CN101898079B - Treatment method of storage tank-dissipating stinking sulfur-containing waste gas - Google Patents
Treatment method of storage tank-dissipating stinking sulfur-containing waste gas Download PDFInfo
- Publication number
- CN101898079B CN101898079B CN2009100117616A CN200910011761A CN101898079B CN 101898079 B CN101898079 B CN 101898079B CN 2009100117616 A CN2009100117616 A CN 2009100117616A CN 200910011761 A CN200910011761 A CN 200910011761A CN 101898079 B CN101898079 B CN 101898079B
- Authority
- CN
- China
- Prior art keywords
- bubbling
- liquid
- waste gas
- uptake zone
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a treatment method of storage tank-dissipating stinking sulfur-containing waste gas, which comprises the steps that: under the action of a pipeline pressure controller at a waste gas inlet, a fan is started up, with the help of the power provided by the fan, hydrogen sulfide and organic sulfide in the waste gas are purified by using an efficient bubble column, moisture in the waste gas is then removed by preliminary condensation and hydrocarbon components in the waste gas are further condensed and recovered, and in the end, the purifying gas is exhausted; the bubble column is a counter current pulse bubble absorption column, and gas phase is dispersed via a nozzle of the absorption column and then subject to contact oxidation together with absorbent in a bubble absorption area in order to absorb sulfur-containing compounds therein, and the nozzle of the bubble absorption column is structured as bubble pulse valve. The method according to the invention has simple flow and high treatment efficiency, can be used for the purification of sulfide and hydrocarbon mixed gas thereof in the process of various productions, and is particularly suitable for the purification of waste gas dissipated from the tanks in oil refining company, such as processing device, waste oil tank, sulfur-containing sewage tank, crude diesel tank, crude gasoline tank, etc.
Description
Technical field
The present invention relates to the method, the particularly processing method of the foul waste gas of harmful constituents such as organic sulfur compound such as sulfide hydrogen, methyl mercaptan and hydro carbons of the sulfur-containing foul waste gas processing of chemical storage tank loss.
Background technology
Oil plant contains various storage tanks such as sour water jar, oil product pans etc. are that important foul gas distributes the source; The pollutant such as volatile hydrocarbon, hydrogen sulfide, organic sulfur compound, ammonia that contains higher concentration in the foul gas that distributes; The worker is long-term movable in the environment that is polluted by these materials; Possibly cause diseases such as respiratory system, digestive system, reproductive system, also possibly cause body disease and carcinogenic; When seriously polluted, also can make the people produce dizziness, larynx painful, feel sick, acute poisoning symptom such as vomiting.
These waste gas components are complicated, not only cause surrounding enviroment odor pollution, health is threatened, and cause huge hydrocarbon loss.Therefore the improvement of this type waste gas is also more and more urgent.
Traditional exhaust gas treatment method such as absorption method, burning method, Production by Catalytic Combustion Process, condensation method, absorption process etc. can not well be administered this type waste gas.The used adsorbent of existing absorption method exists potential safety hazard, and similar incidents took place in practical application the spontaneous combustion problem as adsorbent causes.There is high, the less economical shortcoming of energy consumption in burning method.Though the Production by Catalytic Combustion Process energy consumption reduces, waste gas component is complicated, the easy poison deactivation of catalyst.Condensation method and absorption process only can be removed the part component in this type of waste gas.
CN01127539.1 has introduced a kind of method that purifies hydrogen sulfide, and CN1133568A has introduced the method that a kind of absorption process is removed hydrogen sulfide.CN91110451.8 has introduced the method for recovering solvents in a kind of hydro carbons process.These methods all only can be removed hydrogen sulfide or hydro carbons, can not purify simultaneously.
2005 28 the 4th phases of volume of " petrochemical industry environmental protection " magazine have been introduced the improvement method that adopts absorption process purification of sulphur-containing sewage jar waste gas.This method adopts the secondary absorption process to handle acid water pot waste gas, and absorbent is an alkaline solution.The tail gas that several sour water jars and alkaline residue jar are extracted through jet pump earlier with alkali lye blended absorbent in venturi mixer; In alkali liquid tank, carry out gas-liquid separation; Absorb processing through one-level alkali lye absorption tower and secondary deodorant absorption tower then, be pooled to the laggard smoke stack emission of deodorant jar gas-liquid separation at last.But this technology only can transform the sulfide oxidation that absorbs, but does not remove the ability of hydro carbons.
