CN103112982A - Method and device for degassing acidic water - Google Patents
Method and device for degassing acidic water Download PDFInfo
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- CN103112982A CN103112982A CN2013100363087A CN201310036308A CN103112982A CN 103112982 A CN103112982 A CN 103112982A CN 2013100363087 A CN2013100363087 A CN 2013100363087A CN 201310036308 A CN201310036308 A CN 201310036308A CN 103112982 A CN103112982 A CN 103112982A
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Abstract
The invention relates to a method and a device for degassing acidic water. The method comprises the following steps of: separating gas dissolved in the acidic water by a decompression method, wherein the separated gas is divided into a gas phase and a liquid phase by a gravity subsiding method; separating gas still dissolved in the acidic water and part of small bubble under the pressure by a whirl centrifugal degassing method, wherein the gas dissolved in the acidic water is separated out as a result of reduction of the partial pressure of the pressure gradient field based on the pressure gradient and centrifuge filed of whirl centrifugal degassing equipment, and further separating the separated gas and small bubbles under the centrifuge field; and as for the gas phase part, removing the carried liquid drop by hydrocyclone separation or agglutination separation. By using the method and device for degassing acidic water, liquid in the gas is effectively removed, and the shortage of the conventional acidic water degassing tanks is overcome.
Description
Technical field
The present invention relates to the degassed method and apparatus of a kind of sour water, relate in particular to a kind of flash distillation-centrifugal coupling technique that utilizes and carry out the degassed method and apparatus of sour water.
Background technology
In Crude Oil Processing, the part sulphur in crude oil, nitrogen enter into the form of hydrogen sulfide, ammonia the sour water that CDU is discharged.Subsequently, acidic water stripping device will carry out pre-treatment from the sour water of the devices such as atmospheric and vacuum distillation, catalytic cracking, delayed coking, hydrocracking, hydrofining and sulfur recovery, make purifying waste water after processing can be back to the process upstream device, or satisfy influent quality requirement into the sewage-farm, hydrogen sulfide in sour water, ammonia remove and are reclaimed by steam stripped mode, so not only purify sour water, also reduced the refining losses of enterprise.Therefore, the sour water stripping is the indispensable environmental protecting device of refinery.And from each sour water that installs of refinery, can carry or dissolve the gases such as a part of hydrocarbon gas, H2S and NH3 secretly and enter acidic water stripping device under certain pressure, along with sour water flows to the tank field, the pressure of material reduces gradually, originally be in the part lower carbon number hydrocarbons vaporization of liquid state, become gas, when entering the people tank field, sour water discharges into gas phase, therefore the sour water degassing vessel can be set before sour water enters acid water pot carries out Separation and Recovery to gas, and the gas that tank deck is deviate from enters low pressure gas pipe network or burning.
The sour water degassing vessel adopts horizontal, overhead placement usually at present, the principle that adopts is flash distillation-gravity settling separation technology, because the micro-bubble that disperses in the water that leans on flash evaporation can't effectively remove, flash separation is gone out to dissolved gases under this degassing vessel working pressure also can't effectively be removed by gravity settling, this portion gas extends and also can separate out at tank deck due to pressure decreased and settling time after entering downstream sour water purification pot, cause potential safety hazard and resource loss, therefore needed to adopt more efficient sour water Degassing Technology to process.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the invention provides a kind of flash liberation and centrifugal degassed coupling technique of utilizing the entrained gas of sour water with pressure and this minute are depressed the method and apparatus that solution gas carries out high efficiency separation.The method that the technology of the present invention adopts flash separation to combine with centrifugation is processed sour water, before the flash tank outlet, rotary fluid gas separation facilities is set, rely on the pressure gradient field that rotary fluid gas separates (radial section from pressure reduce gradually) outside to inside further to separate, relies on the centrifugal field of rotary fluid gas separation that micro-bubble is effectively removed dissolved gases under the flash tank working pressure, be provided with gas-liquid separator before gaseous phase outlet, entrained liquids in gas is effectively removed, made up the deficiency of present sour water degassing vessel.
Concrete technical scheme is:
A kind of method that sour water is degassed is characterized in that, comprises the following steps:
Step 1: adopt step-down to process gassiness sour water is carried out the separation of liquid gas, the pressure of gassiness sour water is 0.2～20MPa, and pressure is reduced to 0.01～19.99MPa, and treatment temp is 5～99 ℃;
Step 2: the pressure gradient field of adopting that centrifugal degassing method relies on that rotary fluid gas separates is carried out liquid gas to sour water and is separated, and this pressure gradient field internal pressure differences is 0.01～10MPa, and treatment temp is 5～99 ℃;
Step 3: adopt the method for centrifugal or coarse separation that gas entrainment liquid in gaseous phase outlet is separated, this sepn process pressure is reduced to 0.0001～0.05MPa.
Further, the step-down in described step 1 is treated to flash distillation.
A kind ofly realize aforementioned de-gassing vessel, comprise the centrifugal degassing equipment of eddy flow that a decompression device and is attached thereto, the centrifugal degassing equipment of this eddy flow comprises shell, be arranged at the centrifugal degassed core pipe of a plurality of parallel connection rotational flows in shell, be arranged at entrance, liquid-phase outlet and gaseous phase outlet on shell, the centrifugal degassed core pipe of this eddy flow comprises a cavity, this cavity is provided with the import of core pipe liquid gas, core pipe gaseous phase outlet and core pipe liquid-phase outlet, this core pipe gaseous phase outlet inserts in this cavity from this cavity upper surface center, and depth of penetration is 0.1～3 times of this cavity maximum diameter.
Further, this decompression device is one to be provided with the flash tank of entrance, gaseous phase outlet and liquid-phase outlet, the centrifugal degassing equipment enclosure of described eddy flow is communicated with this flash tank, be placed between de-gassing vessel entrance and gaseous phase outlet, form a complete cavity with this flash tank, the liquid-phase outlet of the centrifugal degassing equipment of this eddy flow is the liquid-phase outlet of this de-gassing vessel.
Further, this decompression device is a cold low separator, and its outlet is connected with the centrifugal degassing equipment entrance of eddy flow.
Further, the entrance liquid feeding form of described flash tank adopts multitube Venturi spray pattern.
Further, described de-gassing vessel top also is provided with liquidometer.
beneficial effect of the present invention is: at first the degas method that the present invention adopts utilizes the reduction flashing pressure, to be dissolved in the hydrocarbon gas of sour water, the air release such as H2S and NH3 out, at first sour water being carried the solution gas that gas and pressure drop discharge under the gravity field effect separates, to under this degassing vessel working pressure dissolved gases by flash evaporation can't effectively remove thereafter, the micro-bubble that disperses in the water that flash separation is gone out also can't effectively be removed by gravity settling and utilize centrifugal degas method to carry out secondary separation, this minute, the gas dissolved depressed relied on the pressure gradient field that rotary fluid gas separates (radial section from pressure reduce gradually) outside to inside to separate, the micro-bubble of carrying secretly in sour water relies on centrifugal field effectively to remove.
In the method for the invention, carry out also needing with pump, degassed rear sour water to be carried out the outer defeated words of supercharging after flash liberation as sour water in technique, can directly adopt centrifugal degas method to carry gas to import sour water and solution gas separates, can further effectively reduce like this energy consumption of repressurize after step-down.
That the equipment that the present invention adopts has is simple to operate, floor space is little, the degassing efficiency advantages of higher, overcome present sour water after degassing vessel in downstream line, equipment partial drop of pressure cause air release and the local corrosion (H2S), vapour lock and resource loss (hydrocarbon gas) problem that cause, can be widely used in the sour water treating processes of petrochemical process.
Description of drawings
Fig. 1 is the structural representation of the acid de-gassing vessel of first embodiment of the invention.
Fig. 2 is the first embodiment of the invention process flow sheet.
Fig. 3 is the structural representation of the acid de-gassing vessel of second embodiment of the invention.
Fig. 4 is the second embodiment of the invention process flow sheet.
Fig. 5 is the structural representation of the degassed core pipe of eddy flow.
Fig. 6 is the centrifugal degassed core pipe pressure Gradient distribution schematic diagram of eddy flow, comprise the centrifugal degassed core tubular construction schematic diagram of Fig. 6-1 eddy flow, the centrifugal degassed core pipe of Fig. 6-2 eddy flow is along the radial pressure schematic diagram of the sectional view of A-A hatching line, and the centrifugal degassed core caliber of Fig. 6-3 eddy flow is to cross section pressure gradient distributed simulation figure.
Nomenclature:
1 is flash tank, and 11 is entrance, and 12 is tank body, and 13 is gaseous phase outlet, and 2 is the centrifugal degassing equipment of eddy flow, and 21 is the centrifugal degassed core pipe of eddy flow, and 21-1-1 is the import of core pipe liquid gas axial-flow type; 21-1-2 is that core pipe liquid autogenous cutting is to import; 21-2 is core tubing string chamber; 21-3 is core pipe cone chamber; 21-4 is core pipe liquid-phase outlet; 21-5 is core pipe inner cone; 21-6 is core pipe upflow tube back taper heavy wall; 21-7 is the two not good liquor outlets of core pipe; 21-8 is core pipe ring groove gap, 21-9 is core pipe inspection secondary separation upflow tube, and 21-9-1 is hydraucone, and 21-9-2 is core pipe the first overflow tubing string chamber, 21-9-3 is core pipe back taper connection chamber, 21-9-4 is core pipe the second overflow tubing string chamber, and 21-9-5 is the core tube cylinder, and 22 is shell, 23 is liquid-phase outlet, 24 is the sour water entrance, and 25 is liquid level meter, and 26 is gaseous phase outlet.
Embodiment
On technique, the band gas sour water the first step is separated dissolved gases in sour water by the step-down method, and isolated gas relies on the method for gravity settling to be divided into gas phase and liquid phase; The gas and the part micro-bubble that still are dissolved in sour water under this pressure separate by the centrifugal degas method of the eddy flow of second step, rely on pressure gradient and the centrifugal field of the centrifugal degassing equipment of eddy flow, the gas that is dissolved in sour water is because the reduction of pressure gradient field dividing potential drop is separated out, and this part bubbing and micro-bubble are further separated under centrifugal field; The gas phase part goes out device after removing the drop that carries totally by cyclonic separation or coarse separation.
The centrifugal degassed core pipe of eddy flow involved in the present invention comprises and is provided with a cavity, this cavity is provided with the import of liquid gas, gaseous phase outlet and liquid-phase outlet, this gaseous phase outlet inserts in this cavity from this cavity upper surface center, and depth of penetration is 0.1～3 times of this cavity maximum diameter.This depth of penetration is that gaseous phase outlet end, the gaseous phase outlet least significant end that namely is positioned at cavity are to the degree of depth of cavity upper surface.
Further, described cavity comprises a post chamber, is arranged under the post chamber with one, maximum diameter is identical and the cone chamber that is communicated with it or post chamber.
Further described gaseous phase outlet realizes by a upflow tube, and to be diameter become large spray chamber by supreme under the chamber to the runner of this upflow tube gradually.
Further, described injection upflow tube end is provided with the annular space fluting.
Further, this device also is provided with a cylindrical shell and surrounds described upflow tube forming the cavity of a sealing, and this closed cavity lower end offers the secondary liquid-phase outlet.
Further, described upflow tube gos deep into cavity part end and also is provided with a hydraucone.
Further, described upflow tube gos deep into also being provided with a back taper heavy wall on described cavity part end perisporium, and the import of described liquid gas is higher than the base of this back taper heavy wall.
Further, this bottom, cone chamber is provided with an interior centrum, and this inner cone base area gos deep into the base area of cavity part end greater than gaseous phase outlet.
Further, the tangential outlet of described liquid-phase outlet employing, the outlet bottom is concordant bottom inner cone.
Further, the import of described liquid gas can be adopted axial-flow type, tangential, spiral-line or involute urve form.
See also Fig. 6, this patent inventor studies discovery by experiment, is 0.5～3 times of position of post chamber diameter at post chamber height, and there is significant pressure gradient in eddy flow core bore to the cross section, i.e. radial position pressure from outside to inside reduces gradually.According to Henry's law, near this cross-sectional height, swirler core tube edge wall liquid pressure is high, center pressure is low, the outside wall is depressed gas dissolved in this minute and be can migrate to the central position, the overflow gaseous phase outlet is located at this position can further be removed dissolved gases in liquid under certain intake pressure, utilize centrifugal field to remove entrained liquids the centrifugal Degassing Technology of present eddy flow and widen and utilize centrifugal field to be combined with the pressure gradient field, remove the gas dissolved that entrained liquids and import liquid necessarily minute are depressed.
see also Fig. 5, specific embodiment for the centrifugal degassed core pipe 21 of eddy flow involved in the present invention, the centrifugal degassed core pipe of this eddy flow comprises that the core pipe cone chamber 21-3(that is located at the bottom also can be the post chamber), be located on core pipe cone chamber 21-3, identical and the core tubing string chamber 21-2 that is communicated with it of maximum diameter, this core pipe cone chamber 21-3 and core tubing string chamber 21-2 form a closed cavity, the closed cavity bottom is provided with a core pipe liquid-phase outlet 21-4, closed cavity top is provided with the import of liquid gas, closed cavity top is provided with a gaseous phase outlet, this gaseous phase outlet inserts closed cavity from upper surface, the degree of depth of inserting is 0.1～3 times of cavity maximum diameter, and be arranged at the cavity center, gaseous phase outlet is one to fall hydraucone, its tail end section is over against the central position of radial section pressure gradient field pressure minimum, collect the gas phase of overflowing because center pressure is less in order to utilize as much as possible pressure gradient.This gaseous phase outlet is specifically realized by a core pipe inspection secondary separation upflow tube 21-9, as shown in the figure, this core pipe inspection secondary separation upflow tube 21-9 is arranged on the 21-2 central shaft of core tubing string chamber, comprise a core pipe hydraucone 21-9-1, core pipe the first overflow tubing string chamber 21-9-2 and a core pipe back taper connection chamber 21-9-3, with core pipe the second overflow tubing string chamber 21-9-4, forming radius first reduces the injection shape overflow cavity of rear increase, can strengthen the collection and confinement of gases area, improve gaseous phase outlet pressure when improving the collection and confinement of gases rate.This core pipe second overflow tubing string chamber 21-9-4 week side offers annular space fluting 21-8, core pipe ring gap fluting 21-8 is provided with a core tube cylinder 21-9-5 outward and surrounds described upflow tube to form the cavity of a sealing, this core tube cylinder 21-9-5 bottom offers two not good liquors outlet 21-7, in core pipe the second overflow tubing string chamber 21-9-4, in order to utilize gas rotating centrifugal force that the liquid of gas entrainment is carried out effective elimination, realize effective separation of entrained liquids in gas, can eliminate the problem because of the secondary separation of exit gas entrained liquids.The lower end of core pipe the first overflow tubing string chamber 21-9-2 also is provided with a hydraucone 21-9-1, overflows gas with large as far as possible catching.This hydraucone 21-9-1 week side is provided with a core pipe upflow tube back taper heavy wall 21-6, this core pipe upflow tube back taper heavy wall 21-6 is from this hydraucone 21-9-1 one until the upper surface of core tubing string chamber 21-2, carries out liquid gas and separates so that the liquid gas that guiding enters from the liquid gas import that is arranged at cavity top or top enters pressure gradient significant zone as early as possible because the space increases gradually.The import of above-mentioned liquid gas can be adopted axial-flow type, tangential, spiral-line or involute urve form.Be provided with centrum 21-5 in a core pipe bottom this core pipe cone chamber 21-2, this core pipe inner cone 21-5 base area gos deep into the base area of cavity part end hydraucone 21-9-1 greater than gaseous phase outlet, and in outlet liquid, gas carries to reduce.
For the ease of observing, the centrifugal degassed core pipe of the eddy flow in all the other accompanying drawings does not remake the details sign.
Embodiment 1:
See also Fig. 1, structural representation for the acid de-gassing vessel of the first embodiment of the present invention, this device comprises flash tank 1 and the centrifugal degassing equipment 2 of eddy flow that is communicated with it, flash tank 1 comprises a shell 12, a sour water entrance 11, with gaseous phase outlet 13, the centrifugal degassing equipment 2 of eddy flow comprises a shell 22, is arranged at the centrifugal degassed core pipe 21 of a plurality of aforementioned eddy flow in shell 22, and the centrifugal degassing equipment of eddy flow 2 bottoms are provided with a liquid-phase outlet 23.Centrifugal degassing equipment 2 internal communication of flash tank 1 and eddy flow form a closed cavity, and this closed cavity is provided with a sour water entrance 11, liquid-phase outlet 23 and gaseous phase outlet 13.
The steam stripped technical process of refinery sour water realizes by following steps usually: the sour water with pressure of taking gas is undertaken degassed by flash distillation, isolated liquid phase is further carried out oil phase by the water oil removal plant and is reclaimed, liquid phase continues to enter purification sour water storage tank, is processed by pump delivery to stripping tower at last.
Compare existing technical process, the present invention has further adopted aforementioned means as shown in empty frame.see also Fig. 2, be the first embodiment of the invention process flow sheet: at first, sour water carries out low pressure flash in flash tank, under the gravity field effect, the solution gas that sour water carries gas and pressure drop release separates, thereafter, can't effectively remove by flash evaporation at 2 pairs of centrifugal degassing equipments of eddy flow dissolved gases under the flash tank working pressure, the micro-bubble that disperses in the water that flash separation is gone out also can't effectively be removed by gravity settling and utilize centrifugal degas method to carry out secondary separation, particularly, this minute, the gas dissolved depressed relied on the pressure gradient field that rotary fluid gas separates (radial section from pressure reduce gradually) outside to inside to separate, the micro-bubble of carrying secretly in sour water relies on centrifugal field effectively to remove.Eddy flow or coalescent gas-liquid separator are set before gaseous phase outlet, the liquid of gas entrainment is effectively removed.
Table 1 is character and the operating parameters of certain refinery acidic water stripping device charging sour water, and that advances this stripper plant has coking sour water, catalysis sour water and the normal decompression of part sour water.
Table 1
according to above-mentioned flow process, each installs the sour water mixing and enters flash liberation tank 1 by entrance 11, the working pressure of flash tank 1 is 0.3MPa, sour water after separating first through flash tank 1 is established the centrifugal degassing equipment 2 of eddy flow before outlet, the limit wall pressure power of the centrifugal degassed core pipe of eddy flow in the centrifugal degassing equipment 2 of eddy flow is 0.3MPa, the central position is 0.001MPa, gaseous phase outlet sectional position pressure is 0.0001Mpa, dissolved gases in flash tank 0.3MPa outlet sour water is carried out secondary separation, the gas phase that secondary separation goes out gets back to by the second overflow tubing string chamber 21-9-4 that flash tank 11 is interior together enters gaseous phase outlet 13 with other isolated gases, entering the downstream gas-treatment means after by the cyclone gas-liquid separating core pipe that arranges before gaseous phase outlet, gas entrainment liquid effectively being removed processes, the liquid phase that secondary separation goes out flows out by the liquid-phase outlet 23 of the centrifugal degassing equipment of eddy flow, enters the downstream liquid-phase treatment apparatus and processes.
Implementation result adopts this technology when flash liberation tank working pressure is 0.3MPa, to this sour water carry and the gas dissolved separating effect to reach flash liberation tank working pressure be separating effect (under 0.01MPa, separation efficiency 〉=99%) under the 0.01MPa condition.
Compare with former technical process (being that sour water directly carries out Acidulous water oil removing purification, gaseous volatilization, carries out the sour water stripping by flash distillation), have following beneficial effect:
1, a large amount of hydrocarbon gas at sour water flash distillation-centrifugal degasification process efficient recovery, purify volatilization gas minimizing in the sour water storage tank, have improved gas reclaiming rate and have reduced potential safety hazard;
2, in sour water, H2S gas effectively separates in sour water flash distillation-centrifugal degasification process, can reduce the energy consumption of sour water stripping process;
3, eliminated at the degassed corrosion of piping that causes the H2S gas evolution to bring because of pressure-drop in pipeline to the sour water stripping process of sour water.
4, the Vapor Entrainment drop has carried out effective removal, has reduced gas entrainment liquid and the environmental protection and the safety problem that produce.
Embodiment 2:
See also Fig. 3, structural representation for the acid de-gassing vessel of the second embodiment of the present invention, this device comprises the centrifugal degassing equipment 2 of eddy flow, the centrifugal degassing equipment 2 of eddy flow comprises a shell 22, be arranged at the centrifugal degassed core pipe 21 of a plurality of aforementioned eddy flow in shell 22, also be provided with an entrance on centrifugal degassing equipment 2 shells 22 of eddy flow, this shell 22 bottoms are provided with a liquid-phase outlet 23, this shell 22 tops also are provided with liquid level meter 25, and this shell 22 tops are provided with cyclone gas-liquid separating core pipe and gaseous phase outlet 26.
Hydrogenation unit is sent the sour water processing technological flow outside and usually realized by following steps: the sour water with pressure of taking gas enters the cold low separator, and to carry out three-phase settlement separate, and isolated gas phase, oil phase reclaim, and liquid phase is sent to stripper plant as sour water and processes.
Compare existing technical process, the present invention has further adopted aforementioned means as shown in empty frame after the sour water outlet of cold low separator.see also Fig. 2, be the first embodiment of the invention process flow sheet: at first, sour water enters the cold low separator and carries out the step-down separation, thereafter, can't effectively remove by flash evaporation at 2 pairs of centrifugal degassing equipments of eddy flow dissolved gases under cold low separator operation pressure, the micro-bubble that disperses in the water that flash separation is gone out also can't effectively be removed by gravity settling and utilize centrifugal degas method to carry out secondary separation, particularly, this minute, the gas dissolved depressed relied on the pressure gradient field that rotary fluid gas separates (radial section from pressure reduce gradually) outside to inside to separate, the micro-bubble of carrying secretly in sour water relies on centrifugal field effectively to remove.
It is 25～30t/h that certain refinery hydrogenation unit is sent the sour water flow outside, and pressure is 1.9～2.2MPa, and temperature is 30～50 ℃, and oil-contg is 200～500mg/L.The problems such as the pipeline local corrosion that causes due to gas sucking-offs such as pipeline pressure drop dissolved hydrogen sulfide, lighter hydrocarbons in sending process outside for fear of this sour water, vapour lock, to send the row that advances outside centrifugal degassed, the sour water after degassed is delivered to acidic water stripping device outward to this sour water.According to above-mentioned technical process, the centrifugal degassed core tube edge wall dividing potential drop of the built-in eddy flow of the centrifugal degassing equipment of the design of the centrifugal degassing equipment of eddy flow is 1.9～2.2MPa, and the central position is 0.5MPa, and gaseous phase outlet cross section pressure is 0.35MPa.
Implementation result: adopt this technology when sour water pressure is 1.9～2.2MPa, to this sour water carry and the gas dissolved separating effect to reach flash liberation tank working pressure be separating effect (under 0.5MPa, separation efficiency 〉=99%) under the 0.5MPa condition.
Compare with former flow process:
1, lighter hydrocarbons recovery efficient improves, and has reclaimed resource, and the device productivity effect promotes;
2, far away to the general fed distance of acidic water stripping device because of hydrogenation unit sour water, eliminated the vapour lock problem that sour water causes gas evolution to bring due to the reduction of pipeline local pressure in pipe conveying procedure, promoted the security of carrying;
3, eliminated in the course of conveying because the pipeline local pressure reduces the pipeline localized corrosion problems that causes the H2S gas evolution to produce.
Only for the preferred embodiment of invention, be not to limit practical range of the present invention in sum.Be that all equivalences of doing according to the content of the present patent application the scope of the claims change and modify, all should be technology category of the present invention.
Claims (7)
1. the method that sour water is degassed, is characterized in that, comprises the following steps:
Step 1: adopt step-down to process gassiness sour water is carried out the separation of liquid gas, the pressure of gassiness sour water is 0.2～20MPa, and pressure is reduced to 0.01～19.99MPa, and treatment temp is 5～99 ℃;
Step 2: the pressure gradient field of adopting that centrifugal degassing method relies on that rotary fluid gas separates is carried out liquid gas to sour water and is separated, and this pressure gradient field internal pressure differences is 0.01～10MPa, and treatment temp is 5～99 ℃;
Step 3: adopt the method for centrifugal or coarse separation that gas entrainment liquid in gaseous phase outlet is separated, this sepn process pressure is reduced to 0.0001～0.05MPa.
2. the degassed method of sour water as claimed in claim 1, is characterized in that, the step-down in described step 1 is treated to flash distillation.
3. realization de-gassing vessel as described in claim 1 method, comprise the centrifugal degassing equipment of eddy flow that a decompression device and is attached thereto, it is characterized in that, the centrifugal degassing equipment of this eddy flow comprises shell, be arranged at the centrifugal degassed core pipe of a plurality of parallel connection rotational flows in shell, be arranged at the entrance on shell, liquid-phase outlet and gaseous phase outlet, the centrifugal degassed core pipe of this eddy flow comprises a cavity, this cavity is provided with the import of core pipe liquid gas, core pipe gaseous phase outlet and core pipe liquid-phase outlet, this core pipe gaseous phase outlet inserts in this cavity from this cavity upper surface center, depth of penetration is 0.1～3 times of this cavity maximum diameter.
4. de-gassing vessel as claimed in claim 3, it is characterized in that, this decompression device is one to be provided with the flash tank of entrance, gaseous phase outlet and liquid-phase outlet, the centrifugal degassing equipment enclosure of described eddy flow is communicated with this flash tank, be placed between de-gassing vessel entrance and gaseous phase outlet, form a complete cavity with this flash tank, the liquid-phase outlet of the centrifugal degassing equipment of this eddy flow is the liquid-phase outlet of this de-gassing vessel.
5. de-gassing vessel as claimed in claim 3, is characterized in that, this decompression device is a cold low separator, and its outlet is connected with the centrifugal degassing equipment entrance of eddy flow.
6. de-gassing vessel as claimed in claim 3, is characterized in that, the entrance liquid feeding form of described flash tank adopts multitube Venturi spray pattern.
7. de-gassing vessel as claimed in claim 3, is characterized in that, described de-gassing vessel top also is provided with liquidometer.
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