CN106474896A - The processing method of sulfide hydrogen hydrocarbon-contained waste gas - Google Patents
The processing method of sulfide hydrogen hydrocarbon-contained waste gas Download PDFInfo
- Publication number
- CN106474896A CN106474896A CN201510769162.6A CN201510769162A CN106474896A CN 106474896 A CN106474896 A CN 106474896A CN 201510769162 A CN201510769162 A CN 201510769162A CN 106474896 A CN106474896 A CN 106474896A
- Authority
- CN
- China
- Prior art keywords
- gas
- bed
- waste gas
- tower
- rotary shaft
- 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.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a kind of processing method of sulfide hydrogen hydrocarbon-contained waste gas, comprises the steps：Gas-oil or rough coal oil enter rotary drill reactor carries out devolatilization pretreatment；The material that rotary drill reactor liquid-phase outlet is discharged enters absorption equipment as absorbent, contacts with sulfide hydrogen hydrocarbon-contained waste gas and is reacted, and the rich lyosoption that absorption equipment is discharged enters hydrogenation plant and processed；Entrance crystallizing tower after the material that rotary drill reactor gaseous phase outlet is discharged and the waste gas mixing that absorption equipment is discharged, is contacted with ammonia and is reacted, the waste gas qualified discharge that discharges after process.The inventive method process is simple, and economical rationality is suitable for the absorption process handling process of sulfide hydrogen hydrocarbon-contained waste gas.
Description
Technical field
The present invention relates to a kind of processing method of waste gas, particularly a kind of method for processing sulfide hydrogen hydrocarbon-contained waste gas.
Background technology
Various oil product storage tanks, sump oil basin, oil article vehicle（Ship）, oil product processing and some chemical processes etc. typically outwards discharge a certain amount of waste gas in normal operation condition, hydro carbons containing higher concentration in these waste gas, if effectively do not recycled, on the one hand a large amount of wastes to resource are caused, on the other hand serious environmental pollution is caused, while also there is certain potential safety hazard.
The recovery and treatment method of hydrocarbon-contained waste gas is more common absorption process, absorption method, condensation method, embrane method Investigation of Petroleum Vapor Recovery Technology etc., and such as Huang Weiqiu etc. exists《Middle outer energy》5th phase in 2006 " application study of Investigation of Petroleum Vapor Recovery Technology ", a text was described, it is considered that normal pressure and temperature absorption process recovery technology is preferably as presently preferred scheme.Can also be the combination of some techniques, in oil-gas recovery method as disclosed in CN03135766.0, recycle after substantial amounts of oil gas initially with the supercharging method of reducing phlegm and internal heat, then be reclaimed using pressure absorption process, pressure adsorption method, emulsification absorption method further.
The mercaptans content of light hydrocarbons material is one of important quality index, such as liquid hydrocarbon, gasoline, kerosene etc..The light hydrocarbons of many technique productions all contain a certain amount of mercaptan, it is therefore desirable to which suitable method removing is processed.Hydrogenation technique can be used for light hydrocarbons removal of mercaptans, but hydrogenation subtraction unit is complicated, and investment is big, and operating cost is high, some indexs of light hydrocarbons（Octane number as gasoline）Impacted, gasoline desulfating method etc. as disclosed in CN1478866A.Oxidation sweetening is the important method of light hydrocarbons removal of mercaptans, i.e., under certain condition, be disulphide etc. with air by the mercaptan oxidation in light hydrocarbons, and separates further and remove, such as US4, air sweetening method etc. disclosed in 090,954.Air sweetening process is general at a certain temperature, carries out air sweetening reaction with excessive air, as the boiling point of light hydrocarbons material is relatively low, therefore contains substantial amounts of hydro carbons in oxidized tail gas, and general volume fraction is up to 5%～65%.
Due to containing substantial amounts of hydro carbons in oxidation sweetening tail gas, the processing method for adopting at present include incinerator burn, be directly discharged into air, absorb after enter air, condensation and be catalyzed oxygen and the method such as combined.The deficiency of incineration treatment method is to cause ample resources to waste, and due to also there is potential safety hazard containing oxygen in tail gas.Air not only waste of resource is directly discharged into, also results in serious environmental pollution.Absorption process is the hydro carbons in a kind of employing solvent absorption waste gas, the method that tail gas enters air after absorption, and the method can reclaim most of hydro carbons, but increasingly strict due to environmental regulation, it is impossible to realize qualified discharge.Such as《Oil refining design》The demercaptaning for gasoline by catalyst cracking exhaust gas treating method of the 6th phase of volume 28 introduction of page 31～32, is absorbed using packed tower, and the method adopts ventional absorption technology, and its treatment effect need to be improved further.Condensation is combined with catalysis oxidation i.e. can reclaim most of volatile hydrocarbon, it is also possible to realize tail gas qualified discharge, but which is disadvantageous in that technological process is long, and operating cost is high, and economy is affected.
In hydrocarbon-contained waste gas absorption process recovery process, absorbent is the key factor for affecting assimilation effect and absorption technique economy.Select special absorptive agent when, absorbent relatively costly, while absorbent regeneration workshop section must also be arranged, equipment investment and running expense are all higher.Also there is the scheme of commodity in use diesel oil or commodity kerosene for absorbent in prior art, the rich absorbent for obtaining is due to containing the lighter hydro carbons of cut, typically cannot need to return to oil refining enterprise and re-work directly as commodity selling, same have the high deficiency of operating cost.Use gas-oil or rough coal oil as waste gas absorbent, the rich absorbent for obtaining by normal gas-oil or rough coal oil processing scheme, economically for be the absorbent being particularly suitable for.But hydrogen sulfide and light component is usually contained in gas-oil and rough coal oil, more serious to the exhaust gases after process, there is presently no suitable means and processed.
On the one hand the recycling technology of hydrocarbon-contained waste gas will consider cost recovery, on the other hand will consider the problem up to standard of emission, although existing method has certain technique effect in some aspects, overall target need to be improved further.The economy of hydrocarbon-contained waste gas recycling process is to realize the important indicator of commercial Application.
Content of the invention
For the deficiencies in the prior art, a kind of process of present invention offer is simple, the sulfide hydrogen hydrocarbon-contained waste gas processing method of economical rationality, is suitable for the absorption process handling process of sulfide hydrogen hydrocarbon-contained waste gas
The present invention provides a kind of processing method of sulfide hydrogen hydrocarbon-contained waste gas, and methods described includes following content：
（1）Gas-oil or rough coal oil enter rotary drill reactor carries out devolatilization pretreatment；
（2）Step（1）The material that middle rotary drill reactor liquid-phase outlet is discharged enters absorption equipment as absorbent, contacts with sulfide hydrogen hydrocarbon-contained waste gas and is reacted, and the rich lyosoption that absorption equipment is discharged enters hydrogenation plant and processed；
（3）Step（1）Material and step that middle rotary drill reactor gaseous phase outlet is discharged（2）Crystallizing tower is entered after the waste gas mixing that middle absorption equipment is discharged, contact under the conditions of 0～40 DEG C with ammonia and reacted, the waste gas qualified discharge that discharges after process.
In the processing method of sulfide hydrogen hydrocarbon-contained waste gas of the present invention, the sulfide hydrogen hydrocarbon-contained waste gas can be from the sulfide hydrogen hydrocarbon-contained waste gas in various devices, such as oil product storage tank discharge gas, sour water tank discharge gas, oxidation sweetening of oil product alcohol tail gas etc., typically require hydrocarbon in sulfide hydrogen hydrocarbon-contained waste gas volume content be more than 2%, preferably 5%～80%, the hydrocarbon-contained waste gas of low concentration are unsuitable for reclaiming using absorption process, in sulfide hydrogen hydrocarbon-contained waste gas, the volume content of hydrogen sulfide is more than 5%, preferably 7%～70%.
In the processing method of sulfide hydrogen hydrocarbon-contained waste gas of the present invention, step（2）Described in absorption equipment can adopt packed tower commonly used in the art, bubble tower, spray column etc..Generally -30～50 DEG C of the operation temperature of absorption equipment, preferably 0～25 DEG C, operating pressure is normal pressure to 1MPa, and gaseous phase volume air speed is 1～200h-1, preferably 5～100h-1, the liquid air volume ratio of absorption equipment entrance is 0.005～0.5, preferably 0.01～0.1.Above-mentioned parameter according to the property of the content of hydrocarbon in waste gas and absorbent, require that the material elementses such as the absorptivity for reaching determine.Absorbent and/or sulfide hydrogen hydrocarbon-contained waste gas can improve the absorption efficiency of hydro carbons to reduce temperature using the mode such as cool.
In the processing method of sulfide hydrogen hydrocarbon-contained waste gas of the present invention, step（3）Described in crystallizing tower include to be provided with the upper cover of gas vent, tower body and be provided with the low head of gas access and material outlet, tower body includes crystallized region, wherein, tower tray is provided with crystallized region, and tower tray includes the upwardly extending multiple upper crystallization components of the tray deck stretched out from the inwall of tower body and the upper surface from tray deck.
The upper crystallization component includes column body and flexible wire, and flexible wire is arranged in column body to form torsion wire brush gear.Column body can be stainless steel, tetrafluoro material or carbon steel outer lining tetrafluoro material etc., and flexible wire is not for reacting with ammonium hydro sulfide and water-fast material, such as carbon fiber, nylon, fluoroplastics, any one in stainless steel wire.A diameter of 1mm～12mm of flexible wire, when flexible wire is for metal material, the diameter of flexible wire is preferably 1mm～3mm, and when flexible wire is for non-metallic material, the diameter of flexible wire is preferably 2mm～5mm.
Wherein, one end of tray deck is connected with the inwall of tower body, the other end cross out and the inwall of the opposite side of external part and tower body between can be formed with gas passage gaps.
Preferably, be provided with crystallized region successively between the upper and lower every multilayer tower tray, multilayer tower tray is arranged on the both sides of the central axis of tower body and forms left and right interlaced arrangement so that the gas passage gaps that gas phase can successively upwardly through each tray deck are to form baffling.
It is highly preferred that tower tray also includes multiple lower crystallization components, multiple lower crystallization components are arranged in the lower surface of the tray deck at each interval.The lower crystallization element structure is identical with upper crystallization component.In two neighbouring tower trays, between the bottom of the lower crystallization component of the top of the upper crystallization component of the tower tray of lower section and the tower tray of top, there is height gap, height gap is preferably 20mm～150mm, more preferably 50mm～100mm.
Tower body may also include cooling section, is provided with and takes hot component in cooling section, take any one in hot component preferably shell and tube devaporizer, heat-exchangers of the plate type, electrical chillers, gas type lithium bromide chiller.Tower body may also comprise the feed jet mixing section below cooling section, arrange gaseous distributer in the feed jet mixing section, and gaseous distributer is preferably aeration head, board-like gaseous distributer or slotted disc type gaseous distributer etc..Upper cover can also be provided with water inlet, and water inlet can be connected with water inlet distribution pipe, can be provided with some nozzles in water inlet distribution pipe.Water inlet can be same mouth with gas vent, or water inlet is independently arranged with gas vent.
In the processing method of sulfide hydrogen hydrocarbon-contained waste gas of the present invention, step（3）In, with described step（1）Material and step that middle rotary drill reactor gaseous phase outlet is discharged（2）Hydrogen sulfide content meter in the waste gas that middle absorption equipment is discharged, hydrogen sulfide are 1 with the raw materials components mole ratio of ammonia:1～1:2, preferably 5:6～2:3, the hydrogen sulfide is 0～20 DEG C with the reaction temperature of ammonia.
In the processing method of sulfide hydrogen hydrocarbon-contained waste gas of the present invention, gas-oil or rough coal oil are oil refining enterprise's diesel hydrotreating unit or the raw material of kerosene hydrogenation device, it is typically from still-process, secondary processing process of heavy distillate of raw material etc., can not need to be hydrogenated with further just and can obtain qualified commodity directly as commodity selling.The rich absorbent for absorbing hydrocarbons in waste gas that absorption equipment is discharged, can be directly entered hydrogenation plant, not produce any impact to hydrogenation plant.
Rotary drill reactor of the present invention includes that cylinder, bed component, upper cover and low head are constituted, cylinder, upper cover and low head constitute enclosed construction, bed component is arranged on the inner space of above-mentioned enclosed construction, bed component axial centre is rotary shaft, rotary shaft upper end is fixed on upper cover in a rotatable manner, rotary shaft lower end is fixed on low head in a rotatable manner, and rotary shaft lower end is stretched out low head and coupled with driving means；Gaseous phase outlet is set on cylinder top or upper cover, liquid-phase outlet is set in cylinder bottom or low head；The integral structure that bed component is made up of upper cover plate, bed, lower cover and rotary shaft, upper cover plate and lower cover are separately fixed at the upper and lower of rotary shaft, bed is clamped between upper cover plate and lower cover, it is hollow tubular structure that rotary shaft is located at the part on the internal and bed top of bed, rotary shaft is located on the tube wall inside bed and opens up some through holes, i.e., the part rotary shaft is while be liquid distributor.
In rotary drill reactor of the present invention, rotary shaft upper end is stretched out upper cover and is connected in swivel joint mode with liquid phase entrance pipe, or liquid phase entrance pipe is stretched into revolving bed inner space and connected with rotary shaft top in swivel joint mode.
In rotary drill reactor of the present invention, gaseous phase materials intake need not be set, and gaseous phase materials are prevented without flow through the sealing structure of bed.
In rotary drill reactor of the present invention, the hermetic unit being related to can be using conventional mechanical seal structure.Driving means can be driven using Motor drive or other power-equipments.Bed can be using conventional filling-material structure, screen net structure, mesh structure etc..Aperture on liquid distributor can be uniformly arranged, and bore dia is generally 1～10mm.Bed is clamped between upper cover plate and lower cover, constitute bed center closed area.Generally 200～5000 revs/min, preferably 400～2000 revs/min of the rotating speed of bed component in revolving bed.
In the inventive method, for sulfide hydrogen hydrocarbon-contained waste gas, devolatilization pretreatment is carried out to gas-oil or rough coal oil by revolving bed, hydrogen sulfide that can be in gas-oil or rough coal oil, the volatilization impurity that grades effectively are deviate from, gas-oil or rough coal oil are used as absorbent, and improve assimilation effect, by arranging crystallizing tower, ammonium hydro sulfide is generated using ammonia with hydrogen sulfide reaction in waste gas, the hydrogen sulfide of hydrogen sulfide in waste gas and gas-oil or the abjection in rough coal oil can be removed, sulfide hydrogen hydrocarbon-contained waste gas can realize qualified discharge after treatment.
In the methods of the invention, be provided with crystallized region tower tray and multiple on crystallize component, the brush crystallization component of torsion wire is especially set, significantly increase crystal bond area, when last layer tower tray crystal falls, the tow space of the crystallization post is still present, and can make to fall crystal in soft fluffy state, sulphur hydrogenation ammonia mutually can still be passed through, and continue crystallization attachment in crossing process；But also the crystal surface that falls can be also served as crystallizing attachment surface use, significantly increase crystallization bond area.Crystallizing tower of the present invention, as the silk thread for crystallizing post is soft material, when gas phase flows through crystallization post, around which flowing have differences, crystallization attachment be heterogeneous state, gas phase flowing brush and center of gravity skew, cause to crystallize post swing, crystal is easy to peel off from crystallization post.
Description of the drawings
Fig. 1 sulfide hydrogen hydrocarbon-contained waste gas processing technological flow schematic diagram of the present invention；
Fig. 2 is crystallizing tower structural representation of the present invention, and the arrow of in figure represents the flow direction of gas phase, that is, forms baffling figure upwards；
Fig. 3～Fig. 4 is the structural representation of the tower tray of the embodiment not of the same race of the present invention；
Fig. 5 is the structural representation for crystallizing component in the present invention；
Fig. 6 revolving bed structural representation of the present invention；
The bed modular construction schematic diagram of Fig. 7 revolving bed of the present invention.
Specific embodiment
The technology of the present invention content and effect are further illustrated with reference to the accompanying drawings and examples.
As shown in Figure 1, in sulfide hydrogen hydrocarbon-contained waste gas processing method of the present invention, gas-oil or rough coal oil 22 are after the pretreatment of revolving bed 23, the fugitive constituents such as hydrogen sulfide, lighter hydrocarbons in gas-oil or rough coal oil are deviate from, removing hydrogen sulfide, the gas-oil of fugitive constituent or the rough coal oil 24 that discharges from revolving bed liquid-phase outlet enters pans 25, then 26 bottom of bubble absorption bed is entered through pump, absorption is contacted with sulfide hydrogen hydrocarbon-contained waste gas 21 in bubble absorption bed 26, absorb the hydrotreater that the rich absorbent 28 after hydro carbons is discharged into gas-oil；Waste gas 27 after gas-oil or rough coal oil absorb is exported after the gas phase 29 that discharges is mixed with ammonia 31 with revolving bed volatilization gas and enters crystallizing tower 30, using H2S occurs crystallization reaction to generate ammonium hydro sulfide with ammonia, remove the hydrogen sulfide in waste gas and gas-oil or the remaining hydrogen sulfide in rough coal oil, and then go the malodor components of remaining in removing exhaust gas, waste gas 32 after treatment can realize qualified discharge, ammonium hydro sulfide crystallization 33 is deposited in crystallizing tower, when tower to be crystallized needs handover operation, crystallizing tower is rinsed with water, crystallization is emitted entrance follow up device in the form of a solution and is processed further.
As shown in Figure 6 and Figure 7, revolving bed of the present invention is designed for rough coal oil or gas-oil removing hydrogen sulfide, including upper cover 3, bed component 4, cylinder 5 and low head 6 are constituted, wherein, bed component 4 includes liquid distributor 41, upper cover plate 42, bed 43, lower cover 44 and axle 45, cylinder 5, upper cover 3 and low head 6 constitute enclosed construction, bed component 4 is arranged on the inner space of above-mentioned enclosed construction, 4 axial centre of bed component is rotary shaft, rotary shaft upper end is fixed on upper cover 3 in a rotatable manner, rotary shaft lower end is fixed on low head 6 in a rotatable manner, rotary shaft lower end is stretched out low head and is coupled with driving device motor 9；Stoste entrance 1 is connected with liquid distributor top by swivel joint 12（Liquid distributor is structure as a whole with axle, and epimere is liquid distributor, and hypomere is axle）, volatilization gas outlet 11 is set on upper cover, devolatilization liquid outlet 10 is set on low head 6.
Revolving bed operation principle of the present invention is, driving device motor band moving axis, liquid distributor are rotated, revolving bed layer high-speed rotation is driven, and needs the stoste of devolatilization revolving bed, the aperture through opening up on liquid distributor tube wall to be entered from stoste entrance, it is sprayed at bed inwall, under the bed centrifugal action of high-speed rotation, the nowed forming of liquid phase becomes very thin liquid film and minimum drop, or even forms droplet state, and under bed effect, droplet surface can be obtained quick and be constantly updated.Under the hypergravity effect of revolving bed, on the one hand the resistance that volatile material is deviate from from liquid phase reduces, the specific surface area of another aspect liquid phase unit volume is greatly improved, and so as to promote volatile component to spread to liquid-vapor interface in the liquid phase, greatly enhances alternate transmittance process.In addition, the bed of high-speed rotation, produces larger centrifugal force, can form tiny structure, beneficial to the devolatilization processes of liquid phase.
As shown in Fig. 2～Fig. 5, the invention provides a kind of crystallizing tower, the crystallizing tower includes to be provided with the upper cover 1 of gas vent 4, tower body 2 and is provided with the low head 3 of gas access 8 and material outlet 7, tower body 2 includes crystallized region 11, tower tray 14 is provided with crystallized region 11, tower tray 14 includes the upwardly extending multiple upper crystallization components 16 of the substantial transverse tray deck 15 for stretching out and the upper surface from tray deck 15 from the inwall of tower body 2.Upper crystallization component 16 includes column body 17 and flexible wire 18, and flexible wire 18 is arranged in column body 17 to form torsion wire brush gear.This similar hairbrush shape can largely increase crystallization area, and crystal is easy to come off, and the crystal surface that falls also can be used as crystallization attachment surface.
In addition, when mounted, its one end is connected tray deck 15 with the inwall of tower body 2, the other end cross out and the inwall of the opposite side of external part and tower body 2 between be formed with gas passage gaps, gas phase can pass through the gas passage gaps, not necessarily form perforation etc. on tray deck 15.Gas passage gaps are conducive to guiding to form air channel, to brush upper crystallization component and lower crystallization component.For example, be provided with the crystallized region 11 shown in Fig. 2 successively between the upper and lower every multilayer tower tray 14 when, multilayer tower tray 14 is arranged on the central axis of tower body 2（For clarity, in figure is not indicated）Both sides and form left and right interlaced arrangement so that the gas passage gaps that gas phase can successively upwardly through each tray deck 15 are to form baffling.When gas phase flows to form baffling along the direction shown in figure arrow, the upper crystallization component 16 on each tray deck 15 can be brushed, be conducive to crystallization and the peeling of crystal.Certainly, cross out from the inwall of tower body 2 or tray deck 16 that lateral inclination stretches out is not limited to illustrate between the upper and lower every the arrangement staggered with left and right, be also not necessarily limited to polylith, the tray deck 15 of monolithic also only can be installed in tower body 2, perforation can be also formed on single tray plate 15 and is passed through for air-flow.A kind of mode for more having choosing is that as described in Figure 5, the tower tray of the crystallizing tower also includes lower crystallization component 19, and multiple lower crystallization components 19 are arranged in the lower surface of the tray deck 15 at each interval, and the lower crystallization component 19 is as upper crystallization 16 structure of component.