" design of sulphur phosphorus and powder technology " the 6th phase in 2004 has been introduced the waste gas that adopts solid absorbent adsorption cleaning sour water jar.This method adopts the swage adsorbent that this waste gas is handled, and has obtained certain effect.But this method only purifies hydrogen sulfide, and other pollutant does not purify, and also there is safety problem in adsorbent.
Said method can not discharge the volatile hydrocarbon material in the gas by effective elimination, and this causes certain environmental pollution on the one hand, has wasted precious resources on the other hand.For the processing method of hydrocarbon gas, traditional volatile hydrocarbon recovery technology mainly comprises three types: the one, and condensation method reclaims, and adopts two-stage or the condensation of three grades of mechanical refrigeration degree of depth, with the major part hydrocarbon condensing and recycling of volatilizing; The 2nd, absorption process reclaims, and adopts various The suitable solvent to absorb the volatilization hydrocarbon; The 3rd, absorption is reclaimed, and adopts various suitable solid absorbents such as charcoal absorption volatilize hydrocarbon, regeneration then.Three types technology respectively has its advantage and deficiency, on the basis of these three kinds of technology, has various improvement technologies to produce again, aspect adsorption technology, is mainly developing to some extent aspect technology and the adsorbent two.
CN01100559.9 adopts traditional condensation method to carry out hydro carbons and reclaims, and after precooling-deep cooling condensed in two stages was adopted in this invention, condensation temperature reached-70 ℃, then, discharged through after the charcoal absorption.This method can make discharging gas hydro carbons concentration up to standard.
CN03254728.5 and CN03254729.3 have proposed the device that a kind of absorption method oil gas reclaims respectively, adopt active carbon as adsorbent, and the hydro carbons behind the vacuum desorption absorbs as liquefied gas or diesel oil.With active carbon or NACF is adsorbent, and its advantage is that adsorbance is bigger, and adsorption efficiency is higher, and discharging tail gas reaches the environmental protection index requirement easily.But when its deficiency was in the running to be difficult to the higher oil gas of control absorption temperature rise, particularly adsorption concentration, the active carbon bed temperature was very high, and tangible potential safety hazard is arranged.
CN200410023944.7 has narrated a kind of device for recovering oil and gas, and import is equipped with flowmeter, and outlet is equipped with densimeter, is single tower.Though this patent import has the tonifying Qi safety measure, but still hot-spot in the inevitable bed, cause the charcoal spontaneous combustion and cause danger.
A kind of method that CN02805902.6 proposes the steam desorb of charcoal absorption waste gas and reclaims.There is the dangerous safety problem of the above-mentioned too high initiation of heat of adsorption in this patent during to the higher hydro carbons waste gas purification of concentration equally.
Above-mentioned these oil-gas recovery methods are only applicable to the recovery and the purification of pure hydro carbons volatile component; Containing high-concentration hydrogen sulfide and hydro carbons waste gas and be not suitable for for loss such as oil refining enterprise oil product storage tank, slop tanks; When handling sulfide hydrogen waste gas, there is etching problem, in the active carbon adsorption like condensation method; The also easy adsorption of hydrogen sulfide of active carbon itself, the general technology of vacuumizing can't be regenerated to active carbon preferably.
Summary of the invention
Deficiency to above-mentioned prior art; The present invention provides the purification method of a kind of chemical storage tank loss sulfur-bearing and hydro carbons foul waste gas; Be used for the sulfide that various production processes produce and the purified treatment of sulfide and hydro carbons mist, be specially adapted to the purified treatment of storage tank loss waste gas such as oil refining enterprise processing unit (plant), slop tank, sour water jar, gas-oil jar, raw gasoline jar.
Treatment method of storage tank-dissipating stinking sulfur-containing waste gas of the present invention comprises following content: at blower fan waste gas employing bubble tower purification hydrogen sulfide and organic sulfur compound under the power are provided; Remove moisture in the waste gas through preliminary condensation then; Hydrocarbon component in the further again condensing and recycling waste gas, the discharging of final purification gas.Blower fan is arranged on the bubble absorbing tower waste gas outlet pipeline, and the startup of blower fan is by the pressure controller control that is arranged on the bubble absorbing tower exhaust gas entrance.
In the purification method of the foul waste gas of chemical storage tank loss sulfur-bearing of the present invention and hydro carbons, the startup of blower fan is associated with pressure inductor on the exhaust gas entrance pipeline.When pressure was high, rotation speed of fan increased, and treating capacity increases, and when pressure hanged down, rotation speed of fan reduced, and treating capacity reduces.The absorption tower evenly disperses gas phase through suitable nozzle arrangements in liquid phase, improved gas-liquid contact effect greatly, has improved absorptivity and operating flexibility, has reduced equipment scale, has saved occupation of land.
In the purification method of the foul waste gas of chemical storage tank loss sulfur-bearing of the present invention and hydro carbons, absorbent is an alkaline solution, can contain oxidant simultaneously in the absorbent, and alkaline solution is selected from and contains NaOH, KOH, K
2CO
3, Na
2CO
3, NaHCO
3, KHCO
3In one or more solution, alkaline matter concentration is 0.5%～50% (weight), preferred 1%～30%.Oxidant is selected from NaClO, H
2O
2, ClO
2, sulfonated phthalocyanine cobalt, molysite, KMnO
4Deng among one or more, oxidant concentration is 0～30% (weight), and is preferred 0.5%～20%, most preferably 1%～10%.
In the purification method of the foul waste gas of chemical storage tank loss sulfur-bearing of the present invention and hydro carbons; Condensation removes water vapour and the condensing and recycling hydro carbons can adopt existing condensation technology; The condensation temperature that condensation removes water vapour is 0～10 ℃, and the condensation temperature of condensing and recycling hydro carbons is-75～-55 ℃.
In the purification method of the foul waste gas of chemical storage tank loss sulfur-bearing of the present invention and hydro carbons, the operating pressure that condensation removes water vapour and condensing and recycling hydro carbons is 0～100KPaG (G representes gauge pressure).
In the purification method of the foul waste gas of chemical storage tank loss sulfur-bearing of the present invention and hydro carbons, adopt adverse current pulsed bubbling absorption tower, gas phase through after the nozzle dispersion on absorption tower with absorbent in the bubbling uptake zone catalytic oxidation, absorb sulfur-containing compound wherein.The nozzle of bubble absorbing tower is a bubbling pulse valve structure; The bubbling pulse valve comprises that the bottom passes the logical tube of circle, heavy ball and the heavy ball limited cap of bubbling uptake zone column plate; Circular logical tube top movable is placed the sealing heavy ball, and the heavy ball limited cap is arranged on the heavy ball top, and heavy ball limited cap and heavy ball top are provided with suitable space; Heavy ball can be free movable between circle logical tube open upper end and heavy ball limited cap; The heavy ball limited cap is fixedly connected with circular logical tube, and the heavy ball limited cap is offered sieve aperture, and absorbent flows downward through the downspout that is arranged on the bubbling uptake zone column plate.
The inventive method adverse current pulsed bubbling can be provided with 1～5 grade of bubbling uptake zone in the absorption tower, and the height of liquid layer of every grade of bubbling uptake zone can be 100～1000mm, preferred 200～600mm, and absorption tower inlet liquid gas volume ratio is 50～500L/m
3, operating temperature can be carried out at ambient temperature.
The inventive method is through the suitable process combination of employing, and the capital equipment structure optimization design, has improved exhaust-gas treatment efficient, has reduced operating cost.Particularly use custom-designed pulsed bubbling absorption tower; This absorption tower is evenly dispersed in waste gas in the absorbent through suitable nozzle arrangements, has improved gas-liquid contact effect greatly, has improved absorptivity and operating flexibility; Reduce equipment scale, saved occupation of land.
Description of drawings
Fig. 1 is a kind of process chart of the present invention.
Fig. 2 is the installation diagram of a kind of concrete structure pulsed bubbling tower of the inventive method use.
Fig. 3 is a bubbling uptake zone tower tray modular construction sketch map.
Fig. 4 drenches liquid dish structural representation for the bubbling uptake zone.
Fig. 5 spatters plate dispensing arrangement sketch map for what drench the liquid dish.
Wherein: 1 is the gas outlet, and 2 is the upper end end socket, and 3 is demister, and 4 is the liquid phase distributor, and 5 is bubbling uptake zone tower tray assembly; 6 for drenching the liquid dish, and 7 is liquid seal trough, and 8 is downspout, and 9 is cylindrical shell, and 10 is vapor distributor; 11 is air inlet, and 12 is low head, and 13 is liquid outlet, and 5-1 is a bubbling uptake zone column plate, and 5-2 is the circular logical tube of bubbling pulse valve; 5-3 is heavy ball, and 5-4 is the heavy ball limited cap, and 6-1 is the cylindrical shape cofferdam, and 6-2 is for drenching the liquid column plate, and 6-3 is for spattering the plate distributor; 6-3-1 is a pull bar, and 6-3-2 is that plate is spattered on top, and 6-3-3 is that plate is spattered in the centre, and 6-3-4 is that plate is spattered in the bottom.
The specific embodiment
When exhaust gas pressure reaches certain value in the chemical storage tank; Start blower fan c through pressure inductor a, under blower fan provided power, waste gas got into through blower fan through bubble absorbing tower and removes water condenser d dehydration; Waste gas after the dehydration gets into hydrocarbon and reclaims condenser e; At condenser e, a large amount of hydro carbons become liquid, are reclaimed by the bottom.Absorbent is squeezed into the absorption tower through lye pump g, gets into alkali lye storage tank f behind the absorption sulfide, and circulation absorbs.
A kind of concrete structure on the pulsed bubbling absorption tower that the inventive method is used comprises cylindrical shell, vapor distributor, liquid phase distributor, downspout and at least one bubbling uptake zone, and in order to reach suitable absorptivity, the bubbling uptake zone is traditionally arranged to be 2～5 layers; Vapor distributor is arranged on the cylindrical shell bottom; The liquid phase distributor is arranged on cylindrical shell top, and the bubbling uptake zone is arranged between vapor distributor and the vapor distributor, and bottom, bubbling uptake zone is the tower tray assembly; The tower tray assembly comprises bubbling uptake zone column plate and the nozzle of distributed and arranged on bubbling uptake zone column plate; Nozzle is a bubbling pulse valve structure, and bubbling pulse valve structure comprises that the bottom passes the logical tube of circle, heavy ball and the heavy ball limited cap of bubbling uptake zone column plate, and circular logical tube top movable is placed a sealing heavy ball; The heavy ball limited cap is arranged on the heavy ball top; Heavy ball limited cap and heavy ball top are provided with suitable space, and heavy ball can be free movable between circle logical tube open upper end and heavy ball limited cap, and the heavy ball limited cap is fixedly connected with circular logical tube; The heavy ball limited cap is offered sieve aperture, and downspout is the logical barrel structure through bubbling uptake zone column plate.The corrosion resistant steel ball of the suitable employing of heavy ball.
In the bubble tower; Below at least one bubbling uptake zone (being bubbling uptake zone layer), spray section is set; Below the bubbling uptake zone, be provided with and drench the liquid dish, downspout imports the liquid on the bubbling uptake zone and drenches the liquid dish, drenches the liquid dish liquid dispersion is contacted with the gas phase that upwards flows.The structure of drenching the liquid dish comprises drenches liquid column plate, cylindrical shape cofferdam and spatters the plate distributor; Cylindrical shape cofferdam distributed and arranged is being drenched on the liquid column plate; The inner pouring liquid column plate in cylindrical shape cofferdam is provided with opening, and the opening below is hung and spattered the plate distributor, and upper end, cylindrical shape cofferdam has the V-arrangement teeth groove.Spatter that the plate distributor spatters plate by at least one and pull bar constitutes, pull bar will spatter the plate distributor to be hung drenching liquid column plate bottom, spatters and offers sieve aperture on the plate.
The liquid level that downspout open upper end height need be controlled according to the bubbling uptake zone confirms that open upper end is offered the V-arrangement teeth groove, and the downspout lower end is provided with liquid seal trough.
Bubble tower top is provided with inlet and gas outlet, and the bottom is provided with air inlet and liquid outlet, and vapor distributor communicates with air inlet, and the liquid phase distributor communicates with inlet.The liquid phase distributor is made up of ring pipe, adapter and flange; The ring pipe lower surface is offered some apertures.Vapor distributor is made up of concetrated pipe, some arms and flange; The arm lower surface is offered some apertures.
Spatter the plate distributor and can be the multi-deck screen plate structure, several layers spatter plate from top to bottom its diameter successively decrease, and with pull bar several layers is spattered plate and links together.Liquid seal trough is made up of cylindrical shell and circular bottom plate, and several V-type teeth groove are offered in the cylindrical shell upper edge of liquid seal trough.
The sieve diameter that the heavy ball limited cap is offered is φ 1～φ 5mm, and preferred diameter is φ 3mm, and percent opening 10%～50% is preferably 30%.Downspout is tubular, and several V-type teeth groove are offered in the downspout upper edge, do not have changeover portion between teeth groove, 30 °～120 ° of teeth groove angles, preferred 60 °, tooth depth 3mm～20mm, preferred 10mm.Drench upper edge, liquid dish cylindrical shape cofferdam and offer several V-type teeth groove, do not have changeover portion between teeth groove, 30 °～120 ° of teeth groove angles, preferred 60 °, tooth depth 3mm～10mm, preferred 5mm.Spattering the plate distributor is the multi-deck screen plate structure, spatters to offer sieve aperture on the plate, and sieve diameter is φ 5mm, and percent opening 20%～50% is preferably 30%.Several layers sieve plate its diameter from top to bottom successively decreases, and with pull bar several layers is spattered plate and link together.Liquid seal trough is made up of cylindrical shell and circular bottom plate.Several V-type teeth groove are offered in the cylindrical shell upper edge of liquid seal trough, do not have changeover portion between teeth groove, 30 °～120 ° of teeth groove angles, preferred 60 °, tooth depth 3mm～20mm, preferred 10mm.Liquid seal trough is welded on and drenches on the liquid dish, and is higher than pouring liquid dish certain altitude, makes liquid seal trough top form the profile of tooth weir plate.
Bubble tower of the present invention is when work, and liquid phase enters into the liquid phase distributor that is arranged on cylindrical shell top through inlet, and some holes in spraying of offering from the ring pipe lower surface are spread across bed; Gas phase enters into vapor distributor from the tower bottom import, offers being distributed in the tower of some apertures from concetrated pipe arm lower surface.Downspout exceeds bubbling uptake zone column plate certain altitude, and liquid phase forms liquid layer on bubbling uptake zone column plate, and several V-type teeth groove are offered in the downspout upper edge, and whole bed liquid phase is evenly flowed.Gas phase is passed and is spattered the plate distributor, gets into the bubbling pulse valve, generates bubble at heavy ball limited cap place; Be distributed in the liquid layer on the bubbling uptake zone column plate,, heavy ball be in the unsettled air-flow because the heavy ball limited cap is provided with sieve aperture; The heavy ball meeting continuously opens and closes, and gas phase forms pulsating flow, on bubbling uptake zone column plate, generates evenly and the bubble of coalescence not; Gas-liquid two-phase is realized the bubbling contact at this, carries out mass transfer and reaction.When tolerance (pressure) reduced, pulse valve cut out automatically, to gas phase time of gathering was provided, and when tolerance (pressure) reaches when numerical value is set, pulse valve is opened automatically, and therefore, exercisable scope is very wide.
From flowing to liquid seal trough, the cylindrical shell upper edge of liquid seal trough is higher than drenches the liquid dish to liquid phase from downspout, and the cylindrical shell upper edge offers several V-type teeth groove, and liquid phase is evenly distributed to drenches on the liquid dish.Liquid phase is evenly distributed to each and spatters on the plate distributor, and liquid phase drops down onto in gravity effect tenesmus spatters on the plate, forms splash stream, forms countercurrent spray with from bottom to top gas phase and contact realization mass transfer and reaction.Said structure organically is combined in two kinds of gas-liquid contact mass transfer means of bubbling and spray in the equipment, has made full use of the device space simultaneously, has improved the serviceability of equipment.
The pulsed bubbling tower that the inventive method is used is provided with some inner members according to gas-liquid mass transfer and reaction process characteristics, and during work, liquid phase enters into the liquid phase distributor that is arranged on cylindrical shell top through inlet, is sprayed onto bed; Gas phase enters into vapor distributor from the tower bottom import, is distributed in the tower.Downspout exceeds the column plate certain altitude, and liquid phase forms liquid layer on bubbling uptake zone column plate; Several bubbling pulse valves have been installed on the bubbling uptake zone column plate; Form air chamber between bubbling uptake zone column plate and pouring liquid column plate; Open and close along with the bubbling pulse valve; This air chamber internal pressure generation rule property fluctuation, gas phase form pulsating flow, make evenly and not coalescence of the bubble that generates in the liquid layer of gas phase on bubbling uptake zone column plate; Gas-liquid two-phase is realized the bubbling contact at this, carries out mass transfer and reaction.From flowing to liquid seal trough, the cylindrical shell upper edge of liquid seal trough is higher than drenches the liquid column plate to liquid phase from downspout, and liquid phase is evenly distributed to drenches on the liquid column plate, drench cylindrical shape cofferdam and respective numbers be set on the liquid column plate spatter the plate distributor; Liquid phase stream is gone into the cofferdam and is dropped down onto in gravity effect tenesmus and spatter on the plate, forms splash stream, forms countercurrent spray with from bottom to top gas phase and contact realization mass transfer and reaction.So far accomplish the bubbling-spray contact process of a bed.Above-mentioned mass transfer structure (realizing the structure and the structure that realizes spray of bubbling) is processed the vertical multi-stage cascaded structure, and gas-liquid two-phase is realized bubbling-spray contact process repeatedly, and realization liquid phase and gas phase are accomplished top-down adverse current " bubbling-spray " haptoreaction.This pulsed bubbling tower helps gaseous pressure is transformed the power of gas phase dispersion, and is simultaneously in same mass transfer apparatus that two kinds of gas-liquid way of contact combinations, gas liquid contacting efficiency are high.
Certain slop tank tidal air sulfide hydrogen 1000mg/m of enterprise
3, hydrocarbon-containifirst 20v% (volume fraction), flow are 100Nm
3About/h.Adopt tertiary vein towards bubble absorbing tower, comprise three bubbling uptake zones and three spray uptake zones, the absorption tower inner member is confirmed by preference data in the specific embodiment.Bubbling uptake zone liquid phase layer thickness is 350mm, and the spray section height is 250mm.Absorbent is a 5%NaOH solution, and liquid-gas ratio is 100L/m
3, operating temperature is 25 ℃.Waste gas after the absorption is through behind condensation dehydration and the condensing and recycling hydrocarbon, and 2 ℃ of dehydration condenser chilling temperatures reclaim hydrocarbon condenser condenses temperature-75 ℃, the direct emptying of fixed gas on a small quantity.
After absorption condensation is handled; Slop tank tidal air hydrogen sulfide purifying rate 100%; The hydro carbons rate of recovery reaches 96% (quality); Annual about 300 tons of the hydro carbons that reclaim, tail gas from absorption tower is a normal pressure, tail gas concentration and mass rate of emission all meet " storage tank farm atmosphere pollutants emission standards " (GB20950-2007) exhaust of oil standard.
Certain sour water jar tidal air sulfide hydrogen 1000mg/m of enterprise
3, methyl mercaptan 200mg/m
3, methyl disulfide 50mg/m
3, hydro carbons 10v%, flow are 150Nm
3About/h.Adopt tertiary vein towards bubble absorbing tower, comprise three bubbling uptake zones and three spray uptake zones, the absorption tower inner member is confirmed by preference data in the specific embodiment.Bubbling uptake zone liquid phase layer thickness is 350mm, and the spray section height is 250mm.Absorbent is the solution that contains 5%NaOH, 10%NaClO, 5% sulfonated phthalocyanine cobalt, and liquid-gas ratio is 50L/m
3, operating temperature is 25 ℃.Waste gas after the absorption is through behind condensation dehydration and the condensing and recycling hydrocarbon, and 2 ℃ of dehydration condenser chilling temperatures reclaim hydrocarbon condenser condenses temperature-75 ℃, condenser operating pressure 50kPaG, the direct emptying of fixed gas on a small quantity at last.
After absorption condensation is handled, slop tank tidal air hydrogen sulfide and methyl mercaptan purifying rate 100%, methyl disulfide purifying rate 99%, the hydro carbons rate of recovery 97%.Exhaust emissions speed all meets Purge gas and meets the current national discharge standard.
Claims (10)
1. treatment method of storage tank-dissipating stinking sulfur-containing waste gas; Comprise following content: waste gas employing bubble tower purification hydrogen sulfide and organic sulfur compound under the power are provided at blower fan; Remove moisture in the waste gas through preliminary condensation then; Hydrocarbon component in the further again condensing and recycling waste gas, the discharging of final purification gas; Wherein bubble tower is adverse current pulsed bubbling absorption tower; Gas phase through after the nozzle dispersion on absorption tower with absorbent in the bubbling uptake zone catalytic oxidation, absorb sulfur-containing compound wherein; The nozzle of bubble absorbing tower is a bubbling pulse valve structure, and the bubbling pulse valve comprises that the bottom passes the logical tube of circle, heavy ball and the heavy ball limited cap of bubbling uptake zone column plate, and circular logical tube top movable is placed a sealing heavy ball; The heavy ball limited cap is arranged on the heavy ball top; Heavy ball limited cap and heavy ball top are provided with suitable space, and heavy ball can be free movable between circle logical tube open upper end and heavy ball limited cap, and the heavy ball limited cap is fixedly connected with circular logical tube; The heavy ball limited cap is offered sieve aperture, and absorbent flows downward through the downspout that is arranged on the bubbling uptake zone column plate;
In the bubble tower, below at least one bubbling uptake zone, spray section is set, below the bubbling uptake zone, is provided with and drenches the liquid dish, downspout imports the liquid on the bubbling uptake zone and drenches the liquid dish, drenches the liquid dish liquid dispersion is contacted with the gas phase that upwards flows; The structure of drenching the liquid dish comprises drenches liquid column plate, cylindrical shape cofferdam and spatters the plate distributor; Cylindrical shape cofferdam distributed and arranged is being drenched on the liquid column plate; The inner pouring liquid column plate in cylindrical shape cofferdam is provided with opening, and the opening below is hung and spattered the plate distributor, and upper end, cylindrical shape cofferdam has the V-arrangement teeth groove; Spatter that the plate distributor spatters plate by at least one and pull bar constitutes, pull bar will spatter the plate distributor to be hung drenching liquid column plate bottom, spatters and offers sieve aperture on the plate.
2. according to the described method of claim 1, it is characterized in that: absorbent is an alkaline solution, and alkaline solution contains NaOH, KOH, K
2CO
3, Na
2CO
3, NaHCO
3, KHCO
3In one or more solution, the alkaline matter weight concentration is 0.5%～50%.
3. according to claim 1 or 2 described methods, it is characterized in that: contain oxidant in the absorbent, oxidant is selected from NaClO, H
2O
2, ClO
2, sulfonated phthalocyanine cobalt, molysite and KMnO
4Among one or more, the oxidant weight concentration is 0～30%.
4. according to the described method of claim 3, it is characterized in that: absorbent neutral and alkali material concentration is 1%～30%, and oxidant concentration is 0.5%～20%.
5. according to the described method of claim 1, it is characterized in that: the condensation temperature that condensation removes moisture is 0～10 ℃, and the condensation temperature of condensing and recycling hydro carbons is-75～-55 ℃.
6. according to the described method of claim 1, it is characterized in that: the height of liquid layer of bubbling uptake zone is 100～1000mm in the pulsed bubbling absorption tower, and absorption tower inlet liquid gas volume ratio is 50～500L/m
3
7. according to claim 1 or 6 described methods; It is characterized in that: the pulsed bubbling absorption tower comprises cylindrical shell, vapor distributor, liquid phase distributor, downspout and at least one bubbling uptake zone; Vapor distributor is arranged on the cylindrical shell bottom, and the liquid phase distributor is arranged on cylindrical shell top, and the bubbling uptake zone is arranged between vapor distributor and the vapor distributor; Bottom, bubbling uptake zone is the tower tray assembly, and the tower tray assembly comprises bubbling uptake zone column plate and the nozzle of distributed and arranged on bubbling uptake zone column plate.
8. according to the described method of claim 7, it is characterized in that: the bubbling uptake zone is set to 2～5 layers.
9. according to the described method of claim 7, it is characterized in that: the liquid level that downspout open upper end height need be controlled according to the bubbling uptake zone confirms that open upper end is offered the V-arrangement teeth groove, and the downspout lower end is provided with liquid seal trough.
10. according to the described method of claim 1, it is characterized in that: blower fan is arranged on the bubble absorbing tower waste gas outlet pipeline, and the startup of blower fan is by the pressure controller control that is arranged on the bubble absorbing tower exhaust gas entrance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100117616A CN101898079B (en) | 2009-05-25 | 2009-05-25 | Treatment method of storage tank-dissipating stinking sulfur-containing waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100117616A CN101898079B (en) | 2009-05-25 | 2009-05-25 | Treatment method of storage tank-dissipating stinking sulfur-containing waste gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101898079A CN101898079A (en) | 2010-12-01 |
| CN101898079B true CN101898079B (en) | 2012-05-30 |
Family
ID=43224203
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009100117616A Active CN101898079B (en) | 2009-05-25 | 2009-05-25 | Treatment method of storage tank-dissipating stinking sulfur-containing waste gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101898079B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489130A (en) * | 2011-12-27 | 2012-06-13 | 江苏惠利特环保科技有限公司 | Processing method of oil-containing stink |
| CN103470951B (en) * | 2013-09-13 | 2016-04-20 | 新疆敦华石油技术股份有限公司 | A kind of accumulator tank Waste resources reused utilized device |
| CN107503209B (en) * | 2017-09-11 | 2019-03-29 | 天津科技大学 | A method of cellulose micro-nano fibril is prepared using Glycyrrhiza uralensisFisch residue |
| CN109847558A (en) * | 2017-11-30 | 2019-06-07 | 中国石油天然气股份有限公司 | Hydrogen sulfide removal system and process for storage tank |
| CN109289504A (en) * | 2018-08-31 | 2019-02-01 | 江苏新久扬环保设备科技有限公司 | A kind of sulfur-containing oil-gas recyclable device and technique |
| CN114130187B (en) * | 2020-09-04 | 2022-12-13 | 中国石油化工股份有限公司 | Device and method for converting organic sulfur in blast furnace gas and method for regenerating organic sulfur conversion catalyst |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3325155A (en) * | 1962-05-07 | 1967-06-13 | Equipment Des Ind Chimiques S | Valve tray apparatus |
| US4201626A (en) * | 1978-08-24 | 1980-05-06 | Uop Inc. | Liquid-liquid contacting apparatus |
| CN2313653Y (en) * | 1997-11-11 | 1999-04-14 | 郭彦书 | Gas-liquid contact controller |
| CN1594077A (en) * | 2004-07-05 | 2005-03-16 | 湖北省化学研究院 | Hydrocarbon trap method for carbon dioxide for foodstuff |
| CN101259364A (en) * | 2008-04-16 | 2008-09-10 | 中冶华天工程技术有限公司 | Wet desulphurization technique for sintered flue gas |
| CN101259367A (en) * | 2008-04-17 | 2008-09-10 | 东北电力大学 | Technique and device for simultaneously removing malodor of multiple gas mixture |
| CN101434381A (en) * | 2008-10-24 | 2009-05-20 | 上海华畅环保设备发展有限公司 | Short process flow recycle hydrogen desulfuration method and apparatus |
-
2009
- 2009-05-25 CN CN2009100117616A patent/CN101898079B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3325155A (en) * | 1962-05-07 | 1967-06-13 | Equipment Des Ind Chimiques S | Valve tray apparatus |
| US4201626A (en) * | 1978-08-24 | 1980-05-06 | Uop Inc. | Liquid-liquid contacting apparatus |
| CN2313653Y (en) * | 1997-11-11 | 1999-04-14 | 郭彦书 | Gas-liquid contact controller |
| CN1594077A (en) * | 2004-07-05 | 2005-03-16 | 湖北省化学研究院 | Hydrocarbon trap method for carbon dioxide for foodstuff |
| CN101259364A (en) * | 2008-04-16 | 2008-09-10 | 中冶华天工程技术有限公司 | Wet desulphurization technique for sintered flue gas |
| CN101259367A (en) * | 2008-04-17 | 2008-09-10 | 东北电力大学 | Technique and device for simultaneously removing malodor of multiple gas mixture |
| CN101434381A (en) * | 2008-10-24 | 2009-05-20 | 上海华畅环保设备发展有限公司 | Short process flow recycle hydrogen desulfuration method and apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101898079A (en) | 2010-12-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101898071B (en) | Method for treating sulfur- and hydrocarbon-containing foul waste gas | |
| CN101450275B (en) | Method for treating stink waste gas containing sulfur and dust | |
| CN101898079B (en) | Treatment method of storage tank-dissipating stinking sulfur-containing waste gas | |
| CN101347708B (en) | Method for processing sulphur-containing exhaust air with fetor escaped from storage tank | |
| CN101898084B (en) | Multi-component stink exhaust gas biological purifying method | |
| CN102309913A (en) | Treatment method for stinky waste gas containing sulfides and hydrocarbons | |
| CN102309914B (en) | Treatment method for stinky waste gas discharged by storage tank | |
| CN101143297B (en) | Sewage storage tank exhaust air-release purification processing method | |
| CN102728196A (en) | Gas-liquid mass transfer reactor and exhaust gas treatment method | |
| CN204619569U (en) | The exhaust treatment system that a kind of epoxychloropropane produces in producing | |
| CN102553390A (en) | Process for purifying chemical tail gas | |
| CN110585861A (en) | Coking waste gas treatment system and treatment method | |
| CN102039077A (en) | Method for treating malodorous waste gas containing hydrocarbon | |
| CN201529486U (en) | Waste gas purification apparatus | |
| NO167496B (en) | PROCEDURE FOR THE REMOVAL OF SO2 FROM GAS CURRENTS. | |
| CN101239271B (en) | Cleaning treatment method of acid sewage storage tank discharging gas | |
| CN108939867B (en) | Treatment method of volatile sulfur-containing organic waste gas | |
| CN102908882A (en) | Treatment method for emissions of sour water storage tank | |
| CN204952588U (en) | Processing system who contains VOCs waste gas | |
| CN210751969U (en) | Naphthalene-containing waste gas treatment system | |
| CN212790409U (en) | Waste gas treatment device for coal chemical industry sewage treatment | |
| CN204865437U (en) | Extension active carbon life's device | |
| CN211612166U (en) | Coking waste gas treatment system | |
| CN103223287A (en) | Purifying and recovering device of exhaust gas comprising toluene, and exhaust gas purifying and recovering method | |
| CN204294114U (en) | A kind of device for administering sulfur-bearing water pot discharge gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |