lower floor.Described downflow weir 816 is made up of sidewall baffle plate and top flap, and described sidewall baffle plate and top flap are solid barrier.Described upper cover 802 is provided with gas phase connected entrance 822 and two observation panels 823, and the both sides being arranged on upper cover 802 of two described observation panel 823 symmetries are so that observe the filtration of filtering in molten sulphur device, molten sulphur situation.The evaporation vapour such as the moisture produced in molten sulphur process can be communicated with 822 mouthfuls of discharges from gas phase.Described filtration is melted sulphur device and is also provided with two manholes, 824, manhole 824 and is arranged on upper cover, and another manhole 824 is arranged on cylindrical shell bottom.Described upper cover 802 is ellipsoidal head, and described low head 803 is ellipsoidal head or conical head.In described filter 810, the first filter course is SNGLA type packing layer or porcelain ball filter course; The second described filter course, the 3rd filter course and the 4th filter course are SNGLB type packing layer or metal packing filter course.
Vertical pipe 2 is passed into from top from the tail gas of sulfur recovery facility solvent absorption tower top or sulphur pond tail gas or both sulfur-containing tail gas of mixing, oxidation solution in oxidation solution storage tank 6 is delivered to top and the bottom spray of vertical pipe 2, the oxidation solution being delivered to the top of vertical pipe 2 sprays downwards, the oxidation solution of downward ejection and tail gas co-current contact, be delivered to the oxidation solution upward spraying of the bottom of vertical pipe 2, the oxidation solution upwards sprayed and tail gas counter current contacting, there is oxidation reaction and generate elemental sulfur and water in the sulfur-bearing thing in tail gas and oxidation solution (hydrogen peroxide), complete first order oxidation, through the tail gas of first order oxidation, oxidizing tower 1 is entered with water together with oxidation solution with the elemental sulfur generated, tail gas through first order oxidation rises in oxidizing tower 1, the oxidation solution counter current contacting that sulfur-bearing thing in tail gas and oxidizing tower 1 top spray, complete second level oxidation, the cleaning of off-gas outlet that the tail gas again after oxidation sweetening is pushed up by oxidizing tower 1 after foam removal drains into sulfur recovery unit burning part and continues process, the elemental sulfur generated, water enter bottom oxidizing tower 1 together with oxidation solution, and the elemental sulfur offscum bottom oxidizing tower 1 on liquid level enters molten sulphur device 8 separating and filtering of filtration and obtains elemental sulfur, oxidation solution bottom oxidizing tower 1 and filtration are melted the oxidation solution after filtering in sulphur device 8 and are converged with the fresh oxidation solution from oxidation solution storage tank 6, and the equipment shower nozzle 5 being delivered to the top of the plumbing nozzle in the same way 3 at the top of vertical pipe 2, the reverse plumbing nozzle 4 of bottom and oxidizing tower 1 by oxidation solution circulating pump 7 sprays.
Described oxidation solution to be concentration be 1% ~ 10% hydrogen peroxide.
Adopt the method for the present embodiment device process sulfur recovery facility tail gas, step is as follows:
(1), from the tail gas of sulfur recovery facility solvent absorption tower top with 14116kg/h flow (wherein H in tail gas
2the flow of S is 5.51kg/h) pass into vertical pipe 2 from top, oxidation solution (5% hydrogen peroxide) in oxidation solution storage tank 6 is delivered to the top of vertical pipe 2 and bottom and oxidizing tower 1 top spray with 100t/h global cycle amount drench, the oxidation solution being delivered to the top of vertical pipe 2 sprays downwards, the oxidation solution of downward ejection and tail gas co-current contact, be delivered to the oxidation solution upward spraying of the bottom of vertical pipe 2, the oxidation solution upwards sprayed and tail gas counter current contacting, the sulfur-bearing thing in tail gas and H
2o
2there is oxidation reaction and generate elemental sulfur and water, complete first order oxidation at normal temperatures, through first order oxidation tail gas, enter oxidizing tower with water with the elemental sulfur generated together with oxidation solution.
(2) tail gas, through first order oxidation rises in oxidizing tower 1, the oxidation solution counter current contacting sprayed with oxidizing tower 1 top, complete second level normal temperature oxidation, after foam removal, tail gas sulfur-bearing substrate concentration drains into sulfur recovery unit burning part lower than the cleaning of off-gas outlet that 20ppmV is pushed up by oxidizing tower 1 and continues process, and such assimilation effect can ensure the SO after burning in final discharge flue gas
2be reduced to 35mg/Nm
3below; The elemental sulfur, the water that generate enter bottom oxidizing tower 1 together with oxidation solution, and the elemental sulfur offscum bottom oxidizing tower 1 on liquid level enters through the elemental sulfur outlet of oxidizing tower 1 lower side and filters molten sulphur device 8 separating and filtering and obtain elemental sulfur (5kg/h); Oxidation solution bottom oxidizing tower 1 with filter the oxidation solution after filtering in molten sulphur device 8 and converge from the fresh oxidation solution (the present embodiment need supplement fresh oxidation solution 150kg/h) of oxidation solution storage tank 6, be delivered to the top circulated sprinkling of the top of vertical pipe 2, bottom and oxidizing tower 1 by oxidation solution circulating pump 9.
Sulfur-bearing thing in step (1), (2) in tail gas and the generation oxidation reaction at normal temperatures of oxidation solution, described normal temperature refers to temperature 10 ~ 40 DEG C.
Above embodiment is only and technological thought of the present utility model is described, protection domain of the present utility model can not be limited with this, every technological thought according to the utility model proposes, any change that technical scheme basis is done, all falls within the utility model protection domain; The technology that the utility model does not relate to all is realized by prior art.
Claims (6)
1. a treating apparatus for sulfur recovery facility tail gas, is characterized in that comprising oxidizing tower, the vertical pipe connecting sulfur recovery facility and oxidizing tower bottom, oxidation solution storage tank, filtering molten sulphur device; The bottom being provided with plumbing nozzle, vertical pipe in the same way at the top of described vertical pipe is provided with reverse plumbing nozzle; Described oxidizing tower is hollow-spraying-tower type tower, is provided with equipment shower nozzle on the top of oxidizing tower, is provided with demister and cleaning of off-gas outlet at the top of oxidizing tower; Described oxidizing tower is connected with the sulfur-bearing liquid entrance filtering molten sulphur device through the elemental sulfur outlet of lower side, and the bottom that sulphur device is melted in described filtration is provided with the outlet of molten sulphur; The scavenging solution outlet that sulphur device bottom is melted in liquid outlet bottom described oxidizing tower and described filtration is connected through the equipment shower nozzle of oxidation solution circulating pump with the plumbing nozzle in the same way of vertical pipe, reverse plumbing nozzle and oxidizing tower; The entrance of described oxidation solution circulating pump is connected with oxidation solution storage tank.
2. the treating apparatus of sulfur recovery facility tail gas according to claim 1, is characterized in that also being provided with oxidation solution delivery pump at the export pipeline of described oxidation solution storage tank.
3. the treating apparatus of sulfur recovery facility tail gas according to claim 1, is characterized in that at least being provided with one deck plumbing nozzle in the same way on the top of described vertical pipe, is at least provided with the reverse plumbing nozzle of one deck in the bottom of described vertical pipe; One deck equipment shower nozzle is at least provided with on the top of described oxidizing tower.
4. the treating apparatus of sulfur recovery facility tail gas according to claim 1, is characterized in that being provided with two-layer plumbing nozzle in the same way on the top of described vertical pipe, is provided with the reverse plumbing nozzle of one deck in the bottom of described vertical pipe; Two to three-layer equipment shower nozzle is provided with on the top of described oxidizing tower.
5. the treating apparatus of sulfur recovery facility tail gas according to claim 1, is characterized in that described filtration melts the number of sulphur device for two or more.
6. the treating apparatus of sulfur recovery facility tail gas according to claim 1, is characterized in that also comprising oxidation solution filter Sum decomposition device at the treating apparatus of described sulfur recovery facility tail gas; Arrange bypass at the outlet line of described oxidation solution circulating pump, described bypass is connected with the liquid-inlet of oxidation solution filter, and the liquid outlet of described oxidation solution filter is connected with decomposer, oxidation solution storage tank respectively through two pipelines in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520412748.2U CN204746071U (en) | 2015-06-15 | 2015-06-15 | Processing apparatus of sulphur recovery unit tail gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520412748.2U CN204746071U (en) | 2015-06-15 | 2015-06-15 | Processing apparatus of sulphur recovery unit tail gas |
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| CN204746071U true CN204746071U (en) | 2015-11-11 |
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| CN201520412748.2U Active CN204746071U (en) | 2015-06-15 | 2015-06-15 | Processing apparatus of sulphur recovery unit tail gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US11266946B2 (en) | 2018-05-16 | 2022-03-08 | Saudi Arabian Oil Company | Purification of gases containing sulfur compounds |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11266946B2 (en) | 2018-05-16 | 2022-03-08 | Saudi Arabian Oil Company | Purification of gases containing sulfur compounds |
| US11607643B2 (en) | 2018-05-16 | 2023-03-21 | Saudi Arabian Oil Company | Purification of gases containing sulfur compounds |
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