In addition, referring to Fig. 2, cooling section 10 being further comprises in tower body 2, being provided with and take hot component 13 in cooling section, take any one in hot component 13 preferably shell and tube devaporizer, heat-exchangers of the plate type, electrical chillers, gas type lithium bromide chiller.The gas that crystallizing tower is entered by gas access 8 can be cooled down by taking hot component 13, be cooled to and be close to crystallization reaction temperature, consequently facilitating crystallized region 11 up produces crystallization reaction immediately.Certainly, cooling for gas to be crystallized and its cooling device are may also be arranged on outside tower body 2 as needed.And, tower body 2 also includes the feed jet mixing section 9 positioned at 10 lower section of cooling section, arranges gaseous distributer 12 in the feed jet mixing section 9, and gaseous distributer 12 is preferably aeration head, board-like gaseous distributer or slotted disc type gaseous distributer etc..Gaseous distributer 12 can cause gas to be evenly distributed, and flow field is stable, and crystallization is uniform.Additionally, upper cover 1 is additionally provided with water inlet 5, water inlet 5 is connected with water inlet distribution pipe 6, and water inlet distribution pipe 6 is provided with some nozzles.By the water spray of nozzle, flushable, dissolving crystallized thing is flowed out from the material outlet 7 of tower body bottom with forming such as acid water etc..Wherein, as shown in Fig. 2 water inlet 5 independently can be arranged with gas vent 4, but due to water filling and handover operation of the reaction end gas for different periods is discharged, thus water inlet 5 is preferably same mouth with gas vent 4.
Embodiment 1
Certain sour water tank tank field tank deck discharge gas, temperature 45 C or so, total hydrocarbon concentration are 100000～1000000mg/m3, sulfide concentration is 2000～10000mg/m3.Absorbent adopts the rough coal oil from oil refining apparatus fractionating column, and temperature is 60 DEG C.Gas-oil enters the revolving bed as shown in Fig. 5 structure, and bed rotating speed is 600 revs/min.The liquid phase that revolving bed is discharged enters bubbling bed with waste gas after being cooled to 15 DEG C and carries out hydro carbons absorption, and the gas space velocity in bubbling bed is 60h-1The agent of bubbling bed inlet absorption is 0.1 with the volume ratio of waste gas, the rich absorbent that bubbling bed is discharged is used as the charging of kerosene hydrotreater, the gas phase that waste gas after gas-oil or rough coal oil absorb is discharged with revolving bed is cooled to 20 DEG C after mixing with ammonia, crystallizing tower is entered, obtains gaseous stream and ammonium hydro sulfide crystallization.The ammonium hydro sulfide crystallization deposition is in crystallizing tower.Waste gas after solvent absorption with crystallizing tower process, hydrogen sulfide content are less than 2mg/m3, it is possible to achieve qualified discharge.
Claims (20)
1. a kind of processing method of sulfide hydrogen hydrocarbon-contained waste gas, methods described include following content：
（1）Gas-oil or rough coal oil enter rotary drill reactor carries out devolatilization pretreatment；
（2）Step（1）The material that middle rotary drill reactor liquid-phase outlet is discharged enters absorption equipment as absorbent, contacts with sulfide hydrogen hydrocarbon-contained waste gas and is reacted, and the rich lyosoption that absorption equipment is discharged enters hydrogenation plant and processed；
（3）Step（1）Material and step that middle rotary drill reactor gaseous phase outlet is discharged（2）Crystallizing tower is entered after the waste gas mixing that middle absorption equipment is discharged, contact under the conditions of 0～40 DEG C with ammonia and reacted, the waste gas qualified discharge that discharges after process；
Wherein, step（3）Described in crystallizing tower include to be provided with the upper cover of gas vent, tower body and be provided with the low head of gas access and material outlet, tower body includes crystallized region, wherein, tower tray is provided with crystallized region, and tower tray includes the upwardly extending multiple upper crystallization components of the tray deck stretched out from the inwall of tower body and the upper surface from tray deck.
2. method according to claim 1, it is characterised in that：In the sulfide hydrogen hydrocarbon-contained waste gas, the volume content of hydrocarbon is more than 2%, preferably 5%～80%.
3. method according to claim 1, it is characterised in that：In the sulfide hydrogen hydrocarbon-contained waste gas, the volume content of sulphur is more than 5%, preferably 7%～70%.
4. method according to claim 1, it is characterised in that：Step（2）Described in absorption equipment be packed tower, bubble tower or spray column.
5. method according to claim 1, it is characterised in that：Step（2）The operation temperature of middle absorption equipment is -30～50 DEG C, and operating pressure is normal pressure to 1MPa, and gaseous phase volume air speed is 1～200h-1, the liquid air volume ratio of absorption equipment entrance is 0.005～0.5.
6. method according to claim 1 or 5, it is characterised in that：Step（2）The operation temperature of middle absorption equipment is 0～25 DEG C, and operating pressure is normal pressure to 1MPa, and gaseous phase volume air speed is 5～100 h-1, the liquid air volume ratio of absorption equipment entrance is 0.01～0.1.
7. method according to claim 1, it is characterised in that：The upper crystallization component includes column body and flexible wire, and flexible wire is arranged in column body to form torsion wire brush gear.
8. method according to claim 7, it is characterised in that：The column body is stainless steel, tetrafluoro material or carbon steel outer lining tetrafluoro material, and the flexible wire is not for reacting with ammonium hydro sulfide and water-fast material, preferably carbon fiber, nylon, fluoroplastics, any one in stainless steel wire.
9. method according to claim 7, it is characterised in that：A diameter of 1mm～12mm of the flexible wire, when the flexible wire is metal material, the diameter of the flexible wire is preferably 1mm～3mm, and when the flexible wire is non-metallic material, the diameter of the flexible wire is preferably 2mm～5mm.
10. the method according to any claim in claim 1-9, it is characterised in that：One end of the tray deck is connected with the inwall of the tower body, the other end cross out and the inwall of the opposite side of external part and the tower body between be formed with gas passage gaps.
11. methods according to claim 10, it is characterised in that：Be provided with the crystallized region successively between the upper and lower every multilayer described in tower tray, tower tray described in multilayer is arranged on the both sides of the central axis of the tower body and forms left and right interlaced arrangement so that the gas passage gaps that gas phase can successively upwardly through tray deck each described are to form baffling.
12. methods according to claim 11, it is characterised in that：The tower tray also includes multiple lower crystallization components, and multiple lower crystallization components are arranged in the lower surface of the tray deck at each interval.
13. methods according to claim 11, it is characterised in that：The lower crystallization element structure is identical with upper crystallization element structure.
14. methods according to claim 1, it is characterised in that：The tower body also includes cooling section, is provided with and takes hot component in the cooling section, any one for taking hot component and being preferably in shell and tube devaporizer, heat-exchangers of the plate type, electrical chillers, gas type lithium bromide chiller.
15. methods according to claim 1, it is characterised in that：The tower body also includes the feed jet mixing section below the cooling section, arranges gaseous distributer in the feed jet mixing section, and the gaseous distributer is preferably aeration head, board-like gaseous distributer or slotted disc type gaseous distributer.
16. methods according to claim 1, it is characterised in that：The upper cover is additionally provided with water inlet, and the water inlet is connected with water inlet distribution pipe, and the water inlet distribution pipe is provided with some nozzles.
17. methods according to claim 16, it is characterised in that：The water inlet is same mouth with the gas vent, or the water inlet is independently arranged with the gas vent.
18. methods according to claim 1, it is characterised in that：Step（1）Described in revolving bed, including cylinder, bed component, upper cover and low head, cylinder, upper cover and low head constitute enclosed construction, bed component is arranged on the inner space of above-mentioned enclosed construction, bed component axial centre is rotary shaft, rotary shaft upper end is fixed on upper cover in a rotatable manner, and rotary shaft lower end is fixed on low head in a rotatable manner, and rotary shaft lower end is stretched out low head and coupled with driving means；Gaseous phase outlet is set on cylinder top or upper cover, liquid-phase outlet is set in cylinder bottom or low head；It is characterized in that：The integral structure that bed component is made up of upper cover plate, bed, lower cover and rotary shaft, upper cover plate and lower cover are separately fixed at the upper and lower of rotary shaft, bed is clamped between upper cover plate and lower cover, it is hollow tubular structure that rotary shaft is located at the part on the internal and bed top of bed, rotary shaft is located on the tube wall inside bed and opens up some through holes, i.e., the part rotary shaft is while be liquid distributor.
19. methods according to claim 1, it is characterised in that：The rotary shaft upper end of revolving bed is stretched out upper cover and is connected in swivel joint mode with liquid phase entrance pipe, or liquid phase entrance pipe is stretched into revolving bed inner space and connected with rotary shaft top in swivel joint mode.
20. methods according to claim 1, it is characterised in that：In revolving bed, the rotating speed of bed component is 200～5000 revs/min, preferably 400～2000 revs/min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510769162.6A CN106474896B (en) | 2015-11-12 | 2015-11-12 | The processing method of sulfide hydrogen hydrocarbon-contained waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510769162.6A CN106474896B (en) | 2015-11-12 | 2015-11-12 | The processing method of sulfide hydrogen hydrocarbon-contained waste gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106474896A true CN106474896A (en) | 2017-03-08 |
| CN106474896B CN106474896B (en) | 2019-09-10 |
Family
ID=58238299
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510769162.6A Active CN106474896B (en) | 2015-11-12 | 2015-11-12 | The processing method of sulfide hydrogen hydrocarbon-contained waste gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106474896B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1393405A (en) * | 2001-07-02 | 2003-01-29 | 中国石油化工股份有限公司 | Process for purifying and recovering ammonia gas |
| US20030101869A1 (en) * | 2001-12-05 | 2003-06-05 | Yvan Baudry | Method and installation for treating effluent gas containing hydrocarbons |
| CN202625938U (en) * | 2012-07-05 | 2012-12-26 | 西安石油大学 | Scale-induced crystallizing reactor |
| CN104587816A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司大连石油化工研究院 | Treating method for waste gas containing sulfur and hydrocarbons |
-
2015
- 2015-11-12 CN CN201510769162.6A patent/CN106474896B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1393405A (en) * | 2001-07-02 | 2003-01-29 | 中国石油化工股份有限公司 | Process for purifying and recovering ammonia gas |
| US20030101869A1 (en) * | 2001-12-05 | 2003-06-05 | Yvan Baudry | Method and installation for treating effluent gas containing hydrocarbons |
| CN202625938U (en) * | 2012-07-05 | 2012-12-26 | 西安石油大学 | Scale-induced crystallizing reactor |
| CN104587816A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司大连石油化工研究院 | Treating method for waste gas containing sulfur and hydrocarbons |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106474896B (en) | 2019-09-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102311790B (en) | Liquid phase circular hydrogenation treatment method capable of improving mixed amount of hydrogen | |
| CN102309913B (en) | Treatment method for stinky waste gas containing sulfides and hydrocarbons | |
| CN101637687B (en) | Method for processing light hydrocarbons oxidation sweetening tail gas | |
| CN104587814B (en) | Treating method for waste gas containing sulfur and hydrocarbons | |
| CN102309914A (en) | Treatment method for stinky waste gas discharged by storage tank | |
| KR102001695B1 (en) | Integrated Hydrotreating and Isomerization Process with Aromatic Separation | |
| EA016377B1 (en) | Configurations and methods for fuel gas treatment with total sulfur removal and olefin saturation | |
| CN104587816B (en) | Treating method for waste gas containing sulfur and hydrocarbons | |
| CN104587815B (en) | Treating method for waste gas containing sulfur and hydrocarbons | |
| CN103965953B (en) | Distillate oil two-phase hydrogenation reactor and hydrogenation process | |
| CN101455933A (en) | Tower-top eddy flow purification method and device of recycle hydrogen desulfurizing tower | |
| CN103785343B (en) | The absorption process of revolving bed and hydrocarbon-contained waste gas | |
| CN215995660U (en) | Pyrolysis oil-gas cooling separation and dust removal integrated equipment | |
| CN102908882B (en) | Treatment method for emissions of sour water storage tank | |
| CN102049171B (en) | Method for reclaiming and treating hydrocarbon-containing waste gas | |
| CN103789000B (en) | The recovery method of revolving bed and hydrocarbon-contained waste gas | |
| CN106479558A (en) | A kind of processing method of sulfide hydrogen hydrocarbon-contained waste gas | |
| CN106474897A (en) | A kind of method for processing sulfide hydrogen hydrocarbon-contained waste gas | |
| CN106474896A (en) | The processing method of sulfide hydrogen hydrocarbon-contained waste gas | |
| CN101239271B (en) | Cleaning treatment method of acid sewage storage tank discharging gas | |
| CN103789001B (en) | The recovery method of a kind of revolving bed and hydrocarbon-contained waste gas | |
| CN107243242A (en) | Refinery's amine liquid desulphurization system and its sulfur method | |
| CN209974689U (en) | Oxidized asphalt tail gas recovery and purification device | |
| US2179008A (en) | Process for refining oil | |
| CN205760493U (en) | Waste gas containing benzene cleaning system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |