CN106978208B - A kind of method of lighter hydrocarbons desulfurization - Google Patents
A kind of method of lighter hydrocarbons desulfurization Download PDFInfo
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- CN106978208B CN106978208B CN201610028954.2A CN201610028954A CN106978208B CN 106978208 B CN106978208 B CN 106978208B CN 201610028954 A CN201610028954 A CN 201610028954A CN 106978208 B CN106978208 B CN 106978208B
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- lye
- lighter hydrocarbons
- phase mixtures
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G19/00—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment
- C10G19/02—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment with aqueous alkaline solutions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/26—Fuel gas
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to refining arts, disclose a kind of method of lighter hydrocarbons desulfurization, this method is implemented in the system for including caustic wash unit, this method comprises: lye is introduced in reactor shell side from the dispersed phase entrance of two-phase mixtures reactor, and lye enters mixing runner through distribution hole and contacted with the lighter hydrocarbons that reactor inlet and mixing flow channel entry point are introduced in mixing runner are passed sequentially through；Lye in reactor shell side flow direction in the flow direction in mixing runner on the contrary, lye contact with lighter hydrocarbons after the mixture that is formed successively process mixes runner exit and reactor outlet is led to except two-phase mixtures reactor.In the method for the invention, by using two-phase mixtures reactor, sulfur-bearing lighter hydrocarbons and lye is enabled to flow and be vigorously mixed mixing runner high speed, resistance to mass tranfer is low, so that contained acidity sulphur-containing substance is sufficiently reacted with lye in sulfur-bearing lighter hydrocarbons, realize that the deep desulfuration of sulfur-bearing lighter hydrocarbons, acid sulphur-containing substance removal efficiency are greater than 90%.
Description
Technical field
The present invention relates to refining arts, and in particular, to a kind of method of lighter hydrocarbons desulfurization.
Background technique
Contain in the lighter hydrocarbons such as thick liquefied gas (predominantly C4 hydro carbons) and light petrol (predominantly C5 hydro carbons) that oil plant generates
A large amount of acidity sulphur-containing substances (predominantly hydrogen sulfide and mercaptan), the industrial general method by alkali cleaning remove acid sulfur-bearing object
Matter.
Removal of mercaptans is step important in liquefied gas subtractive process.The common alkali washing method of industrial liquid gas sweetening
The lye containing excessive NaOH is usually used to contact with liquefied gas, so that mercaptan is reacted with NaOH generates sodium mercaptides, mercaptan
Sodium is dissolved in lye to remove the mercaptan in liquefied gas.
Lye containing sodium mercaptides needs to regenerate, and removes mercaptan sodium.The method of alkali liquid regeneration is usually lye and gas
Body (can be air or oxygen rich gas) mixes, dissolved with catalyst (such as sulfonated phthalocyanine cobalt) in lye, in the effect of catalyst
Under, the sodium mercaptides in lye can be oxidized by oxygen generation disulphide.Disulphide is not soluble in water, as long as therefore generation
Disulphide is separated from lye, can realize the regeneration of lye.
But in the actual process, the density of disulphide and lye is very close, and disulphide and lye have cream
The phenomenon that change, therefore a large amount of disulphide are difficult to be kept completely separate out from lye, but be reproduced lye entrainment and return to
In liquefied gas caustic wash desulfuration equipment.
Moreover, because disulphide is soluble in liquefied gas, therefore the disulphide carried secretly in lye can be dissolved in liquefaction
Gas causes desulfuration of liquefied gas ineffective.
Further, since partial oxidation can be dissolved in lye during alkali liquid regeneration.This is partly dissolved oxygen can be in regenerating alkali
Liquid generates disulphide, and be stranded in liquefied gas again and in liquefied gas contact process under the action of catalyst, so as to cause
Liquefied gas caustic wash desulfuration partial failure.
Therefore, during liquid gas sweetening, the removing of disulphide is extremely important.
Summary of the invention
The purpose of the present invention is overcoming the deficiencies of existing technologies, a kind of satisfaction containing under low mass transfer Impetus Condition is provided
The method of sulphur lighter hydrocarbons deep desulfuration.
To achieve the goals above, the present invention provides a kind of method of lighter hydrocarbons desulfurization, and this method is including caustic wash unit
Implement in system, the caustic wash unit includes two-phase mixtures reactor, and the two-phase mixtures reactor includes reactor inlet, anti-
Answer device outlet and reactor tank body, include first partition and second partition in the inner cavity of the reactor tank body, described first every
Reactor shell side, the first partition and described the are formed between plate and the second partition and the inner wall of the reactor tank body
Two partitions are connected by least one mixing runner, are provided on the wall of the mixing runner so that the reactor shell side and institute
State the distribution hole of mixing runner connection；This method comprises: lye is introduced from the dispersed phase entrance of the two-phase mixtures reactor
To in the reactor shell side, and the lye through the distribution hole enter the mixing runner with pass sequentially through described react
The lighter hydrocarbons that device entrance and the mixing flow channel entry point are introduced in the mixing runner are contacted；The lye is in the reaction
Flow direction in device shell side in the flow direction in the mixing runner on the contrary, the lye contacted with the lighter hydrocarbons after shape
At mixture successively by the mixing runner exit and the reactor outlet lead to the two-phase mixtures reactor it
Outside.
In the method for the invention, by using two-phase mixtures reactor, sulfur-bearing lighter hydrocarbons is enabled to mix with lye
Runner high speed is flowed and is vigorously mixed, and resistance to mass tranfer is low, so that contained acidity sulphur-containing substance (such as mercaptan) in sulfur-bearing lighter hydrocarbons
It is sufficiently reacted with lye, realizes that the deep desulfuration of sulfur-bearing lighter hydrocarbons, acid sulphur-containing substance removal efficiency are greater than 90%, it is preferable that lighter hydrocarbons
In acid sulphur-containing substance concentration can be down to 10ppm or less or lower.
Method of the invention is particularly suitable for sulphur-containing substance concentration acid in lighter hydrocarbons (such as liquefied gas and/or light petrol) compared with
Low (such as tens ppm), thus deep desulfuration is carried out in the lower situation of mass transfer force.At this point, in method of the invention
Two-phase mixtures reactor in two-phase mixed at high speed contact, resistance to mass tranfer is very low, mercaptan etc. acidity sulphur-containing substance can fill
Ground is divided to separate with after lye haptoreaction with lighter hydrocarbons.
Two-phase mixtures reactor of the invention, before two-phase mixtures contact, flow direction of the two-phase in respective runner is excellent
It is selected as countercurrent flow, reflux type can make the pressure difference of each distribution hole two sides be uniformly distributed, and a phase can be equably from each
The outflow of a distribution hole and with another mixing that is in contact, thus the effect that realization multistage cross flow is mixed in two-phase mixtures reactor
Fruit strengthens mass-transfer performance, and avoiding the part distribution hole as caused by Pressure difference distribution is uneven can not push fluid out, to reduce
The phenomenon that mass-transfer efficiency.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the cross section knot of the first partition of the two-phase mixtures reactor of a preferred embodiment of the invention
Structure schematic diagram.
Fig. 2 is the vertical section structure schematic diagram of the two-phase mixtures reactor of a preferred embodiment of the invention.
Fig. 3 is the flow chart of the method for the lighter hydrocarbons desulfurization of a preferred embodiment of the invention.
Description of symbols
1, flow channel entry point 2, reactor inlet are mixed
3, reactor outlet 4, reactor tank body
5, first partition 6, second partition
7, reactor shell side 8, mixing runner
9, distribution hole 10, distributing chamber
11, runner exit 12, collecting chamber are mixed
13, sedimentation unit 14, oxidation regeneration unit
15, anti-extraction unit 16, fresh lye
17, lighter hydrocarbons 18, regeneration lye
19, sulfur-bearing lye 20, oxygen-containing gas
21, light-end products 22, sulfur-bearing light-end products
23, desulfurization lighter hydrocarbons 24, caustic wash unit
25, dispersed phase entrance
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of method of lighter hydrocarbons desulfurization, this method is implemented in the system for including caustic wash unit, described
Caustic wash unit includes two-phase mixtures reactor, and the two-phase mixtures reactor includes reactor inlet, reactor outlet and reaction
Device tank body, includes first partition and second partition in the inner cavity of the reactor tank body, the first partition and described second every
Reactor shell side, the first partition and the second partition are formed between plate and the inner wall of the reactor tank body by least
One mixing runner connects, and is provided on the wall of the mixing runner so that the reactor shell side is connected to the mixing runner
Distribution hole；This method comprises: lye is introduced to the reactor enclosure from the dispersed phase entrance of the two-phase mixtures reactor
Cheng Zhong, and the lye through the distribution hole enter the mixing runner and pass sequentially through the reactor inlet and it is described mix
The lighter hydrocarbons that flow channel entry point is introduced in the mixing runner are closed to be contacted；Flowing of the lye in the reactor shell side
Direction in the flow direction in the mixing runner on the contrary, the lye contacted with the lighter hydrocarbons after the mixture that is formed successively
It is led to except the two-phase mixtures reactor by the mixing runner exit and the reactor outlet.
In the two-phase mixtures reactor of the invention, the first partition and the second partition and the reactor
Reactor shell side is formed between the inner wall of tank body, so that reactor shell side mixes between runner independently of each other with described.It is preferred that setting
Set multiple mixing runners, the settings of multiple mixing runners so that each mixing runner formed keeps mutually indepedent, in lye and
In the contact and reaction process of lighter hydrocarbons, the fluid between adjacent mixing runner will not be interfered with each other, and each mixing runner
It is respectively formed relatively independent microreactor, is conducive to the mixing of strengthening fluid, improves mass transfer and reactivity worth.
The outer shape of the two-phase mixtures reactor is not required particularly, can for cylindrical shape, rectangular-shape,
Elliptic Cylinder shape, cube-shaped, triangular prism shape etc., under preferable case, the two-phase mixtures reactor is cylindrical shape.
Preferably, the two-phase mixtures reactor further comprises collecting chamber and distributing chamber, and the lighter hydrocarbons successively pass through institute
Reactor inlet, the distributing chamber and the mixing flow channel entry point are stated into the mixing runner, the lye and it is described gently
The mixture formed after hydrocarbon contact is successively led to by the mixing runner exit, the collecting chamber and the reactor outlet
Except the two-phase mixtures reactor.Distributed component can be contained in the distributing chamber of the invention.
Under preferable case, in order to guarantee that fluid can preferably be reacted in two-phase mixtures uniformly across each mixing runner
Distributing chamber containing distributed component is set in device, to guarantee that fluid can be uniformly across each mixing runner.In two-phase mixtures
In reactor, after fluid enters distributing chamber, distributed component is able to suppress the excessive problem of the fluid flow for mixing runner placed in the middle,
The fluid flow for increasing distributed component two sides, the fluid that may be implemented in each mixing runner in this way can be uniformly distributed.Distribution
Multi-disc distributed component can also can be set, the shape of distributed component can with feature structures such as sieve pore, item seams in the form of component
To be the shapes such as circle, rectangle, diamond shape.
The fluid of the invention can be appointing in sulfur-bearing lighter hydrocarbons, lye, desulfurization lye, sulfur-bearing lye, desulfurization lighter hydrocarbons
It anticipates one or more, those skilled in the art according to the present invention can describe unambiguously to determine fluid difference herein
Which kind of substance is represented, those skilled in the art should not be construed as limiting the invention.
Preferably, in the two-phase mixtures reactor, the mixing runner is cylindrical shape, Elliptic Cylinder shape, pros
At least one of body shape and rectangular-shape；It is highly preferred that the mixing runner is cylindrical shape or rectangular-shape.
Preferably, in the two-phase mixtures reactor, the first partition and the second partition pass through at least two
Runner connection is mixed, the number of the distribution hole on the wall of each mixing runner is identical or different, and each mixed flow
The number of distribution hole on the wall in road is each independently 1-100.
Preferably, in the two-phase mixtures reactor, the aperture of each distribution hole is 0.1-2mm.
Preferably, according to the flow direction of the lye in the reactor shell side, the aperture of the distribution hole is sequentially increased.
Preferably, according to the flow direction of the lye in the reactor shell side, the aperture ratio downstream of the distribution hole of upstream
The small 0.01-1mm in the aperture of adjacent distribution hole.
Preferably, in the two-phase mixtures reactor, on the wall of each mixing runner, two neighboring distribution hole
Central point distance be 0.5-40mm；More preferably 1-30mm.
Preferably, in the two-phase mixtures reactor, the depth of the distribution hole is 0.1-3mm；More preferably 0.3-
2.5mm。
Preferably, in the two-phase mixtures reactor, the axial direction (center of the as described distribution hole of the distribution hole
Line) it with the angle of the flow direction of the fluid mixed in runner is any angle, the preferably described angle is 45-90 degree, more preferably
It is 90 degree.
Preferably, in the two-phase mixtures reactor, the distribution hole is flowed along the fluid in the mixing runner
Direction is point-blank set gradually.But the setting of the distribution hole is not limited thereto, when the number of the distribution hole
When being more than one, the distribution hole can not also be set along the straight line parallel with the fluid flow direction in mixing runner
It sets.
The distribution hole can be set in entirely mixing runner, it is preferable that the distribution hole setting enters in proximal response device
Mouth end, so that being conducive to the lye from the reactor shell side and the lighter hydrocarbons from the reactor inlet can mix described
Collaborate the nearly entrance end in contact in road and react, and the mixture fluid obtained after mixing can make in longer mixing runner
Contact and the reaction for obtaining mixture fluid are more abundant.
Preferably, according to the flow direction of the lye in the reactor shell side, the dispersed phase entrance is arranged described
The upstream of reactor shell side, also, the upstream of each distribution hole is arranged in the dispersed phase entrance.
Preferably, at least one fiber filament can be set in the mixing runner.The filametntary material can be gold
The inorganic material such as category, glass are also possible to organic material, or the composite material of the above different materials.Filametntary selection root
Depending on property according to the fluid in reactor shell side, if the fluid in reactor shell side is aqueous solution, fiber filament
The hydrophilic materials such as stainless steel or glass can be selected；If the fluid in reactor shell side is oil product, fiber filament is optional
With lipophilic organic material.It is preferred that the filametntary diameter is 1 μm to 5mm, more preferably 2-50 μm.It mixes in runner and adds
Enter fiber filament, the compatibility of drop can be formed by the lye in reactor shell side by it, in filament surface
Very thin liquid film is formed, interphase mass transfer area is increased, shortens mass transfer distance, improves mixing efficiency.
To the filametntary diameter and length, there is no particular limitation, and those skilled in the art can be according in the art
Conventional parameter selected.The filametntary length can be arranged, the fiber according to the length of the mixing runner
Silk can mix runner through entire, and preferably according to the fluid flow direction in mixing runner, the filametntary length is
From the central point of the distribution hole of most downstream to the distance of mixing runner exit.
Under preferable case, the fiber filament is linear or helical form.
Lye can enter reactor shell side by dispersed phase entrance, and pass through connection reactor shell side and the mixing
The distribution hole of runner is entered in mixing runner and is connect with the lighter hydrocarbons from the reactor inlet mixed in runner
Touching and/or reaction, and the reactor outlet is led to from the mixing runner exit.
Preferably, the connection type between the first partition and the second partition and the inner wall of the reactor tank body
Including detachable connection method and non-detachable connection method.
Preferably, the connection type between the first partition and the second partition and the inner wall of the reactor tank body
Selected from flanged joint, welded connecting, threaded connection, expanded joint, seam connection is stung, is glued and at least one of connected with blind rivet.
Preferably, the mixing runner and the first partition and the connection type of the second partition also include detachable
Connection type and non-detachable connection method.
The number of the preferably described mixing runner of the present invention is at least two, more preferably more than two multiple mixed flows
Road, multiple mixing runners, which advantageously allow the two-phase mixtures reactor, has biggish processing capacity.
Preferably, the cross-sectional area in each mixing runner perpendicular to fluid flow direction is 0.5-20mm2, preferably
For 1-10mm2。
According to a kind of preferred embodiment, the cross of the first partition 5 of the two-phase mixtures reactor of the invention
Cross section structure schematic diagram is as shown in Figure 1, include mixing flow channel entry point 1 in the first partition.
According to another preferred embodiment, the vertical section structure of the two-phase mixtures reactor of the invention shows
It is intended to as shown in Fig. 2, specifically, which includes reactor inlet 2, reactor outlet 3 and reactor tank body
4, it include first partition 5 and second partition 6 in the inner cavity of the reactor tank body 4, the first partition 5 and the second partition
Reactor shell side 7, the first partition and the second partition are formed between 6 and the inner wall of the reactor tank body 4 by extremely
A few mixing runner 8 connects, and is provided on the wall of the mixing runner so that the reactor shell side mixes runner with described
The distribution hole 9 of connection；Distributing chamber 10 is set between the reactor inlet 2 and the mixing flow channel entry point 1, mixes runner exit
Collecting chamber 12 is set between 11 and the reactor outlet 3, and lye is introduced into reactor shell side 7 by dispersed phase entrance 25.?
In the preferred embodiment of the invention, since the reactor tank body is set as cylindrical.However, of the invention described two
Mixing reactor may be set to be the shapes such as triangular prism, quadrangular, and those skilled in the art should not be by above-mentioned preferred circle
Bar shape is interpreted as limitation of the present invention.
Preferably, this method further include: the mixture obtained from the reactor outlet is introduced into the caustic wash unit
Initial gross separation is carried out in precipitation apparatus, obtains the first sulfur-bearing lye and the first lighter hydrocarbons；Then first lighter hydrocarbons introducing is located at
The second separation is carried out in the sedimentation unit in the caustic wash unit downstream, obtains the second sulfur-bearing lye and desulfurization lighter hydrocarbons；And by institute
It states the first sulfur-bearing lye and the second sulfur-bearing lye is introduced into oxidation regeneration unit and reacts with oxygen-containing gas progress oxidation regeneration；And
The desulfurization lye obtained in the oxidation regeneration unit is introduced into anti-extraction unit and is separated, regeneration lye is obtained；And
The regeneration lye is recycled back in the caustic wash unit.
That is, the method for the lighter hydrocarbons desulfurization of the invention is successively including caustic wash unit, sedimentation unit, is aoxidizing again
Implement in the system of raw unit and anti-extraction unit, lighter hydrocarbons pass through caustic wash unit and the contained acid sulfur-bearing object of sedimentation unit removal
Matter, and lye realizes regeneration by oxidation regeneration unit and anti-extraction unit.
In the liquid liquid two phase flow that lye and lighter hydrocarbons are formed, a phase is as continuous phase, and another phase is as dispersed phase.
NaOH can be contained in the lye, the preferably concentration of NaOH is 10-20 weight %.In the caustic wash unit,
Acid sulphur-containing substance in lighter hydrocarbons is reacted with NaOH generates sulfur-bearing sodium salt, and sulfur-bearing sodium salt is dissolved in lye.By desulfurization
The mixture that the lighter hydrocarbons and lye of reaction are formed, which enters, carries out initial gross separation in the precipitation apparatus of caustic wash unit, obtain the first sulfur-bearing
Lye and the first lighter hydrocarbons；Then first lighter hydrocarbons are introduced into and carry out second in the sedimentation unit in the caustic wash unit downstream
It separates (the described second isolated first purpose is that the lye by the sulfur-bearing carried secretly in first lighter hydrocarbons is sufficiently separated),
Obtain the second sulfur-bearing lye and desulfurization lighter hydrocarbons；The desulfurization lighter hydrocarbons, which can enter the processes such as subsequent washing purification, to carry out continuing to locate
Reason.
The first sulfur-bearing lye and the second sulfur-bearing lye are introduced into oxidation regeneration unit (usually can be with oxygen-containing gas
For air, oxygen rich gas or oxygen) carry out oxidation regeneration reaction.The reactor of oxidation regeneration unit typically bubbling bed
Reactor and/or filler bubbling bed reactor.In the reactor of oxidation regeneration unit, the first sulfur-bearing lye and described
Sulfur-bearing sodium salt and oxygen-containing gas in two sulfur-bearing lye catalyst (the ARI 100EXL catalyst containing sulfonated phthalocyanine cobalt or its
It has catalytic action substance) under the action of reacted, will be in the first sulfur-bearing lye and the second sulfur-bearing lye
Sulfur-bearing sodium salt be converted into disulphide not soluble in water, obtain desulfurization lye.
The disulphide does not dissolve in lye, therefore separates disulphide by the precipitation apparatus in oxidation regeneration unit
With desulfurization lye.But since the density of lye and disulphide is very close, the desulfurization lye that is discharged by oxidation regeneration unit
In still contain a large amount of disulphide, need to introduce anti-extraction unit and continue to separate.
It preferably, include at least one described two-phase mixtures reactor in the anti-extraction unit.
For the two-phase mixtures reactor in the caustic wash unit, as continuous phase, lye is used as to be divided the preferably described lighter hydrocarbons
Dephasing；And for the two-phase mixtures reactor in the anti-extraction unit, the preferably described lye is made as continuous phase, petroleum benzin
For dispersed phase.In the anti-extraction unit of the invention, the petroleum benzin as dispersed phase can be conventional use in the art
Various gasoline.
In caustic wash unit and anti-extraction unit, in the two-phase mixtures reactor, preferably continuous phase is from the reaction
Device entrance enter the mixing runner in, and the dispersed phase from the dispersed phase entrance successively through the reactor shell side and institute
Distribution hole is stated to enter in the mixing runner.
In the anti-extraction unit, the desulfurization lye and disulphide are soluble in light-end products therein such as gasoline
It is contacted Deng in the two-phase mixtures reactor, realizes the separation of desulfurization lye with the disulphide wherein carried secretly, regenerated
Lye.Precipitation apparatus through anti-extraction unit, regeneration lye is separated with the light-end products containing disulphide, by the regeneration lye
It is recycled back to the desulfurization that the caustic wash unit carries out lighter hydrocarbons.It is anti-using two-phase mixtures of the present invention in the anti-extraction unit
Answer the operating method of device similar to the operating method of caustic wash unit, details are not described herein by the present invention.
Preferably, in the caustic wash unit, apparent velocity of the lye in the dispersed phase inlet is 0.2-5m/
s；The lighter hydrocarbons are 0.5-20m/s in the apparent velocity of the mixing flow passage entry.
Preferably, in the caustic wash unit, the contact conditions of the lye and the lighter hydrocarbons include: that temperature is 25-80
DEG C, reaction pressure 0.2-2MPa.
It is preferred that apparent velocity of the dispersed phase in the dispersed phase inlet is 0.2-5m/s, more preferably 0.3-3m/
s.It is further preferred that the continuous phase is 4-10m/s in the apparent velocity of the mixing flow passage entry.
It is preferred that it is 25-80 DEG C that the reaction condition of the anti-extraction unit, which includes: reaction temperature, reaction pressure 0.2-
2MPa。
In the present invention, swiftly flowing liquid liquid two-phase is vigorously mixed in two-phase mixtures reactor, the liquid that dispersed phase is formed
Drop mixes acutely with continuous, and resistance to mass tranfer is low, enables to the mass transport process between two-phase sufficiently to carry out, desulfuration efficiency can
Reach 90% or more, that is to say, that contained acidity sulphur-containing substance (such as mercaptan) and alkali in lighter hydrocarbons can be made in caustic wash unit
Liquid sufficiently reacts, and realizes that the deep desulfuration of lighter hydrocarbons, acid sulphur-containing substance removal efficiency are greater than 90 weight %, acid sulfur-bearing object in lighter hydrocarbons
The mass concentration of matter can be down to 10ppm or less；And being sufficiently mixed for lye and light-end products may be implemented in anti-extraction unit, it will
The disulphide of entrained with is extracted in oily phase (light-end products) in lye after desulfurization, and the extraction yield of disulphide is greater than 90 weights
Measure %.
It is preferred that the pressure drop in two-phase mixtures reactor is 10-800kPa；More preferably 100-600kPa.Dispersed phase is through dividing
Drop is formed after cloth hole to be mixed with continuous phase.Since the diameter of distribution hole is smaller, the size of drop is also smaller, can be with
Obtain biggish interphase mass transfer area.
Two-phase mixtures reactor provided by the invention can be to two since the movement velocity of dispersed phase and continuous phase is very high
The runner for mixing reactor is adequately washed away, and the problem of runner blocks during long-term operation is avoided.It considers
This higher feature of the interfacial tension of liquid liquid system, method of the invention realize that lighter hydrocarbons depth is de- by being vigorously mixed for two-phase
The purpose of sulphur in liquid liquid two-phase contact process and does not use any substance (such as surface-active with reduction system tension
Agent, alcohols etc.) promote two-phase mixtures to contact, therefore avoid the emulsion of system, split-phase is imitated after two-phase mixtures contact
Fruit is good, and not additional waste material generates.
Under preferable case, the petroleum hydrocarbon-fraction that the lighter hydrocarbons are the C4-C5 containing the acid sulphur-containing substance wherein acid
Property sulphur-containing substance be mercaptan, the sulfur content in terms of element sulphur in the lighter hydrocarbons is 50-2000ppm.It is preferred that the lighter hydrocarbons be containing
Sulphur liquefied gas and/or sulfur-bearing light petrol.
By anti-extraction unit be discharged regeneration lye in sulfur content it is lower, can hardly using other extraction steps into
One step reduces sulfur content, therefore returning to sulphur contained in the regeneration lye of caustic wash unit substantially will not be by lighter hydrocarbons in alkaline cleaning procedure
It extracts and the desulfuration efficiency in lighter hydrocarbons is impacted.
It, can be anti-by two-phase mixtures of the invention according to the treating capacity of the concentration of the acid sulphur-containing substance in lighter hydrocarbons and lighter hydrocarbons
Device is answered to carry out separate unit or multi-platform combined use.
Preferred embodiment according to the present invention, two-phase mixtures reactor provided by the invention is using more series connection
Form uses, and the reaction condition in each two-phase mixtures reactor can be identical or different, each independently includes: reaction
Temperature is 25-80 DEG C, reaction pressure 0.2-2MPa.
The method of a kind of preferred embodiment according to the present invention, lighter hydrocarbons desulfurization of the present invention uses Fig. 3
Shown in technique in flow chart carry out, specifically:
In the present invention, fresh lye 16 and/or regeneration lye 18 and lighter hydrocarbons 17 are introduced into caustic wash unit 24, described
In caustic wash unit 24, the acid sulphur-containing substance in lighter hydrocarbons is reacted with the NaOH in lye generates sulfur-bearing sodium salt, and sulfur-bearing sodium salt
It is dissolved in lye.The mixture obtained from the reactor exit of the two-phase mixtures reactor is introduced into the heavy of caustic wash unit
Initial gross separation is carried out in drop equipment, obtains the first sulfur-bearing lye and the first lighter hydrocarbons；Then first lighter hydrocarbons are introduced and is located at institute
It states and carries out the second separation in the sedimentation unit 13 in 24 downstream of caustic wash unit, obtain the second sulfur-bearing lye and desulfurization lighter hydrocarbons 23；Desulfurization
Lighter hydrocarbons 23 enter the processes such as subsequent washing purification and are continued with.And the first sulfur-bearing lye and described second are contained
The sulfur-bearing lye 19 that sulphur lye is formed is introduced into oxidation regeneration unit 14 to react with the progress oxidation regeneration of oxygen-containing gas 20, is aoxidizing
In the reactor of regeneration unit, the sulfur-bearing sodium salt in sulfur-bearing lye 19 is reacted with oxygen-containing gas 20, by containing in sulfur-bearing lye 19
Sulphur sodium salt is converted into disulphide, obtains desulfurization lye.The back suction bill of lading is introduced by the desulfurization lye that oxidation regeneration unit 14 is discharged
Continue the separation of desulfurization lye and disulphide in member 15.In the anti-extraction unit 15, desulfurization lye and light oil
Product 21 contact, and realize the separation of desulfurization lye with the disulphide wherein carried secretly, obtain regeneration lye 18 and sulfur-bearing light-end products
22.The regeneration lye 18 is recycled back to progress lighter hydrocarbons desulfurization in the caustic wash unit 24.
Two-phase mixtures reactor provided by the invention and its application also have the advantages that following specific:
Two-phase mixtures reactor is coupled in lighter hydrocarbons sulfur removal technology, the special construction design of two-phase mixtures reactor both may be used
To strengthen above-mentioned reaction process, and can be with idetified separation process.Two-phase mixtures reactor uses special mixing runner design,
Liquid liquid two-phase mixed at high speed in two-phase mixtures reactor, enhances mass transport process, realizes lighter hydrocarbons deep desulfuration, can will be light
Acid sulphur-containing substance concentration in hydrocarbon is down to the even lower level of 10ppm, and desulfurization degree is up to 90 weight % or more.Two-phase mixtures are anti-
The problem of answering two-phase apparent velocity height in device, being not susceptible to runner blocking.Utilize the high feature of interface tension, it is not necessary to use
Surface reactive material avoids emulsification problem in two-phase mixtures reactor, after two-phase mixtures contact, convenient for split-phase and carries out subsequent
Processing.The treating capacity of two-phase mixtures reactor is big, and structure is simple, and size is small, and voltage endurance capability is strong, convenient for sealing, installation and maintenance.
The present invention will be described in detail by way of examples below.
Below in case of no particular description, used a variety of materials are all from commercially available.
Embodiment 1
The present embodiment carries out the deep desulfuration of sulfur-bearing lighter hydrocarbons using two-phase mixtures reactor of the present invention, specifically such as
Under:
Liquefied gas and lye containing mercaptan contact in caustic wash unit, and mercaptan is reacted with the NaOH in lye generates mercaptan
Sodium is simultaneously dissolved in lye.It is completed after being entered sedimentation unit by the liquefied gas that caustic wash unit is discharged and separated with the part lye that it is carried secretly
The purpose of removal of mercaptans.By sedimentation unit be discharged lye enter oxidation regeneration unit, in filler bubbling bed reactor, lye with
Sodium mercaptides are converted disulphide by air haptoreaction.The desulfurization lye being discharged by oxidation regeneration unit enters the back suction bill of lading
Member is contacted with gasoline, removes the disulphide of entrained with, obtains regeneration lye.The regeneration lye being discharged by anti-extraction unit follows
Loopback caustic wash unit participates in desulfuration of liquefied gas process.
Selected liquefied gas is derived from wuhan petrochemical industry, and volume basis composition is as shown in table 1.
Table 1: liquefied gas hydro carbons volume basis composition
| N-alkane/% | Isoparaffin/% | Alkene/% | |
| C2 | 2.35 | 0 | 1.05 |
| C3 | 44.66 | 0 | 15.96 |
| C4 | 15.73 | 5.89 | 12.87 |
| C5 | 0 | 1.49 | 0 |
The method analysis that acid mercaptan total amount in above-mentioned liquefied gas is provided using SH/T 0222-92, the group of acid mercaptan
It is measured at using GC-SCD chromatography (PONA column).The quality group of surveyed mercaptan total amount becomes methyl mercaptan and accounts for 70.3%, and ethyl mercaptan accounts for
24.4%, propanethiol accounts for 5.3%.
Caustic wash unit and two-phase mixtures reactor used by anti-extraction unit are as depicted in figs. 1 and 2.Two-phase mixtures reaction
It include 19 mixing runners in device, for caustic wash unit, the liquefied gas containing mercaptan enters two-phase mixtures via reactor inlet
In the distributing chamber of reactor, and mixing runner is entered by mixing flow channel entry point.Concentration be 15 weight % NaOH aqueous solution by
Reactor shell side forms drop through distribution hole and enters mixing runner, perpendicular to the cross-sectional area of the mixing runner of lighter hydrocarbons flow direction
For 3mm2, the length for mixing runner is 1000mm.The quantity of distribution hole on the wall of each mixing runner is 4, is distributed hole depth
Degree be 1.0mm, according to flow direction of the lye in reactor shell side, the aperture of each distribution hole be respectively 0.9mm, 1.0mm,
1.1mm and 1.2mm, the centre distance of two neighboring distribution hole are 23mm.Before entering mixing runner, liquefied gas and lye
Flow direction be adverse current.Caustic wash unit is in such a way that two two-phase mixtures reactors are used in series, according to logistics direction,
Temperature in level-one two-phase mixtures reactor is 50 DEG C, pressure 1.2MPa；Temperature in the two-phase mixtures reactor of the second level is
50 DEG C, pressure 0.8MPa.
Liquefied gas is 6m/s in the apparent velocity of mixing flow passage entry, and apparent velocity of the lye in dispersed phase inlet is
0.8m/s, the content of mercaptan sulfur is 1000ppm in liquefied gas.Liquefied gas is sufficiently mixed mass transfer with lye two-phase in mixing runner
Enter collecting chamber afterwards, and draw reactor from reactor outlet, is separated into subsequent separation equipment.
Wherein, after being separated by the fluid that first order two-phase mixtures reactor flows out, liquefied gas enters second level two-phase
Mixing reactor (second level two-phase mixtures reactor is identical as the size of the first order two-phase mixtures reactor) continues
Desulfurization is carried out, by the fluid of second level two-phase mixtures reactor discharge by first point and the desulfurization obtained after separation of sedimentation unit
Liquefied gas afterwards flows out reaction system.In liquefied gas after resulting desulfurization, the content of mercaptan sulfur is 2.4ppm, and desulfurization degree is
99.76 weight %.
Also be used in series using two two-phase mixtures reactors in anti-extraction unit, and the structure of two-phase mixtures reactor with
The structure snd size of the two-phase mixtures reactor of caustic wash unit are all the same.The temperature of first order two-phase mixtures reactor is 50 DEG C,
Pressure is 1.0MPa, and the temperature of second level two-phase mixtures reactor is 50 DEG C, pressure 0.6MPa.Lye is in mixing flow channel entry point
The apparent velocity at place is 6m/s, and apparent velocity of the gasoline in dispersed phase inlet is 0.6m/s.It is entrained in lye after desulfurization
Disulphide, sulfur content 336ppm.The sulfur content in regeneration lye obtained after anti-extraction unit is 12.5ppm.
Due to not adding any surface reactive material that can drop interfacial tension in reaction system, this height of system is utilized
The characteristics of interfacial tension, liquefied gas and lye split-phase can be clarified rapidly in precipitation apparatus, and occur without emulsion layer.
Embodiment 2
The present embodiment carries out the deep desulfuration of sulfur-bearing lighter hydrocarbons using two-phase mixtures reactor of the present invention, specifically such as
Under:
The method of lighter hydrocarbons desulfurization in the present embodiment is similar to embodiment 1, also includes 19 in two-phase mixtures reactor
Runner is mixed, except that:
Lighter hydrocarbons in the present embodiment are light petrol, and it is anti-to only have a two-phase mixtures in caustic wash unit and anti-extraction unit
Answer device.
Selected light petrol is derived from Jiujiang petrochemical industry, and hydro carbons volume basis composition is as shown in table 2.
Table 2: light petrol hydro carbons volume basis composition
| N-alkane/% | Isoparaffin/% | Alkene/% | Diene/% | |
| C4 | 2.141 | 0.978 | 5.237 | 0 |
| C5 | 13.368 | 41.388 | 29.821 | 0.039 |
| C6 | 0 | 5.889 | 1.140 | 0 |
The method measurement that acid mercaptan total amount in light petrol is provided using GB/T 1792-1988, the composition of acid mercaptan
It is measured using GC-SCD chromatography (PONA column).The quality group of surveyed mercaptan total amount becomes methyl mercaptan and accounts for 8.89%, and ethyl mercaptan accounts for
66.7%, propanethiol accounts for 24.4%.
In caustic wash unit: being provided with 3 distribution holes in each mixing runner, distribution hole depth is 1.1mm, and according to alkali
Flow direction of the liquid in reactor shell side, the aperture of each distribution hole are respectively 1.05mm, 0.8mm and 0.6mm, two neighboring
The centre distance of distribution hole is 25mm.Cross-sectional area perpendicular to the mixing runner of lighter hydrocarbons flow direction is 3mm2, mixed flow
The length in road is 500mm.Temperature in two-phase mixtures reactor is 45 DEG C, pressure 1.2MPa.Light petrol enters in mixing runner
Apparent velocity at mouthful is 8m/s, and apparent velocity of the lye in dispersed phase inlet is 0.48m/s, and mercaptan sulfur contains in light petrol
Amount is 78ppm.
Content by mercaptan sulfur in the light petrol of caustic wash unit is 3.2ppm, and desulfurization degree is 95.9 weight %.
In anti-extraction unit: the two-phase mixtures of the caustic wash unit in the structure and the present embodiment of two-phase mixtures reactor are anti-
Answer device structure snd size all the same.The temperature of two-phase mixtures reactor is 52 DEG C, pressure 1.0MPa.Lye enters in mixing runner
Apparent velocity at mouthful is 7m/s, and apparent velocity of the gasoline in dispersed phase inlet is 2m/s.Two sulphur are entrained in desulfurization lye
Compound, sulfur content 52ppm.The sulfur content in regeneration lye obtained after anti-extraction unit is 3.8ppm.
Remaining is in the same manner as in Example 1.
Embodiment 3
The present embodiment carries out the deep desulfuration of lighter hydrocarbons using two-phase mixtures reactor of the present invention, specifically as follows:
The method of lighter hydrocarbons desulfurization in the present embodiment is similar to embodiment 2, except that:
In caustic wash unit: according to flow direction of the lye in reactor shell side, the aperture of each distribution hole is respectively
1mm, 0.7mm and 0.4mm, distribution hole depth are 1mm, and the centre distance of two neighboring distribution hole is 27mm.Perpendicular to lighter hydrocarbons
The cross-sectional area of the mixing runner of flow direction is 6mm2, the length for mixing runner is 1000mm.In two-phase mixtures reactor
Temperature is 50 DEG C, pressure 1.2MPa.Light petrol is 8m/s in the apparent velocity of mixing flow passage entry, and lye enters in dispersed phase
Apparent velocity at mouthful is 1.25m/s.The present embodiment uses light petrol same as Example 2 as lighter hydrocarbons, and thereto
Ethyl mercaptan, which is added, makes the content of mercaptan sulfur in the light petrol of the present embodiment be 1000ppm.
By in the light petrol of caustic wash unit, the content of mercaptan sulfur is 15.6ppm, desulfurization degree is 98.4 weight %.
In anti-extraction unit: the alkali cleaning list in the structure and the present embodiment of the two-phase mixtures reactor in anti-extraction unit
The two-phase mixtures structure of reactor and size of member are all the same.The temperature of two-phase mixtures reactor is 52 DEG C, pressure 1.1MPa.Alkali
Liquid is 6m/s in the apparent velocity of mixing flow passage entry, and apparent velocity of the gasoline in dispersed phase inlet is 3m/s.After desulfurization
Lye in be entrained with disulphide, sulfur content 537ppm.The sulphur in regeneration lye obtained after anti-extraction unit contains
Amount is 42ppm.
Remaining is in the same manner as in Example 2.
Comparative example 1
This comparative example is carried out using method similar to Example 2, the difference is that the two-phase mixtures of this comparative example react
Device is packed extraction tower, and tower diameter 250mm, tower height 2m, bed stuffing height 1.5m, filler is to dissipate heap Raschig ring, Raschig ring
Diameter is 16mm.The processing capacity of packed tower is identical as the ability of two-phase mixtures reactor used in embodiment 1.
Remaining is in the same manner as in Example 2.
As a result: the separating property data of the extraction tower of the de- and anti-extraction unit of the extraction tower of caustic wash unit and 2 phases of implementation
Seemingly, but continuous phase load of the two-phase mixtures reactor provided by the invention on unit cross-sectional area is equivalent to extraction tower
1500 times or more, fully demonstrate that two-phase mixtures reactor volume provided by the invention is small, processing capacity is big, mass transfer in contrast
High-efficient feature.
Comparative example 2
This comparative example is carried out using method similar to Example 2, the difference is that the two-phase mixtures of this comparative example react
Device be concatenated two identical micro- blenders of T-type (runner i.e. where lye with mix runner directly intersect vertically without
The structure of reflux type), the mixing runner cross-sectional area of each mixer is 4mm2.The processing capacity of each micro- blender of T-type
Use a mixing processing capacity for runner of two-phase mixtures reactor of the present invention identical with embodiment 2.
Remaining is in the same manner as in Example 2.
As a result: the desulfurization degree of light petrol is 72 weight %, has fully demonstrated two-phase mixtures provided by the invention in contrast
The high feature of reactor mass-transfer efficiency.
It is can be seen that from the result of the embodiment of the present invention 1-3 and comparative example 1-2 by the present invention in that anti-with two-phase mixtures
When device being answered to carry out lighter hydrocarbons desulfurization, the desulfurization effect of acquirement is obviously better than the desulfurization effect of the prior art.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (14)
1. a kind of method of lighter hydrocarbons desulfurization, this method is implemented in the system for including caustic wash unit, and the caustic wash unit includes two
Reactor is mixed, the two-phase mixtures reactor includes reactor inlet, reactor outlet and reactor tank body, the reaction
It include first partition and second partition in the inner cavity of device tank body, the first partition and the second partition and the reactor tank
Reactor shell side, the first partition and the second partition is formed between the inner wall of body to connect by least one mixing runner
It connects, is provided on the wall of the mixing runner so that the distribution hole that the reactor shell side is connected to the mixing runner；The party
Method includes: to be introduced to lye in the reactor shell side from the dispersed phase entrance of the two-phase mixtures reactor, and described
Lye through the distribution hole enter the mixing runner with pass sequentially through the reactor inlet and the flow channel entry point that mixes draws
The lighter hydrocarbons entered into the mixing runner are contacted；Flow direction of the lye in the reactor shell side with described
The flow direction in runner is mixed on the contrary, the mixture that the lye is formed after contacting with the lighter hydrocarbons successively passes through the mixing
Runner exit and the reactor outlet are led to except the two-phase mixtures reactor；By what is obtained from the reactor outlet
Mixture, which is introduced into the precipitation apparatus of the caustic wash unit, carries out initial gross separation, obtains the first sulfur-bearing lye and the first lighter hydrocarbons；So
First lighter hydrocarbons are introduced into afterwards and carry out the second separation in the sedimentation unit in the caustic wash unit downstream, obtain the second sulfur-bearing
Lye and desulfurization lighter hydrocarbons；And by the first sulfur-bearing lye and the second sulfur-bearing lye be introduced into oxidation regeneration unit with it is oxygenous
Body carries out oxidation regeneration reaction；And the desulfurization lye obtained in the oxidation regeneration unit is introduced into anti-extraction unit and is carried out
Separation obtains regeneration lye；And the regeneration lye is recycled back in the caustic wash unit.
2. according to the method described in claim 1, wherein, the two-phase mixtures reactor further comprises collecting chamber and distribution
Room, the lighter hydrocarbons successively enter the mixed flow by the reactor inlet, the distributing chamber and the mixing flow channel entry point
In road, the mixture that the lye is formed after contacting with the lighter hydrocarbons successively passes through the mixing runner exit, the collecting chamber
It is led to except the two-phase mixtures reactor with the reactor outlet.
3. method according to claim 1 or 2, wherein in the two-phase mixtures reactor, the first partition and institute
State second partition by least two mixing runners connection, it is each it is described mixing runner wall on distribution hole number it is identical or
Difference, and the number of the distribution hole on the wall of each mixing runner is each independently 1-100.
4. method according to claim 1 or 2, wherein in the two-phase mixtures reactor, each distribution hole
Aperture is 0.1-2mm.
5. according to the method described in claim 4, wherein, in the two-phase mixtures reactor, according to the reactor shell side
In lye flow direction, the aperture of the distribution hole is sequentially increased.
6. according to the method described in claim 5, wherein, in the two-phase mixtures reactor, according to the reactor shell side
In lye flow direction, the small 0.01-1mm in aperture of the adjacent distribution hole in the aperture ratio downstream of the distribution hole of upstream.
7. method according to claim 1 or 2, wherein in the two-phase mixtures reactor, in each mixed flow
On the wall in road, the distance of the central point of two neighboring distribution hole is 0.5-40mm.
8. according to the method described in claim 7, wherein, in the two-phase mixtures reactor, in each mixing runner
Wall on, the distance of the central point of two neighboring distribution hole is 1-30mm.
9. method according to claim 1 or 2, wherein in the two-phase mixtures reactor, the depth of the distribution hole
For 0.1-3mm.
10. according to the method described in claim 9, wherein, in the two-phase mixtures reactor, the depth of the distribution hole is
0.3-2.5mm。
11. according to the method described in claim 1, including at least one described two-phase mixtures in the anti-extraction unit wherein
Reactor.
12. method according to claim 1 or 2, wherein apparent velocity of the lye in the dispersed phase inlet be
0.2-5m/s；The lighter hydrocarbons are 0.5-20m/s in the apparent velocity of the mixing flow passage entry.
13. method according to claim 1 or 2, wherein in the caustic wash unit, the lye and the lighter hydrocarbons
Contact conditions include: that temperature is 25-80 DEG C, reaction pressure 0.2-2MPa.
14. according to the method described in claim 1, wherein, the lighter hydrocarbons include sulfur-bearing liquefied gas and/or sulfur-bearing light petrol.
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| CN115746930A (en) * | 2022-11-28 | 2023-03-07 | 中国石油化工股份有限公司 | Micro-channel liquefied gas desulfurization system and application |
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| US20110127194A1 (en) * | 2009-11-30 | 2011-06-02 | Merichem Company | Hydrocarbon Treatment Process |
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| CN1693423A (en) * | 2005-04-29 | 2005-11-09 | 清华大学 | A method for alkaline cleaning of oil products |
| CN101077981A (en) * | 2006-05-24 | 2007-11-28 | 宁波中一石化科技有限公司 | Method for regenerating alkali liquor containing sodium thioalcohol |
| CN102492464A (en) * | 2011-12-02 | 2012-06-13 | 甘肃蓝科石化高新装备股份有限公司 | Gasoline desulfuration and deodorization process |
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