CN203763912U - Three-phase separation device - Google Patents
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- CN203763912U CN203763912U CN201420151255.3U CN201420151255U CN203763912U CN 203763912 U CN203763912 U CN 203763912U CN 201420151255 U CN201420151255 U CN 201420151255U CN 203763912 U CN203763912 U CN 203763912U
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Abstract
The utility model relates to a three-phase separation device which comprises a shell and an inner piece, wherein the shell is provided with a feeding hole, a liquid light phase outlet, a gas pocket, a gas phase outlet, an oil pocket or a water pocket, a liquid heavy phase outlet, a liquid indicator and a position meter in the flowing direction of three phases; the inner piece is provided with a gas-liquid inertia separation distributor, a rotating flow jetting gas desorbing tube, a baffling coalescence plate, a pored corrugated coalescence plate, a hydrophilia corrugated plate, a wire mesh demister and a nano polymerized fiber coalescence layer; the gas-liquid inertia separation distributor is connected with the feeding hole; the wire mesh demister is mounted inside the gas pocket; the baffling coalescence plate is mounted at the boundary of gas and liquid. The device provided by the utility model is small in size, high in separation speed, high in efficiency, wide in application range, stable in performance, and long in service life, and can be widely applied to various processes of energy chemical engineering.
Description
Technical field
The utility model is to belong to derived energy chemical process liquid-liquid three phase separation technical field, the method that relates to a kind of oily dewater degassed or water degasification oil removing, specifically, relate to adopt that gas-liquid inertial separation distributes, rotating flow sprays degassed, gravitational settling and the optimum organization of combination coalescence technology, realize three-phase efficiently, separated rapidly, be suitable for various technique and comprise the processes such as the dehydration of hydro carbons of oil extraction purification, sewage disposal, petroleum refining process is degassed, the dehydration of chemical process hydro carbons is degassed.The utility model also relates to the device using in a kind of above-mentioned three phase separation process.
Background technology
In oil exploitation, petroleum refining and chemical process, operative liquid water and gas remain in oil, have a strong impact on safety, reduce product quality, increase power consumption of polymer processing; Or oil-containing and can carry part hydrocarbon gas or sour gas secretly in the water after processing, has caused larger resource loss and has brought environmental issue.For example, in oil extraction, mostly adopt water injection type exploitation, in crude oil Produced Liquid, can carry the impurity such as a large amount of water and natural gas secretly, and in isolated water, oil is understood entrained oil and hydrocarbon gas or sour gas; In lubricating oil and hydraulic system, moisture gassiness can cause the oxidation of burn into oil, chemical attack, bearing fatigue life reduces and greasy property loss; In hydrogenation technique, owing to containing moisture in crude oil, while going out device, diesel oil also can carry a small amount of moisture, and can, with the hydrogen of participating in reaction, inevitably run into the degassed process of oil dehydration; In alkyl plant, water content in raw material is to reaction efficiency important, and General Requirements water content is less than 20ppm, and the existence of ethene also can increase the consumption of catalyst, therefore, be badly in need of the liquid-liquid three phase separator of the degassed or water degasification oil removing of the oil dehydration of highly effective.
The degassed dehydration in oil of take is example: the water in oil generally exists with the form of free state, dispersed, emulsification state and solubilised state.The water of free state is coalescent water, is more segregative water; The water of dispersed, due in micron particles yardstick, is generally less than 100 microns, and starts to occur water in oil situation; Emulsification state water is oil-in-water or the water in oil state existing in oil, and the drop particle diameter of general emulsification state is 3-50 particulate.Gas in oil generally exists with the form of entrained gas and microbubble, because liquid phase surface tension is large, increases gas floating resistance, and microbubble is almost difficult to simple dependence buoyancy and separation.Meanwhile, little water droplet condenses upon around bubble, and under the effect of the vertical buoyancy of bubble, bubble water droplet is around difficult to sedimentation in oil, and bubble is also difficult to floating, has further increased liquid-liquid separating difficulty; On the one hand, under this operating pressure, in oil, also can there is the gas that is partly dissolved state in addition, after downstream unit, can bring resource loss and other problem, therefore, adopt efficient degassed dehydration technique particularly important.
The common oily water separation technique of petroleum chemical industry has centrifugal process, absorption method, membrane separation process, settling methods and coalescent method.The adaptability of centrifugal process is not strong, cost is high, treating capacity is little, operating condition requires harsh, and Chinese patent 101397506A discloses a kind of diesel oil dewatering process and device, mainly the diesel oil of hydrocracking process is carried out to cyclonic separation, water content in diesel oil is down to below 40mg/kg, but Water-In-Oil and dissolved water etc. be very difficult to be obtained effective separatedly, in isolated water, carry diesel oil secretly, caused the wasting of resources; Adsorption filtration wait fine method separated with film can absorb the moisture in oil, but limited for the situation effect of removing water emulsification or that dissolve from oil, in addition, their treating capacity is undesirable, once absorb saturatedly, just must change, and cost is very high.
Gravitational separation process is to utilize the density contrast of oil-water-gas and mutually insoluble, realizes three phase separation, from practical standpoint under static or flox condition, gravity based separation process is without additional motoricity, do not consume medicament, operation and maintenance cost is low, is a kind of most economical method.Tradition gravity settler can only be removed the water of free state and the gas of carrying secretly, Water-In-Oil in oil (disperse water), dissolved water and microbubble are difficult to remove, Chinese patent CN1204948C discloses a kind of three phase separator, comprise a horizontal retort groove, be provided with the independent outlet of a charging aperture and three-phase material.The initial separator that also comprises a gas zones, the tilted return tray of a gas zones, return tray lower end is positioned near entrance section, forms a passage between the two, has reduced the turbulent flow in liquid phase, has strengthened liquid liquid phase sedimentation separation efficiency.
The coalescent coarse that claims is again the hydro carbons that makes entrapped moisture when the device of coalescent filler is housed, the process that water droplet changes from small to big.Chinese patent CN101857286A discloses a kind of folded plate coalescent deoiling filler, use the material of different surface roughness and offered heavy mud hole, except oilhole and fixing hole, increased the effect of coalescent oil droplet.
The common gas-liquid separation technology of petroleum chemical industry has heating, negative pressure method, absorption method and gravitational separation process.The energy consumption of heating and negative pressure method is high, and is difficult to meet the requirement of high throughput.Absorption method cost is high, is difficult to long-term operation.Gravity Separation is difficult to microbubble to carry out effective separation.Chinese patent 103071318A discloses a kind of device that utilizes eddy flow or centrifugal field and the coupling of barometric gradient field to carry out liquid degassing, and for liquid degassing provides new thinking, but this device does not relate to three phase separation field.
At PETROLEUM PROCESSING and chemical field, liquid gas is separated separated with liquid liquid to carry out conventionally in different equipment, often all in Pressure Vessel, carries out at present.A plurality of pressure vessels have not only increased manufacturing cost, and have increased floor space, have improved operation easier, and service life disunity, strengthen rectification difficulty.Both carried out liquid gas separated, the liquid-liquid three phase separator that carries out again the separation of liquid liquid has solved the problems referred to above, urgently efficiently, the dewater method and apparatus of degassed three phase separation of the hydro carbons that uses of long period.
Utility model content
In order to solve a difficult problem for three phase separation in above-mentioned derived energy chemical, the utility model provides a kind of device that is applicable to three phase separation, and concrete technical scheme is as follows:
A kind of three-phase separating device, described device comprises shell and internals, according to the flow direction of three-phase, described shell is provided with charging aperture, liquid light phase export, gas bag, gaseous phase outlet, oil bag or water bag, liquid heavy out, liquid level gauge and interfacial meter, and described internals are provided with the gas-liquid inertial separation distributor, the rotating flow that are connected with described charging aperture and spray the coalescent layer of the poly-fiber of deaeration pipe, baffling coalescing-plate, perforate ripple coalescing-plate, hydrophily corrugated plating, wire mesh demister and nanometer.
Described wire mesh demister is arranged in gas bag, and three phase separation gas out must remove the liquid that gas is carried secretly through wire mesh demister, is greater than the drop of 3～5 μ m mainly for separating of diameter; Described baffling coalescing-plate is installed gas-liquid interface place.
Described gas-liquid inertial separation distributor is positioned at the centre of liquid stream cross section, and its form can be tube having holes or distribution of inertia arc shaped blade group.
Described rotating flow sprays deaeration pipe and has one or more horizontal tangential inlets, on upper and lower top, be respectively equipped with gas vent and liquid outlet, the center of described liquid outlet is provided with cone, and, described liquid outlet is shaped telescopic tube form, and the outer setting of corresponding described liquid outlet has umbrella liquid distributor.
Described rotating flow sprays deaeration pipe and can be installed in parallel, and meets treating capacity requirement.
Described baffling coalescing-plate adopts hydrophilic oleophobic or oleophilic drainage material, is stainless steel, polypropylene, polytetrafluoroethylene (PTFE) or other material.
The corrugated plating group that described perforate ripple coalescing-plate is placed for pressing certain angle, ripple direction is consistent with liquid flow path direction, at crest and trough place, respectively opens circular hole, and the diameter of described circular hole is 5～50mm, and pitch-row is 5～100mm, and corrugated plating spacing is 5～50mm.
The coalescent layer of the poly-fiber of described nanometer is formed by organic fiber and inorfil braiding, can use glass fibre, polytetrafluoroethylene fibre, polypropylene fibre and stainless steel fibre etc., is guaranteeing that under shaping strength condition, braiding ratio is according to the corresponding adjustment of processing accuracy.
The coalescent layer of the poly-fiber of described baffling coalescing-plate, perforate ripple coalescing-plate and nanometer adopts modular mode setting.
Described three-phase separating device is horizontal type gas and liquid liquid three phase separator or vertical liquid-liquid three phase separator; When using described horizontal type gas and liquid liquid three phase separator to carry out three phase separation, the structure that is folded to of baffling coalescer has increased the chance that drop is captured more, the drop not being removed is captured through identical effect at next turning, and repeated action, has improved demist efficiency greatly.Described baffling coalescer is mainly arranged on gas-liquid interface place.The probability that both can increase trapping drop, has also solved in gas separation process and liquid flow process, easily produces foam on gas-liquid interface, has a strong impact on the difficult problem that liquid level and position, boundary are controlled.
The entrance of horizontal type gas and liquid liquid three phase separator is difficult to install turn of tidal stream and sprays degassed core pipe, and therefore, for gas-liquid separation, the effect of vertical liquid-liquid three phase separator is better than horizontal type gas and liquid liquid three phase separator; In vertical liquid-liquid three phase separator, the horizontal displacement distance of mixing material is limited, and therefore, for water-oil separating, horizontal type gas and liquid liquid three phase separator is better than vertical liquid-liquid three phase separator.
Beneficial effect
The utility model adopts that gas-liquid inertial separation distributes, rotating flow sprays degassed, gravitational settling and the optimum organization of combination coalescence technology after, greatly improved separative efficiency, reduce Operation and Maintenance cost, equipment volume, become the key breakthrough of petrochemical industry liquid-liquid three phase separation technical field.
Accompanying drawing explanation
Fig. 1 is the three phase separation process chart of embodiment;
Fig. 2 is the structural representation that the rotating flow of embodiment 1 sprays deaeration pipe;
Fig. 3 is the structural representation of the horizontal type gas and liquid liquid three phase separator of embodiment 1;
Fig. 4 is the structural representation of the vertical liquid-liquid three phase separator of embodiment 2.
Symbol description
1 tangential entry; 2 cones; 3 pantographic liquid outlets; 4 umbrella liquid distributors; 5 gas vents;
11,21 inertial separation distributors; 12 cowling panels; 13,23 perforate ripple coalescing-plates;
14,24 hydrophily ripple coalescing-plates; 15 baffling demisters; 16,26 wire mesh demisters;
17, the coalescent layer of 25 fibers; 18,28 liquid level gauges; 19,27 interfacial meters; 22 rotating flows spray deaeration pipe.The specific embodiment
Below in conjunction with embodiment, further illustrate content of the present utility model, but these embodiment do not limit protection domain of the present utility model.
Embodiment 1
Cold low separation process in certain petrochemical industry hydrogenation plant adopts this technology, and as shown in Figure 1, the operating parameter of three-phase separating device is as shown in table 1 below for its three phase separation process chart:
Table 1
As shown in Figure 1, concrete implementation step: the oil content of moisture gassiness flows into from import with certain flow velocity, through inertial separation distributor, a large amount of gas is overflowed, and forms gas-liquid interface, and gas phase forms certain space, liquid phase, through distribution effect, prevents the fragmentation of dispersant liquid drop.During by cowling panel, liquid phase obtains the local acceleration of secondary, and water droplet collision is grown up, the coalescent effect of strengthening subsequent, and eliminated turbulent flow.During by perforate ripple coalescing-plate, utilize ripple coalescing-plate to comprise shallow pool principle and collision coalescence, water droplet is grown up and is sunk separated from tapping.Again through the coalescent corrugated plating of hydrophily, less water droplet is at hydrophilic material surface film coalescence, and is polymerized to drop, with gravity and liquid drag force of the flow transport.Rise to the gas of gas-phase space, by the droplet capture effect of baffling demister and wire mesh demister, the gas of purification enters gas bag, then at gas vent, discharges.Oil mixing with water liquid finally passes through the coalescent layer of fiber, and microvoid and the bigger serface of the coalescent layer of fiber are separated significant to becoming more meticulous of water droplet.Powerful collision coalescence effect makes small water droplet constantly collide and grow up, and is settled down to water bag, through water out, arranges outward.Oil phase liquid level in container is during higher than fibrage height, and oil phase flows into oil sump.By the height of oil-water interfaces, control the outer row of the water yield, by the discharge of liquid surface height controlling oil phase in oil sump.
As shown in Figure 2, liquid containing micro bubble enters rotating flow injection deaeration pipe 22 from tangential entry 1, under the effect of centrifugal force, bubble is the separated deaeration pipe center that moves to rapidly, from gas vent 5 overflows, go out, because of gas coalescent at center, therefore be provided with cone 2 and prevent that gas from flowing to lower liquid outlet and reducing liquid removal rate from center, the micro-negative pressure secondary that adopts pantographic liquid outlet 3 to utilize venturi to spray flash principle formation carries out part by dissolved gases in liquid and removes, this partially liq is injected on umbrella liquid distributor 4, form larger liquid film, be conducive to removing of gas, greatly improved separative efficiency and widened application.This process is general to degassed requirement, and emphasis is oil water separation process, so select to adopt horizontal type gas and liquid liquid three phase separator to carry out separation.
The structure of the horizontal type gas and liquid liquid three phase separator that the present embodiment is used as shown in Figure 3, comprises shell and internals, and shell is provided with charging aperture, Shui Bao, water out, gas bag, gas vent 5, oil sump, oil export, liquid level gauge 18 and interfacial meter 19; Internal part comprises inertial separation distributor 11, cowling panel 12, perforate ripple coalescing-plate 13, hydrophily ripple coalescing-plate 14, baffling demister 15, wire mesh demister 16, the coalescent layer 17 of fiber.In Fig. 3, solution-air-liquid three-phase medium enters three phase separator from tangential entry 1, first by the inertial separation distributor 11 being connected with tangential entry 1, carry out the distribution of preliminary separated and liquid, gas is to the upper space of container (three phase separator), all the other two-phase liquid are carrying out fluid rectification by cowling panel 12, making liquid become stable laminar condition enters perforate ripple coalescing section 13 and carries out the tentatively coalescent of profit two-phase, decentralized photo oil droplet or water droplet are grown up, and then enter hydrophily ripple coalescing-plate 14, utilize the projection of hydrophily ripple coalescing-plate 14 partly to make oil droplet floating upward quickly, recessed portion sinks water fast, realize the preliminary separated fast of profit two-phase, finally without the separated clean tiny oil droplets water droplet of ripple segregation section, enter again the coalescent layer 17 of fiber and carry out degree of depth coarse separation, in the coalescent layer 17 of fiber, utilize the special weaving manner of the hydrophilic or oleophylic of fiber to tackle small water droplet or oil droplet, the water after purification or oil are discharged from outlet, gas phase is discharged three phase separator by the gaseous phase outlet 5 from top after wire mesh demister 16 precipitation of liquid droplets.
The effect of three phase separation in the present embodiment: gas removal rate is more than 95% (to stablize), and W/O content is less than 35ppm.
Embodiment 2
Cold low separation process in certain petrochemical industry hydrogenation plant adopts this technology, and as shown in Figure 1, the operating parameter of three-phase separating device is as shown in table 2 below for its three phase separation handling process:
Table 2
This process is had relatively high expectations to degassed, need the gas of degree of depth reclaimer operation process, to oil water separation process, require also higher, so select to adopt vertical liquid-liquid three phase separator to carry out separation, its structure as shown in Figure 4, comprise shell and internals, shell is provided with charging aperture, water out, gas outlet, oil export, liquid level gauge 28, interfacial meter 29.Internals comprise that inertial separation distributor 21, rotating flow spray deaeration pipe 22, perforate ripple coalescing-plate 23, hydrophily ripple coalescing-plate 24, the coalescent layer 25 of fiber, wire mesh demister 26.
Specific implementation process: the oil content of moisture gassiness flows into from import with certain flow velocity, through inertial separation distributor, a large amount of gas is overflowed, and liquid phase, through distribution effect, prevents the fragmentation of dispersant liquid drop.Liquid sprays deaeration pipe through turn of tidal stream again, and to carry out the degree of depth degassed, and in liquid, gas is effectively separated, and gas is upwards discharged after the de-drop of wire mesh demister.Liquid during by perforate ripple coalescing-plate, utilizes ripple coalescing-plate to comprise shallow pool principle and collision coalescence, and water droplet is grown up and sunk from tapping separated.Again through the coalescent corrugated plating of hydrophily, less water droplet is at hydrophilic material surface film coalescence, and is polymerized to drop, with gravity and liquid drag force of the flow transport.Oil mixing with water liquid finally passes through the coalescent layer of fiber, and microvoid and the bigger serface of the coalescent layer of fiber are separated significant to becoming more meticulous of water droplet.Powerful collision coalescence effect makes small water droplet constantly collide and grow up, and sedimentation is arranged outward through water out.By the height of oil-water interfaces, control the outer row of the water yield, by gas-liquid interface height, control the discharge of oil phase.
The three phase separation effect of the present embodiment: gas removal rate is more than 99% (to stablize), outlet W/O content is less than 100ppm, and in water, oil content is less than 150ppm.
Claims (9)
1. a three-phase separating device, device is characterised in that, described device comprises shell and internals, according to the flow direction of three-phase, described shell is provided with charging aperture, liquid light phase export, gas bag, gaseous phase outlet, oil bag or water bag, liquid heavy out, liquid level gauge and interfacial meter, and described internals are provided with gas-liquid inertial separation distributor, rotating flow sprays the coalescent layer of the poly-fiber of deaeration pipe, baffling coalescing-plate, perforate ripple coalescing-plate, hydrophily corrugated plating, wire mesh demister and nanometer; Described gas-liquid inertial separation distributor is connected with described charging aperture, and described wire mesh demister is arranged in described gas bag; Described baffling coalescing-plate is arranged on gas-liquid interface place.
2. three-phase separating device according to claim 1, is characterized in that, described gas-liquid inertial separation distributor is positioned at the centre of liquid stream cross section, and its form is tube having holes or distribution of inertia arc shaped blade group.
3. three-phase separating device according to claim 2, it is characterized in that, described rotating flow sprays deaeration pipe and has one or more horizontal tangential inlets, on upper and lower top, be respectively equipped with gas vent and liquid outlet, the center of described liquid outlet is provided with cone, and described liquid outlet is shaped telescopic tube form, the outer setting of corresponding described liquid outlet has umbrella liquid distributor.
4. three-phase separating device according to claim 1, is characterized in that, described rotating flow sprays deaeration pipe for being installed in parallel.
5. three-phase separating device according to claim 1, is characterized in that, described baffling coalescing-plate adopts hydrophilic oleophobic or oleophilic drainage material.
6. three-phase separating device according to claim 1, it is characterized in that, the corrugated plating group that described perforate ripple coalescing-plate is placed for pressing certain angle, ripple direction is consistent with liquid flow path direction, at crest and trough place, respectively open circular hole, the diameter of described circular hole is 5～50mm, and pitch-row is 5～100mm, and corrugated plating spacing is 5～50mm.
7. three-phase separating device according to claim 1, is characterized in that, the coalescent layer of the poly-fiber of described nanometer is formed by organic fiber and inorfil braiding.
8. three-phase separating device according to claim 1, is characterized in that, the coalescent layer of the poly-fiber of described baffling coalescing-plate, perforate ripple coalescing-plate and nanometer adopts modular mode setting.
9. three-phase separating device according to claim 1, is characterized in that, described three-phase separating device is horizontal type gas and liquid liquid three phase separator or vertical liquid-liquid three phase separator.
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| CN201420151255.3U CN203763912U (en) | 2014-03-31 | 2014-03-31 | Three-phase separation device |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104771961A (en) * | 2015-03-26 | 2015-07-15 | 中国电力工程顾问集团中南电力设计院有限公司 | Horizontal impinging stream gas-water separator |
| WO2015149196A1 (en) * | 2014-03-31 | 2015-10-08 | 华东理工大学 | Combination method and apparatus applying to three-phase separation |
| EP3257565A4 (en) * | 2015-02-09 | 2018-03-14 | East China University Of Science And Technology | Method and apparatus for strengthening oil-water separation and coupled desalting functions in cold low pressure separator |
| CN107952259A (en) * | 2017-12-29 | 2018-04-24 | 上海协升化工科技有限公司 | A kind of high-efficiency blade formula feed distribution mechanism |
| CN109179930A (en) * | 2018-09-30 | 2019-01-11 | 华东理工大学 | A kind of method of high efficiente callback oily in oil, mud, water three phase separation and greasy filth in tank bottom oil sludge |
| CN109304061A (en) * | 2017-07-26 | 2019-02-05 | 中国石油化工股份有限公司 | A kind of oil and gas well testing open flow gas-liquid separator |
| CN110882560A (en) * | 2019-12-03 | 2020-03-17 | 东北石油大学 | Intermittent type formula hydrocyclone separation device |
| CN111085108A (en) * | 2018-10-23 | 2020-05-01 | 中国石化工程建设有限公司 | Gas-liquid separation assembly, alkali liquor regeneration tower and alkali liquor regeneration method |
| CN114058398A (en) * | 2020-08-07 | 2022-02-18 | 国家能源投资集团有限责任公司 | Online split-phase collection device and method for Fischer-Tropsch reaction products |
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2014
- 2014-03-31 CN CN201420151255.3U patent/CN203763912U/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015149196A1 (en) * | 2014-03-31 | 2015-10-08 | 华东理工大学 | Combination method and apparatus applying to three-phase separation |
| EP3257565A4 (en) * | 2015-02-09 | 2018-03-14 | East China University Of Science And Technology | Method and apparatus for strengthening oil-water separation and coupled desalting functions in cold low pressure separator |
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