CN203360386U - Device for improving hydrogen utilization rate of hydrogenation equipment - Google Patents
Device for improving hydrogen utilization rate of hydrogenation equipment Download PDFInfo
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- CN203360386U CN203360386U CN2013203465232U CN201320346523U CN203360386U CN 203360386 U CN203360386 U CN 203360386U CN 2013203465232 U CN2013203465232 U CN 2013203465232U CN 201320346523 U CN201320346523 U CN 201320346523U CN 203360386 U CN203360386 U CN 203360386U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02E60/30—Hydrogen technology
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Abstract
The utility model relates to a device for improving hydrogen utilization rate in the process of thermal high separation. After hydrogenation is performed, preliminary gas-liquid separation is firstly performed on distillate oil, gaseous products and hydrogen by an inertia separation distributor arranged at the inlet of a thermal high-pressure separator at high pressure so as to enable a gas phase enters into a subsequent system; a liquid phase enters into a thermal low-pressure separator, and is separated preliminarily by adopting an ejection flash evaporation technology inside the thermal low-pressure separator at the first step so as to release partial low separation gas (hydrogen mainly), and then is separated into gas phase and liquid phase under the effect of the gravity settling; the hydrogen and partial tiny bubbles dissolved into thermal low separation oil under the pressure are separated by a centrifugal degassing method at the second step; hydrocyclone separation or coalescence separation is performed on the liquid phase part so as to remove drops carried completely, then the gas phase is discharged out of the device, and the distillate oil enters into a subsequent facility. The device for improving hydrogen utilization rate of the hydrogenation equipment improves the recovery rate of hydrogen contained in the distillate oil of hydrogenation equipment after hydrogenation, and can be suitable for other processes for recovering hydrogen.
Description
Technical field
The utility model relates to the refining hydrocarbon ils of hydrogen field, relates in particular to a kind of device that utilizes the inertial separation distribution technique, sprays flash distillation and centrifugal degassed combination technique raising hydrogenation unit hydrogen utilization ratio.
Background technology
Along with the worsening shortages of crude resources and heaviness, in poor quality development, distillate hydrogenation technique is applied widely in Clean Fuel Production.In addition, in current shale gas, Sweet natural gas and Coal Chemical Industry, also extensively adopt distillate hydrogenation technique, to obtain clean fuel.
Tradition hydrocarbon oil hydrogenation process reaction system needs a large amount of hydrogen to guarantee certain hydrogen dividing potential drop, and wherein small portion hydrogen falls by the hydrogenation consumption of chemical reaction, and major part recycles after being boosted by circulating hydrogen compressor.The separation process of the mesohigh hydrogenation technique reaction product such as conventional residual hydrogenation, hydrocracking, hydrotreatment, hydro-upgrading, hydrofining has cold high score flow process and hot high score flow process usually.Usually the flow process that the total overall reaction product separates through the laggard promoting the circulation of qi liquid of air cooler is called cold high score flow process; And the total overall reaction product first carries out a gas-liquid separation at certain temperature, the oil gas flashed off carries out the flow process of secondary separation again after heat exchange and air cooling, is called hot high score flow process.Cold high score and hot high score flow process have been widely used in domestic and international hydrogenation unit.The key problem of the selection of cold high score and hot high score flow process is how two kinds of flow processs to be carried out to economy relatively.The advantage of hot high score flow process is: reduce plant energy consumption, reduce the cold area that changes; Can reduce the congeal generation of phenomenon of air cooler for extremely frigid zones; For the recycle to extinction flow process, be conducive to prevent the accumulation of condensed-nuclei aromatics and stop up high-pressure air cooler.But its shortcoming is: increase the high-temperature oil gas separation system, and hydrogen loss is larger, the concentration of recycle hydrogen, also a little less than cold high score flow process, causes the pressure of whole reactive system slightly to increase.The precondition that adopts hot high score flow process is exactly that the hydrogen contained in low minute gas must be reclaimed effectively, is dissolved in cold hanging down and divides oil and heat to hang down the part that the hydrogen divided in oil is commonly referred to be hydrogen loss.
In current hot high score flow process, hydrogen and hydrogenation after cut oil the high pressure hot separator specified temp with carry out liquid phase under pressure and separate, this separates and adopts gravity settling separation; The high pressure hot separator gas phase is through the circulating hydrogen compressor Returning reacting system that boosts, the high pressure hot separator liquid phase discharges low minute gas after vacuum flashing under thermal low-pressure separators specified temp and pressure, hydrogen richness in low minute gas generally is about 70%, by after gravity settling separation, generally using this part low minute gas as hydrogen-rich gas, delivering to the PSA device, reclaims hydrogen wherein.General mesohigh hydrogenation unit thermal low-pressure separators pressure design is at 1.2～3.0MPa(G), to guarantee that an isolated low minute oily depended on pressure enters into separation column, enter hydrogen that separation column separates because of content low can not the recovery usually used as fuel gas use, the utilising efficiency of hydrogen is lower.
Because high pressure hot separator, thermal low-pressure separators gas-liquid two-phase in current heat from hydrogenation high score flow process all adopt the gravity settling of nature usually, as shown in Figure 1, therefore inevitably portion gas (being mainly hydrogen) is present in liquid phase with micro-bubble, be sent to follow up device thereupon, caused the loss of hydrogen partial; In addition, thermal low-pressure separators adopts traditional flash distillation-gravity settling separation method, because the less flash efficiency that causes of liquid gas phase surface in contact under certain operational condition of the residence time is low, has caused the hydrogen partial loss; Finally because of the thermal low-pressure separators pressure design at 1.2～3.0MPa(G), also can dissolve hydrogen partial in depressing liquid phase in this minute, also caused the loss of hydrogen partial.Therefore need to adopt more efficient method to be recycled this hydrogen partial, this operation efficient, economic to enterprise will bring benefit.
The utility model content
In order to overcome above-mentioned the deficiencies in the prior art, the utility model provides a kind of method and device that improves hydrogen utilization ratio in heat from hydrogenation high score flow process.
Hydrogenation after cut oil, gaseous product and hydrogen at first under high pressure carry out preliminary gas-liquid separation by the inertial separation sparger of high pressure hot separator import setting; strengthening gas delivery efficiency, gas phase through cold anticyclone and follow-up facility by the circulating hydrogen compressor Returning reacting system; The liquid phase the first step is carried out initial gross separation through the injection flash evaporation technology and is discharged the low minute gas (being mainly hydrogen) of a part, and isolated gas phase relies on the gravity settling method to be divided into gas phase and liquid phase; Still being dissolved in the gas of distillate and the part micro-bubble centrifugal degas method by second step under this pressure is separated, rely on pressure gradient (radial section from pressure reduce gradually) outside to inside and the centrifugal field of centrifugal degassing equipment, be dissolved in the gas of distillate because the reduction of pressure gradient field dividing potential drop is separated out, this part bubbing and micro-bubble are further separated under centrifugal field; The gas phase part goes out device after removing totally by cyclonic separation or coarse separation by the drop carried, and distillate removes follow-up facility.The method device has made up the deficiencies in the prior art, has improved the recovery utilization rate of hydrogen.
Concrete technical scheme is:
A kind of device that improves hydrogen utilization ratio in heat from hydrogenation high score flow process, comprise that a high pressure hot separator and that is provided with entrance, liquid-phase outlet and gaseous phase outlet is provided with the thermal low-pressure separators of entrance, liquid-phase outlet and gaseous phase outlet, the liquid-phase outlet of this high pressure hot separator is connected with the entrance of thermal low-pressure separators
This thermal low-pressure separators ingress is provided with an injection flash separator, and this injection flash separator comprises at least one injection flash distillation core pipe;
This thermal low-pressure separators is provided with at least one centrifugal degassed core pipe before liquid-phase outlet, this centrifugal degassed core pipe comprises 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.
Further, this high pressure hot separator can be for vertical or horizontal, be provided with at least one inertial separation sparger in ingress, this inertial separation sparger comprises a plurality of inertial separation distribution blades, upper cover plate and the lower cover that is arranged at both sides, this inertia guide vane comprises that water conservancy diversion straight-line segment, blade rotating angle semicircle and distribution straight-line segment form, and the water conservancy diversion straight-line segment is nearly casing one end;
Further, the upper cover plate of described inertial separation sparger or lower cover employing are from the charging medullary ray to the edge tilt set-up mode, and angle of inclination is 3～60 degree.
Further, described high pressure hot separator gaseous phase outlet is or/and thermal low-pressure separators gaseous phase outlet place is provided with a gas-liquid separator.
Further, described gas-liquid separator is gas-liquid eddy flow or coalescing separator.
Further, described thermal low-pressure separators comprises a plurality of injection flash distillation core pipes, the parallel connection of the plurality of injection flash distillation core pipe, and in the uniform setting of thermal low-pressure separators radial section, thermal low-pressure separators can be horizontal or vertical.
Further, described injection flash separator exit arranges corresponding umbrella liquid distributor, and the 1-30 that umbrella liquid distributor surface-area is injection flash distillation core pipe outlet area doubly.
Further, described thermal low-pressure separators comprises a plurality of described centrifugal degassed core pipes, and the plurality of centrifugal degassed core pipe is in parallel and in the uniform setting of thermal low-pressure separators radial section.
Further, described thermal low-pressure separators also comprises that one is divided into the division plate of two chambers by thermal low-pressure separators, this division plate arranges highly and arranges highly and adapt with described centrifugal degassed core pipe, with the import by centrifugal degassed core pipe and liquid-phase outlet, separates and is placed in aforementioned two chambers.
The high pressure hot separator entrance arranges distillate and the hydrogen mixture of inertial separation sparger after to hydrotreatment and carries out initial gross separation, and the pressure drop of inertial separation sparger is 0.0001～0.01MPa; Secondly carry out secondary separation by gravity settling, the gas phase after separation is removed follow up device through eddy flow or coarse separation, the liquid phase light pressure separator that reduces phlegm and internal heat, and in high pressure hot separator, working pressure is 2-30MPa, service temperature is 200-270 ℃; At first the distillate that enters thermal low-pressure separators is separated the gas phase of dissolving in distillate by spraying flash evaporation technology, and the pressure drop of this process is not more than 0.01MPa; Secondly the gas-liquid two-phase by gravity settling, flash separation gone out is separated, it is degassed that isolated liquid phase adopts centrifugal degassing method to rely on eddy flow or centrifugal pressure gradient field to carry out secondary to distillate, this pressure gradient field internal pressure differences is 0.01～10MPa, isolated gas phase goes out thermal low-pressure separators from top after eddy flow or coarse separation, isolated liquid phase goes out thermal low-pressure separators from bottom, the working pressure of thermal low-pressure separators is 0.6-5MPa, and service temperature is 170-240 ℃;
The beneficial effects of the utility model are: the method strengthening gas-liquid separation that at first the utility model adopts inertial separation to distribute, the Hydrogen Separation efficiency of raising high pressure hot separator, secondly adopt and spray flash distillation, the uniform technology of liquid umbrella improves distillate flash liberation efficiency, at first distillate being carried to the solution gas that gas and pressure drop discharge under the gravity field effect is separated, to under this thermal low-pressure separators working pressure dissolved gases by flash evaporation can't effectively remove thereafter, the micro-bubble disperseed in the distillate that flash separation is gone out also can't effectively be removed and utilize centrifugal degas method to carry out secondary separation by gravity settling, the gas dissolved depressed of this minute pressure gradient field that relies on centrifugate gas to separate (radial section from pressure reduce gradually) is outside to inside separated, the micro-bubble of carrying secretly in distillate relies on centrifugal field effectively to remove.
In method described in the utility model, as through thermal low-pressure separators, distillate out also needs to carry out the words of flash distillation recover hydrogen, can directly adopt centrifugal degas method to carry gas to distillate and solution gas is separated, can further effectively reduce like this energy consumption of repressurize after the liquid phase step-down.
That the equipment that the utility model adopts has is simple to operate, floor space is little, the degassing efficiency advantages of higher, has overcome the large problem of current hot high score flow process hydrogen loss, can be widely used in the distillate hydrogenation treating processes.
The accompanying drawing explanation
Fig. 1-1 is existing process flow diagram.
Fig. 1-2 is the existing apparatus schematic flow sheet.
Fig. 2 is the utility model process flow diagram.
Fig. 3 is the utility model the first embodiment device schematic flow sheet.
Fig. 4 is the utility model the second embodiment device schematic flow sheet.
Fig. 5-1 is high pressure hot separator entrance inertial separation sparger vertical view.
Fig. 5-2 are high pressure hot separator entrance inertial separation sparger left view.
Fig. 6-1 is centrifugal degassed core tubular construction schematic diagram.
Fig. 6-2 are the radial pressure schematic diagram of centrifugal degassed core pipe along the sectional view of A-A hatching line.
Fig. 6-3 are that centrifugal degassed core caliber is to cross section pressure gradient distributed simulation figure.
Fig. 7 is centrifugal degassed core tubular construction detail view.
Nomenclature:
1 is high pressure hot separator; 1-1 is the thermal high entrance; 1-2 is the inertial separation sparger; 1-3 is the thermal high gaseous phase outlet; 1-4 is the liquid/gas separator of working off one's feeling vent one's spleen; 1-5 thermal high liquid-phase outlet; 2 is thermal low-pressure separators; 2-1 is for spraying flash separator; 2-1-1 is for spraying flash distillation core pipe; 2-2 is the umbrella liquid distributor; 2-3 is centrifugal degassing equipment; 2-3-1 is centrifugal degassed core pipe; 2-4 is division plate; 2-5 is gas-liquid separator; 2-6 is the thermal low gaseous phase outlet; 2-7 is the thermal low entrance; 2-8 is the thermal low liquid-phase outlet; 1-1-1 is the thermal high inlet duct; 1-2-1 is inertial separation distribution blade; 1-2-2 is upper cover plate; 1-2-3 is lower cover; 3 is the second thermal low-pressure separators.
2-3-1-1-1 is the import of liquid gas axial-flow type; 2-3-1-1-2 is that the liquid autogenous cutting is to import; 2-3-1-2 is the post chamber; 2-3-1-3 is the cone chamber; 2-3-1-4 is centrifugal degassed core pipe liquid-phase outlet; The 2-3-1-5 inner cone; 2-3-1-6 is upflow tube back taper heavy wall; 2-3-1-7 is two not good liquor outlets; 2-3-1-8 is the ring groove gap, and 2-3-1-9 is for spraying the secondary separation upflow tube, and 2-3-1-9-1 is hydraucone, and 2-3-1-9-2 is the first overflow tubing string chamber, and 2-3-1-9-3 is the back taper connection chamber, and 2-3-1-9-4 is the second overflow tubing string chamber, and 2-3-1-9-5 is cylindrical shell.
Embodiment
The utility model improves the device of hydrogenation unit hydrogen recovery, comprise that a high pressure hot separator and that is provided with entrance, liquid-phase outlet and gaseous phase outlet is provided with the thermal low-pressure separators of entrance, liquid-phase outlet and gaseous phase outlet, the liquid-phase outlet of this high pressure hot separator is connected with the entrance of thermal low-pressure separators, this thermal low-pressure separators ingress is provided with an injection flash separator, and this injection flash separator comprises at least one injection flash distillation core pipe; This thermal low-pressure separators is provided with at least one centrifugal degassed core pipe before being arranged at liquid-phase outlet, this centrifugal degassed core pipe comprises 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.
The technical process of the utility model raising hydrogenation unit hydrogen recovery is as follows: at first hydrogenation after cut oil, gaseous product and hydrogen adopt the inertial separation sparger of high pressure hot separator entrance setting to carry out initial gross separation, and the pressure drop of inertial separation sparger is 0.0001～0.01MPa; Secondly carry out secondary separation by gravity settling, after inertial separation sparger and cavity in high pressure hot separator are settlement separate, gas phase (recycle hydrogen and part benzoline) is removed follow up device, and liquid phase (distillate and solution gas) enters thermal low-pressure separators; At first the distillate that enters thermal low-pressure separators is separated the gas phase of dissolving in distillate by spraying flash evaporation technology, and the pressure drop of this process is not more than 0.01MPa; Secondly the gas-liquid two-phase by gravity settling, flash separation gone out is separated, it is degassed that isolated liquid phase adopts centrifugal degassing method to rely on eddy flow or centrifugal pressure gradient field to carry out secondary to distillate, this pressure gradient field internal pressure differences is 0.01～10MPa, after spraying the flasher flash separation, gas phase (low minute gas, be mainly hydrogen) go PSA to reclaim, liquid phase and solution gas and the micro-bubble carried go centrifugal deaerator to carry out the degassed separation of secondary, liquid (distillate) goes out equipment from bottom afterwards, and isolated gas phase goes PSA to reclaim from the upper gaseous phase outlet.
Enforcement by this utility model, can significantly overcome the inefficient problem of gravity settling separation of high pressure hot separator, thermal low-pressure separators gas-liquid two-phase nature in current heat from hydrogenation high score flow process, solving portion gas (being mainly hydrogen) is present in liquid phase with micro-bubble, be sent to follow up device, the loss of the hydrogen partial caused thereupon; In addition, overcome current thermal low-pressure separators and adopted traditional flash distillation-gravity settling separation method, because the less flash efficiency that causes of liquid gas phase surface in contact under certain operational condition of the residence time is low, caused the problem of hydrogen partial loss; Finally overcome the thermal low-pressure separators pressure design at 1.2～3.0MPa(G) time dissolve hydrogen partial in liquid phase, cause the problem of hydrogen partial loss.The enforcement of this utility model has improved the recovery utilization rate of hydrogen, to efficient, the economical operation of enterprise's production equipment, will bring benefit.
embodiment 1:
Certain petrochemical industry hydrogenation unit adopts hot high score flow process, and high pressure hot separator charging parameter is as follows:
| Title | ? | Unit |
| Name of material: | Hydrogen, oil gas, oil, H 2S、NH3 | ? |
| Total flux | 433290 | kg/h |
| Gas phase | 81520 | kg/h |
| Oil phase | 351770 | kg/h |
| Water | ? | kg/h |
| Service temperature-the highest/normal/minimum | /210/ | ℃ |
| Working pressure-the highest/normal/minimum | 8.4/8.3/ | MPa(g) |
| Vacuum or negative pressure-the highest/minimum | Vacuum | MPa(abs) |
| Under Media density-service temperature | ? | ? |
| Gas phase | 18.3969 | kg/m 3 |
| Oil phase | 733.4492 | kg/m 3 |
Annotate: the operation initial stage: in gas phase, H2 concentration is 73.8946% (v), and H2S concentration is 1.8413% (v), and in liquid phase, H2S concentration is 0.177% (wt); Operate latter stage: in gas phase, H2 concentration is 73.7534% (v), and H2S concentration is 1.3705% (v), and in liquid phase, H2S concentration is 0.132% (wt).
Refer to Fig. 1-1-Fig. 1-2, existing heat from hydrogenation high pressure separation process is realized by following steps, at first hydrogenation after cut oil, gaseous product and hydrogen enter high pressure hot separator 1 and carry out gas-liquid separation under certain temperature and pressures, separate the gravity settling mode that adopts, isolated gas phase is removed follow up device, liquid phase enters thermal low-pressure separators 2 and carries out flash distillation, the gas-liquid two-phase flashed off separates by the gravity settling mode again, isolated gas phase (low minute gas) goes PSA to carry out hydrogen recovery, and liquid phase is removed follow-up desulfurization and fractionation plant.In current sepn process, gas-liquid two-phase all adopts the gravity settling of nature usually, and therefore inevitably portion gas (being mainly hydrogen) is present in liquid phase with micro-bubble, is sent to follow up device thereupon, has caused the loss of hydrogen partial; In addition, thermal low-pressure separators adopts traditional flash distillation-gravity settling separation method, because the less flash efficiency that causes of liquid gas phase surface in contact under certain operational condition of the residence time is low, has caused the hydrogen partial loss; Finally because of the thermal low-pressure separators pressure design at 1.2～3.0MPa(G), also can dissolve hydrogen partial in depressing liquid phase in this minute, also caused the loss of hydrogen partial.Therefore need to adopt more efficient method to be recycled this hydrogen partial, this operation efficient, economic to enterprise will bring benefit.
Compare existing technical process and device, the present embodiment has further adopted the method and apparatus of aforementioned utility model.Refer to Fig. 1～Fig. 2, for the utility model the first embodiment device and schematic flow sheet thereof, this device comprises that one is provided with entrance 1-1, the high pressure hot separator 1 and one of liquid phase 1-5 outlet and gaseous phase outlet 1-3 is provided with entrance 2-7, the thermal low-pressure separators 2 of liquid-phase outlet 2-8 and gaseous phase outlet 2-6, the liquid-phase outlet 1-5 of this high pressure hot separator 1 is connected with the entrance 2-7 of thermal low-pressure separators, this thermal low-pressure separators entrance 2-7 place is provided with an injection flash separator 2-1, this injection flash separator 2-1 comprises a plurality of injection flash distillation core pipe 2-1-1, the plurality of injection flash distillation core pipe 2-1-1 is in parallel and in the uniform installation of thermal low-pressure separators 2 radial section, can increase 1-20 doubly by this injection flash distillation core pipe flow rate of liquid., each sprays flash distillation core pipe 2-1-1 jet orifice place and is equipped with corresponding umbrella liquid distributor 2-2, and the 1-30 that umbrella liquid distributor 2-2 surface-area is injection flash distillation core pipe outlet area is doubly.This thermal low-pressure separators 2 is provided with a plurality of centrifugal degassed core pipe 2-3 before liquid-phase outlet, and the plurality of centrifugal degassed core pipe 2-3 is in parallel and in the uniform setting of thermal low-pressure separators radial section.High pressure hot separator 1 gaseous phase outlet place is provided with a gas-liquid separator 1-4, and thermal low-pressure separators 2 gaseous phase outlet places are provided with a gas-liquid separator 2-5, and this gas-liquid separator 1-4,2-5 are gas-liquid eddy flow or coalescing separator.Thermal low-pressure separators 2 also comprises that one is divided into the division plate 2-4 of two chambers by thermal low-pressure separators 2, this division plate 2-4 arranges highly and arranges highly and adapt with described centrifugal degassed core pipe 2-3, with the import by centrifugal degassed core pipe 2-3 and liquid-phase outlet, separates and is placed in aforementioned two chambers.
At first hydrogenation after cut oil, gaseous product and hydrogen adopt the inertial separation sparger of high pressure hot separator entrance setting to carry out initial gross separation, and the working pressure of high pressure hot separator is 8.3MPa(G), the pressure drop of inertial separation sparger is 0.0004MPa; Secondly carry out secondary separation by gravity settling, the gas phase after separation is removed follow up device through cyclonic separation, and the pressure drop of this process is 0.005MPa, the liquid phase light pressure separator that reduces phlegm and internal heat; At first the distillate that enters thermal low-pressure separators carries out flash separation by spraying flash evaporation technology to the gas phase of dissolving in distillate, and the pressure drop of this process is 0.001MPa, and in thermal low-pressure separators, working pressure is 2.9MPa(G); Secondly the gas-liquid two-phase by gravity settling, flash separation gone out is separated, it is degassed that isolated liquid phase adopts centrifugal degassing method to rely on eddy flow or centrifugal pressure gradient field to carry out secondary to distillate, from outer wall, the pressure difference to center is 1.2MPa to this pressure gradient field internal pressure, isolated gas phase goes out thermal low-pressure separators after cyclonic separation from top, isolated liquid phase goes out thermal low-pressure separators from bottom.Wherein, the service temperature of high pressure hot separator is 225-235 ℃, and the thermal low-pressure separators service temperature is 205-215 ℃.
Implementation result: (be that in high pressure hot separator, gas-liquid adopts gravity settling to be separated with former technical process, in thermal low-pressure separators at first by flash distillation by thermal high in liquid phase out contained gas phase separated, secondly carry out the gas-liquid two-phase separation by gravity settling) compare, there is following beneficial effect:
1, in high pressure hot separator by interior posting port inertial separation sparger, the gas-liquid two-phase separating effect is better, the heavy hydrocarbon component that part was difficult to separate has in the past obtained separation, has improved the efficiency of high pressure hot separator;
2, spray flash separator by interior posting port in thermal low-pressure separators, strengthened the flash separation effect, improved the rate of recovery of hydrogen;
3, improved hydrogen recovery rate by centrifugal Degassing Technology before the thermal low-pressure separators liquid-phase outlet.
embodiment 2:
Referring to Fig. 4, is the second embodiment of the present utility model.Different from the first embodiment is the present embodiment at the gaseous phase outlet 2-6 place of thermal low-pressure separators 2 by interchanger same structure second thermal low-pressure separators 3 of further having connected, after in thermal low, separating 2 gaseous phase outlets, low minute gas has been carried out to heat exchange, the part hydrocarbon becomes liquid phase, then in 3 pairs of low minute gas of logical the second thermal low-pressure separators, institute's hydrogen is further purified.With embodiment 1, compare, this flow process is further purified to hydrogen, more is conducive to the recycling of hydrogen.
Centrifugal degassed core pipe in above-described embodiment, comprise and be provided with a cavity, this cavity is provided with the import of liquid gas, gaseous phase outlet and liquid-phase outlet, and 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 gaseous phase outlet end, the gaseous phase outlet least significant end that the is positioned at cavity degree of depth to the cavity upper surface.Its principle refers to Fig. 6-1～Fig. 6-3, this patent utility model person studies discovery by experiment, 0.5～3 times of position that is post chamber diameter at post chamber height, in swirler radially cross section have significant pressure gradient, i.e. radial position pressure from outside to inside reduces gradually.According to Henry's law, near this cross-sectional height, swirler outside wall liquid pressure is high, center pressure is low, the outside wall is depressed gas dissolved in this minute and be can migrate to central position, the overflow gaseous phase outlet is located to this position can further be removed dissolved gases in liquid under certain intake pressure, utilize centrifugal field to remove entrained liquids current eddy flow Degassing Technology 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.
Specific implementation can be as following example, refer to Fig. 7, comprise that the cone chamber 2-3-1-3(that is located at bottom also can be the post chamber), be located on the cone chamber, identical and the post chamber 2-3-1-2 that is communicated with it of maximum diameter, this cone chamber 2-3-1-3 and post chamber 2-3-1-2 form a closed cavity, the closed cavity bottom is provided with a liquid-phase outlet 2-3-1-4, 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 specifically sprays secondary separation upflow tube 2-3-1-9 by one to be realized, as shown in the figure, this injection secondary separation upflow tube 2-3-1-9 is arranged on the 2-3-1-2 central shaft of post chamber, comprise a hydraucone 2-3-1-9-1, the first overflow tubing string chamber 2-3-1-9-2 and a back taper connection chamber 2-3-1-9-3, with the second overflow tubing string chamber 2-3-1-9-4, 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 second overflow tubing string chamber 2-3-1-9-4 week side offers annular space fluting 2-3-1-8, annular space fluting 2-3-1-8 is provided with a cylindrical shell 2-3-1-9-5 outward and surrounds described upflow tube to form the cavity of a sealing, this cylindrical shell 2-3-1-9-5 bottom offers two not good liquor outlet 2-3-1-7, in the second overflow tubing string chamber 2-3-1-9-4, in order to utilize gas rotating centrifugal force that the liquid of gas entrainment is carried out to 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 the first overflow tubing string chamber 2-3-1-9-2 also is provided with a hydraucone 2-3-1-9-1, with large as far as possible catching, overflows gas.This hydraucone 2-3-1-9-1 week side is provided with a upflow tube back taper heavy wall 2-3-1-6, this upflow tube back taper heavy wall 2-3-1-6 is from this hydraucone 2-3-1-9-1 mono-until the upper surface of post chamber 2-3-1-2 carries out the separation of liquid gas so that the liquid gas that guiding enters from the liquid gas import that is arranged at cavity top or top enters the significant zone of pressure gradient as early as possible because space increases gradually.The import of above-mentioned liquid gas can adopt axial-flow type, tangential, spiral-line or involute urve form.2-3-1-2 bottom in this cone chamber is provided with an interior centrum 2-3-1-5, and this inner cone 2-3-1-5 base area is greater than the base area that gaseous phase outlet gos deep into cavity part end hydraucone 2-3-1-9-1, to reduce gas in outlet liquid, carries.
Inertial separation sparger in above-described embodiment, refer to Fig. 5-1～Fig. 5-2, comprise a plurality of inertial separation distribution blade 1-2-1 that are arranged at both sides, and be covered in the upper cover plate 1-2-2 on a plurality of inertial separation distribution blade 1-2-1, be arranged at the lower cover 1-2-3 under a plurality of inertial separation distribution blade 1-2-1, this inertia guide vane 1-2-1 is by the water conservancy diversion straight-line segment, blade rotating angle semicircle and distribution straight-line segment form, the water conservancy diversion straight-line segment is nearly casing one end, a plurality of inertial separation distribution blade 1-2-1 that are located at both sides are symmetrical for the cross-section center line of high pressure hot separator 1.A plurality of distribution of inertia blade 1-2-1 setting up and down has upper cover plate or lower cover, and this upper and lower cover plates adopts from center to the edge tilt set-up mode, and angle of inclination is 3～60 to spend.
Above-mentioned flash distillation is sprayed the core pipe and can be realized by injector, as venturi-type eductors.
Be only the preferred embodiment of utility model in sum, not be used for limiting practical range of the present utility model.Be that all equivalences of doing according to the content of the utility model claim change and modify, all should be technology category of the present utility model.
Claims (9)
1. a device that improves hydrogen utilization ratio in heat from hydrogenation high score flow process, comprise that a high pressure hot separator and that is provided with entrance, liquid-phase outlet and gaseous phase outlet is provided with the thermal low-pressure separators of entrance, liquid-phase outlet and gaseous phase outlet, the liquid-phase outlet of this high pressure hot separator is connected with the entrance of thermal low-pressure separators, it is characterized in that
This thermal low-pressure separators ingress is provided with an injection flash separator, and this injection flash separator comprises at least one injection flash distillation core pipe;
This thermal low-pressure separators is provided with at least one centrifugal degassed core pipe before liquid-phase outlet, this centrifugal degassed core pipe comprises 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.
2. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 1, it is characterized in that, this high pressure hot separator can be for vertical or horizontal, be provided with at least one inertial separation sparger in ingress, this inertial separation sparger comprises a plurality of inertial separation distribution blades, upper cover plate and the lower cover that is arranged at both sides, this inertial separation distribution blade comprises that water conservancy diversion straight-line segment, blade rotating angle semicircle and distribution straight-line segment form, and the water conservancy diversion straight-line segment is nearly casing one end;
3. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 2, is characterized in that, the upper cover plate of described inertial separation sparger or lower cover employing are from the charging medullary ray to the edge tilt set-up mode, and angle of inclination is 3～60 degree.
4. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 3, is characterized in that, described high pressure hot separator gaseous phase outlet is or/and thermal low-pressure separators gaseous phase outlet place is provided with a gas-liquid separator.
5. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 4, is characterized in that, described gas-liquid separator is gas-liquid eddy flow or coalescing separator.
6. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 1, it is characterized in that, described thermal low-pressure separators comprises a plurality of injection flash distillation core pipes, the parallel connection of the plurality of injection flash distillation core pipe, and, in the uniform setting of thermal low-pressure separators radial section, thermal low-pressure separators can be horizontal or vertical.
7. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 1, it is characterized in that, described injection flash separator exit arranges corresponding umbrella liquid distributor, and the 1-30 that umbrella liquid distributor surface-area is injection flash distillation core pipe outlet area doubly.
8. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 1, it is characterized in that, described thermal low-pressure separators comprises a plurality of described centrifugal degassed core pipes, and the plurality of centrifugal degassed core pipe is in parallel and in the uniform setting of thermal low-pressure separators radial section.
9. the device of hydrogen utilization ratio in raising heat from hydrogenation high score flow process as claimed in claim 1, it is characterized in that, described thermal low-pressure separators also comprises that one is divided into the division plate of two chambers by thermal low-pressure separators, this division plate arranges highly and arranges highly and adapt with described centrifugal degassed core pipe, with the import by centrifugal degassed core pipe and liquid-phase outlet, separates and is placed in aforementioned two chambers.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2013203465232U CN203360386U (en) | 2013-06-17 | 2013-06-17 | Device for improving hydrogen utilization rate of hydrogenation equipment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2013203465232U CN203360386U (en) | 2013-06-17 | 2013-06-17 | Device for improving hydrogen utilization rate of hydrogenation equipment |
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| CN203360386U true CN203360386U (en) | 2013-12-25 |
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| CN2013203465232U Expired - Fee Related CN203360386U (en) | 2013-06-17 | 2013-06-17 | Device for improving hydrogen utilization rate of hydrogenation equipment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103320161A (en) * | 2013-06-17 | 2013-09-25 | 华东理工大学 | Method and apparatus for improving hydrogen utilization rate of hydrogenation equipment |
| WO2014117633A1 (en) * | 2013-01-30 | 2014-08-07 | 华东理工大学 | Method and apparatus for improving hydrogen utilization rate of hydrogenation apparatus |
| CN110339786A (en) * | 2019-07-04 | 2019-10-18 | 华东理工大学 | It is a kind of to strengthen the slurry bed system liquid feedstock method and apparatus for adding hydrogen mass transfer |
| CN112852484A (en) * | 2021-01-05 | 2021-05-28 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
-
2013
- 2013-06-17 CN CN2013203465232U patent/CN203360386U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014117633A1 (en) * | 2013-01-30 | 2014-08-07 | 华东理工大学 | Method and apparatus for improving hydrogen utilization rate of hydrogenation apparatus |
| CN103320161A (en) * | 2013-06-17 | 2013-09-25 | 华东理工大学 | Method and apparatus for improving hydrogen utilization rate of hydrogenation equipment |
| CN103320161B (en) * | 2013-06-17 | 2015-04-15 | 华东理工大学 | Method and apparatus for improving hydrogen utilization rate of hydrogenation equipment |
| CN110339786A (en) * | 2019-07-04 | 2019-10-18 | 华东理工大学 | It is a kind of to strengthen the slurry bed system liquid feedstock method and apparatus for adding hydrogen mass transfer |
| CN112852484A (en) * | 2021-01-05 | 2021-05-28 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
| CN112852484B (en) * | 2021-01-05 | 2023-03-31 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
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