CN215560076U - Device for improving diesel oil quality - Google Patents
Device for improving diesel oil quality Download PDFInfo
- Publication number
- CN215560076U CN215560076U CN202120615986.9U CN202120615986U CN215560076U CN 215560076 U CN215560076 U CN 215560076U CN 202120615986 U CN202120615986 U CN 202120615986U CN 215560076 U CN215560076 U CN 215560076U
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- micro
- reactor
- interface unit
- fractionating tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002283 diesel fuel Substances 0.000 title claims abstract description 22
- 239000001257 hydrogen Substances 0.000 claims abstract description 86
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 86
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 79
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 239000007789 gas Substances 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000002994 raw material Substances 0.000 claims abstract description 13
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 9
- 238000010992 reflux Methods 0.000 claims abstract description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 3
- 238000005984 hydrogenation reaction Methods 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000004939 coking Methods 0.000 claims description 4
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000006185 dispersion Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 239000003921 oil Substances 0.000 description 31
- 239000010724 circulating oil Substances 0.000 description 9
- 239000012071 phase Substances 0.000 description 9
- 238000012546 transfer Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000002845 discoloration Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a device for improving the quality of diesel oil, which comprises a hydrofining reactor and a hydrofining reactor, wherein a first external micro-interface unit and a second external micro-interface unit are arranged outside the hydrofining reactor and are used for dispersing and crushing hydrogen into micro bubbles; the hydro-upgrading reactor is connected with a high-pressure separation tank for separating a reaction material from the bottom into a gas phase containing hydrogen sulfide and hydrogen, the bottom of the high-pressure separation tank is connected with a fractionating tower for purifying desulfurized diesel oil from which the gas phase is separated, a part of gas is extracted from a material from the top of the fractionating tower to a reflux tank at the top of the tower, a part of gas is returned to the fractionating tower, naphtha is extracted from the side line of the fractionating tower, and high-quality diesel oil is separated from the bottom of the fractionating tower. The utility model reduces the reaction pressure, the reaction temperature and the consumption of the circulating hydrogen, improves the utilization rate of the raw materials and the hydrogen, improves the product quality and the yield and saves the cost.
Description
Technical Field
The utility model relates to the field of diesel hydrogenation, in particular to a device for improving the quality of diesel.
Background
Diesel oil is a product obtained by atmospheric fractionation of petroleum. If the diesel oil is directly refined from petroleum, the content of sulfur, nitrogen and oxygen in the diesel oil is higher, and the content of olefin is also higher. The high content of olefin in the product is easy to cause discoloration, and can also influence the service life of motor vehicles and cause relatively large atmospheric pollution.
With the increasing awareness of environmental protection and stricter environmental regulations, the production and use of clean vehicle fuels become a trend, and the development of deep hydrodesulfurization technology for diesel oil becomes a hot spot of current research. At present, most diesel oil hydrofining devices exchange heat between raw oil and refined diesel oil and reaction products, heat the raw oil to the reaction required temperature through a heating furnace, and then hydrogenate the raw oil.
In view of the above, the present invention is particularly proposed.
SUMMERY OF THE UTILITY MODEL
The first purpose of the utility model is to provide a device for improving the quality of diesel oil, which reduces the reaction pressure, the reaction temperature and the consumption of circulating hydrogen, improves the utilization rate of raw materials and hydrogen, improves the product quality and yield and saves the cost by arranging a first external micro-interface unit and a second external micro-interface unit outside a hydrofining reactor.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
the utility model provides a device for improving the quality of diesel oil, which comprises a hydrofining reactor and a hydrofining reactor, wherein a first external micro-interface unit and a second external micro-interface unit are arranged outside the hydrofining reactor and are used for dispersing and crushing hydrogen into micro bubbles;
a heater is arranged between the hydrorefining reactor and the hydroupgrading reactor and used for heating reaction materials coming out of the bottom of the hydrorefining reactor and returning the reaction materials to the hydroupgrading reactor;
a modified micro-interface generator is arranged in the hydrogenation modified reactor and is used for crushing and dispersing hydrogen from the second external micro-interface unit;
the hydro-upgrading reactor is connected with a high-pressure separation tank and used for separating a reaction material from the bottom into a gas phase containing hydrogen sulfide and hydrogen, the bottom of the high-pressure separation tank is connected with a fractionating tower and used for purifying desulfurized diesel oil after the gas phase is separated, a part of gas is extracted from a material from the top of the fractionating tower to a reflux tank at the top of the tower, a part of gas is returned to the fractionating tower, naphtha is extracted from the side line of the fractionating tower, and high-quality diesel oil is separated from the bottom of the fractionating tower.
In the prior art, the diesel hydrogenation process has high energy consumption, large consumption of circulating hydrogen, high pressure and temperature of a hydrogenation reactor and lower productivity.
The device for improving the quality of the diesel oil is provided with the micro-interface generator in the hydrofining reactor to break and disperse the hydrogen into hydrogen micro-bubbles, so that the mass transfer area of the phase boundary of the hydrogen and the raw oil is increased. Because the density of hydrogen is small and the density of raw oil is large, the micro-interface generator is arranged at the bottom of the hydrofining reactor, and the hydrogen coming out from the bottom is mixed with the raw oil from bottom to top, so that the mixing time of the hydrogen and the raw oil is prolonged. In order to better disperse hydrogen, a discharge hole of the micro-interface generator is connected with a catalyst bed layer, a shunt pipe is arranged on the catalyst bed layer, and raw materials and hydrogen microbubbles from the micro-interface generator are uniformly dispersed into the hydrofining reactor. The device for improving the quality of the diesel oil is also provided with a hydro-upgrading reactor, wherein the hydro-upgrading reactor is internally provided with an upgrading micro-interface generator, and the upgrading micro-interface generator is arranged in the middle of the hydro-upgrading reactor and is used for crushing and dispersing hydrogen into hydrogen micro-bubbles, so that the phase boundary mass transfer area of the hydrogen and the raw oil is increased. Meanwhile, the upgrading micro-interface generator is arranged in the middle of the hydro-upgrading reactor so as to better control the temperature in the hydro-upgrading reactor.
Preferably, a refined micro-interface generator is arranged in the hydrofining reactor, the refined micro-interface generator is connected with a catalyst bed layer, and the catalyst bed layer is uniformly provided with shunt tubes for uniformly dispersing the raw oil into the hydrofining reactor.
Preferably, a circulating fan blade is arranged in the first external micro-interface unit and used for circularly stirring the raw material liquid and the hydrogen in the first external micro-interface unit.
The first external micro-interface unit is divided into an upper micro-interface generator and a lower micro-interface generator, the upper micro-interface generator feeds raw oil, and the lower micro-interface generator is connected with a hydrogen inlet pipeline. The middle of the two micro-interface generators is provided with a circulating fan blade, and the circulating fan blade is preferably 3 fan blades. Raw oil flows from top to bottom to drive the circulating fan blades to rotate, when the circulating fan blades rotate, one part of hydrogen containing dispersed and crushed hydrogen is sent to the hydrofining reactor, and the other part of hydrogen returns to the micro-interface generator above the hydrofining reactor through a pipeline. The micro-interface generator below crushes and disperses hydrogen into hydrogen microbubbles, and because the density of the hydrogen is low, raw oil of the hydrogen microbubbles from bottom to top collides, the phase boundary mass transfer area is increased, and the utilization rate of the hydrogen is improved.
Preferably, a water cooler and a first circulating pump are arranged outside the second external micro-interface unit in series to cool and pressurize the reaction materials in the high-pressure separation tank and then send the reaction materials back to the hydrogenation reactor.
The second external micro-interface unit is provided with two micro-interface generators in parallel, the two micro-interface generators are also connected in series with a water cooler and a first circulating pump, the first circulating pump is used for pumping the circulating oil separated by the high-pressure separation tank back to the second external micro-interface unit, the water cooler cools the circulating oil, the two micro-interface generators crush and disperse hydrogen taking the circulating oil as a medium and then return to the hydrofining reactor and the hydro-upgrading reactor, and the cooled circulating oil can control the temperature inside the hydrofining reactor and the hydro-upgrading reactor, so that the hydrocracking reaction and the catalyst carbon deposition phenomenon caused by overhigh temperature are prevented.
It will be appreciated by those skilled in the art that the micro-interface generator used in the present invention is described in the prior patents of the present inventor, such as the patents of application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN 207581700U. The detailed structure and operation principle of the micro bubble generator (i.e. micro interface generator) is described in detail in the prior patent CN201610641119.6, which describes that "the micro bubble generator comprises a body and a secondary crushing member, wherein the body is provided with a cavity, the body is provided with an inlet communicated with the cavity, the opposite first end and second end of the cavity are both open, and the cross-sectional area of the cavity decreases from the middle of the cavity to the first end and second end of the cavity; the secondary crushing member is disposed at least one of the first end and the second end of the cavity, a portion of the secondary crushing member is disposed within the cavity, and an annular passage is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also comprises an air inlet pipe and a liquid inlet pipe. "the specific working principle of the structure disclosed in the application document is as follows: liquid enters the micro-bubble generator tangentially through the liquid inlet pipe, and gas is rotated at a super high speed and cut to break gas bubbles into micro-bubbles at a micron level, so that the mass transfer area between a liquid phase and a gas phase is increased, and the micro-bubble generator in the patent belongs to a pneumatic micro-interface generator.
In addition, the first patent 201610641251.7 describes that the primary bubble breaker has a circulation liquid inlet, a circulation gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed inlet with the gas-liquid mixture outlet, which indicates that the bubble breakers all need to be mixed with gas and liquid, and in addition, as can be seen from the following drawings, the primary bubble breaker mainly uses the circulation liquid as power, so that the primary bubble breaker belongs to a hydraulic micro-interface generator, and the secondary bubble breaker simultaneously introduces the gas-liquid mixture into an elliptical rotating ball for rotation, thereby realizing bubble breaking in the rotating process, so that the secondary bubble breaker actually belongs to a gas-liquid linkage micro-interface generator. In fact, the micro-interface generator is a specific form of the micro-interface generator, whether it is a hydraulic micro-interface generator or a gas-liquid linkage micro-interface generator, however, the micro-interface generator adopted in the present invention is not limited to the above forms, and the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can adopt.
Furthermore, the prior patent 201710766435.0 states that the principle of the bubble breaker is that high-speed jet flows are used to achieve mutual collision of gases, and also states that the bubble breaker can be used in a micro-interface strengthening reactor to verify the correlation between the bubble breaker and the micro-interface generator; moreover, in the prior patent CN106187660, there is a related description on the specific structure of the bubble breaker, see paragraphs [0031] to [0041] in the specification, and the accompanying drawings, which illustrate the specific working principle of the bubble breaker S-2 in detail, the top of the bubble breaker is a liquid phase inlet, and the side of the bubble breaker is a gas phase inlet, and the liquid phase coming from the top provides the entrainment power, so as to achieve the effect of breaking into ultra-fine bubbles, and in the accompanying drawings, the bubble breaker is also seen to be of a tapered structure, and the diameter of the upper part is larger than that of the lower part, and also for better providing the entrainment power for the liquid phase.
Since the micro-interface generator was just developed in the early stage of the prior patent application, the micro-interface generator was named as a micro-bubble generator (CN201610641119.6), a bubble breaker (201710766435.0) and the like in the early stage, and is named as a micro-interface generator in the later stage along with the continuous technical improvement, and the micro-interface generator in the present invention is equivalent to the micro-bubble generator, the bubble breaker and the like in the prior art, and has different names. In summary, the micro-interface generator of the present invention belongs to the prior art.
Preferably, the device comprises a hydrogen inlet pipeline, hydrogen from the hydrogen inlet pipeline passes through a hydrogen pressurizing flow divider, one part of the hydrogen enters a hydrogenation feeding heating furnace to be mixed with the raw material so as to inhibit the raw material from coking in the hydrogenation feeding heating furnace, and the other part of the hydrogen enters the first external micro-interface unit or the second external micro-interface unit.
Preferably, part of the reaction material separated by the separation tank is returned to the second external micro-interface unit to be mixed with hydrogen for dispersion and fragmentation.
Preferably, a water cooling tank is provided between the fractionation column and the reflux drum to liquefy the condensable gas.
Preferably, a reboiling furnace is arranged at the bottom of the fractionating tower and used for heating reaction materials from the bottom of the fractionating tower and returning the reaction materials to the fractionating tower.
Compared with the prior art, the utility model has the beneficial effects that:
(1) according to the device for improving the quality of the diesel oil, the micro-interface generators are arranged on the outer sides of the hydrofining reactor and the hydro-upgrading reactor, so that hydrogen is broken and dispersed into hydrogen micro-bubbles in advance, and the reaction temperature and pressure are reduced, so that the energy consumption is reduced, the reaction yield is improved, and the utilization rate of raw oil is improved;
(2) the device for improving the quality of the diesel oil has the advantages that the circulating fan and the micro-interface generator are matched with each other, so that the utilization rate of raw oil is improved better;
(3) the method for improving the quality of the diesel oil has the advantages of low reaction temperature, great reduction of pressure, reduction of energy consumption and improvement of productivity.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the utility model. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of an apparatus for improving the quality of diesel according to an embodiment of the present invention;
wherein:
10-a hydrogen gas inlet conduit; 11-a hydrogen pressurized splitter;
12-crude oil tank; 13-feedstock booster pump;
14-raw material buffer tank; 15-a heat exchanger;
20-a first external micro-interface unit; 201-circulating fan blades;
16-a hydrogenation feed heating furnace; 17-a hydrogen filter;
21-a second external micro-interface unit; 211-a first circulation pump;
212-a cooler; 30-a hydrofining reactor;
301-a refined micro-interface generator; 302-shunt tube;
303-a heater; 40-a hydro-upgrading reactor;
401-a hydro-upgrading micro-interface generator; 402-a water cooler;
50-high pressure separation tank; 60-a fractionation column;
601-a water cooling tank; 602-a reflux drum;
603-a second circulation pump; 604-reboiling furnace;
605-third circulation pump.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a schematic structural diagram of an apparatus for improving diesel quality according to an embodiment of the present invention mainly includes a hydrogen inlet pipe 10, a raw material tank, a hydrogenation refinement reactor, a hydro-upgrading reactor 40, a first external micro-interface unit 20, a second external micro-interface unit 21, a high-pressure separation tank 50, and a fractionating tower 60.
The feedstock from the feedstock tank is first passed through a feedstock booster pump 13, which increases the flow rate of the feedstock in the apparatus, preventing coking of the feedstock in the piping of the apparatus, the hydrofinishing reactor 30 or other reactors, which affects the reaction rate. The raw oil passing through the raw material booster pump 13 enters the raw material buffer tank 14, and the raw material buffer tank 14 can control the pressure in the system, thereby relieving the problems of explosion and the like caused by overlarge pressure in the device. The feedstock is then sent to the hydrogenation heat exchanger 15 to be mixed with hydrogen.
The hydrogen from the hydrogen inlet pipeline 10 is divided into three paths after passing through the hydrogen pressurizing splitter 11 and enters a hydrogenation system, the first path of hydrogen is mixed with the raw oil from the raw material buffer tank 14 and enters the heat exchanger 15 for preheating, and the preheated raw oil and hydrogen enter the hydrogenation feeding heating furnace 16 and are heated to the reaction temperature. The second path of hydrogen is sent to the first external micro-interface unit 20 and is connected to the micro-interface generator at the bottom of the first external micro-interface unit 20, and because the density of the hydrogen is low, the hydrogen is connected to the bottom of the first external micro-interface unit 20, and the hydrogen collides with the raw oil from bottom to top after coming out, so that the phase boundary mass transfer area is increased. The third path of hydrogen enters the second external micro-interface unit 21, is mixed with the mixed oil in advance and is water-cooled by the cooler 212.
The first path of hydrogen and raw oil are mixed in a heat exchanger 15 and then preheated, and the preheated raw oil and hydrogen are sent to a hydrogenation feeding heating furnace 16 for heating. The primary function of the first path of hydrogen is to prevent raw oil from coking in the hydrogenation feed heating furnace 16, damaging the hydrogenation feed heating furnace 16 and affecting the reaction rate. The heated feedstock oil is sent to a micro-interface generator above the first external micro-interface unit 20.
The first external micro-interface unit 20 has two micro-interface generators, the upper micro-interface generator is fed with raw oil, and the lower micro-interface generator is fed with hydrogen. The two micro-interface generators are connected through a pipeline, and a circulating fan blade 201 is further arranged in the pipeline. When the raw oil flows from top to bottom, the circulation fan 201 is driven to rotate, and the circulation fan 201 winds the hydrogen and the raw oil below the first external micro-interface unit 20 back to the upper part, so that the content of the hydrogen is increased. The first external micro-interface unit 20 is connected to a hydrofining reactor 30.
The second path of hydrogen enters the micro-interface generator below the first external micro-interface unit 20, the hydrogen is broken and dispersed into hydrogen micro-bubbles through the micro-interface generator, the hydrogen micro-bubbles are mixed with the raw oil from top to bottom, the phase interface mass transfer surface of the raw oil and the hydrogen is increased, the circulating fan blades 201 rotate to send the hydrogen micro-bubbles to the micro-interface generator above the first external micro-interface unit 20 for micro-interface reaction again, and the unreacted hydrogen is broken and dispersed.
The raw oil fully mixed with hydrogen is sent to a hydrofining reactor 30 for hydrogenation reaction, the reaction temperature is 350-380 ℃, and the reaction pressure is 3.5-4.5 MPa.
In order to prevent the temperature in the hydrorefining reactor 30 and the hydroupgrading reactor 40 from being too high, the oil from the hydroupgrading reactor 40 returns to the second position micro interface unit through the high-pressure separation tank 50, the second external micro interface unit 21 crushes, disperses and cools the hydrogen and the circulating oil, and then sends the hydrogen and the circulating oil back to the hydrorefining reactor 30 and the hydroupgrading reactor 40, and the temperature in the hydrorefining reactor 30 and the hydroupgrading reactor 40 is reduced.
A heater 303 is disposed between the hydrorefining reactor 30 and the hydroupgrading reactor 40 to heat the material from the hydrorefining reactor 30 to the reaction temperature.
The inside of the hydro-upgrading reactor 40 is provided with a hydro-upgrading micro-interface generator 401 for crushing and dispersing hydrogen.
The second external micro-interface unit 21 comprises two micro-interface generators connected in series, and is also connected in series with a first circulating pump 211 and a cooler 212, the first circulating pump 211 pumps the circulating oil in the high-pressure separation tank 50 back to the second external micro-interface unit 21, and the cooler 212 cools the circulating oil. When hydrogen passes through two micro-interface generators connected in series by taking circulating oil as a medium, the hydrogen is broken and dispersed into hydrogen micro-bubbles, so that the mass transfer area of a phase boundary is increased. The cycle oil containing microbubbles of hydrogen is then sent back to the hydrofinishing reactor 30 and the hydro-upgrading reactor 40. The temperature of the hydro-upgrading reaction is 375-400 ℃, and the pressure of the hydro-upgrading reaction is 5.0-6.2 MPa.
The reactant from the hydro-upgrading reactor 40 enters the high-pressure separation tank 50 through the water cooler 402, and the high-pressure separation tank 50 separates gas and sewage, and the rest is sent to the fractionating tower 60.
The bottom of the fractionating tower 60 is provided with a reboiling heating furnace 604 and a third circulating pump 605, the third circulating pump 605 extracts the reactant from the bottom of the fractionating tower 60, one part of the reactant is sent to the reboiling heating furnace 604 for reboiling and then returned to the fractionating tower 60, and the other part of the reactant produces high-quality diesel oil.
A side draw from fractionator 60 directly produces naphtha.
The top of the fractionating tower 60 is provided with a water cooling tank 601, a second flow pump and a reflux tank 602, the gas from the top of the fractionating tower 60 is cooled to a certain temperature through the water cooling tank 601, the gas which is not liquefied enters a gas collecting tank through the reflux tank 602, and the liquefied gas returns to the fractionating tower 60 again for reaction.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the utility model has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (8)
1. A device for improving the quality of diesel oil is characterized by comprising a hydrofining reactor and a hydrofining reactor, wherein a first external micro-interface unit and a second external micro-interface unit are arranged outside the hydrofining reactor and are used for dispersing and crushing hydrogen into micro bubbles;
a heater is arranged between the hydrorefining reactor and the hydroupgrading reactor and used for heating reaction materials coming out of the bottom of the hydrorefining reactor and returning the reaction materials to the hydroupgrading reactor;
a modified micro-interface generator is arranged in the hydrogenation modified reactor and is used for crushing and dispersing hydrogen from the second external micro-interface unit;
the hydro-upgrading reactor is connected with a high-pressure separation tank and used for separating a reaction material from the bottom into a gas phase containing hydrogen sulfide and hydrogen, the bottom of the high-pressure separation tank is connected with a fractionating tower and used for purifying desulfurized diesel after the gas phase is separated, a part of gas is extracted from a material from the top of the fractionating tower to a reflux tank on the top of the tower, a part of gas is returned to the fractionating tower, naphtha is extracted from the side line of the fractionating tower, and high-quality diesel is separated from the bottom of the fractionating tower.
2. The device of claim 1, wherein a refined micro-interface generator is arranged inside the hydrofining reactor, the refined micro-interface generator is connected with a catalyst bed layer, and the catalyst bed layer is uniformly provided with shunt tubes for uniformly dispersing the raw oil into the hydrofining reactor.
3. The device as claimed in claim 1, wherein the first external micro-interface unit is provided with a circulation fan inside for circularly stirring the raw material liquid and the hydrogen in the first external micro-interface unit.
4. The apparatus of claim 1 wherein a water cooler and a circulating pump are arranged in series outside the second external micro-interface unit to cool and pressurize the reaction material in the high-pressure separation tank and then feed the reaction material back to the hydrogenation reactor.
5. The apparatus of claim 1, comprising a hydrogen inlet conduit, wherein hydrogen from the hydrogen inlet conduit passes through a hydrogen pressurization splitter, a portion of the hydrogen enters the hydrogenation feed furnace and mixes with the feedstock to inhibit coking of the feedstock in the hydrogenation feed furnace, and another portion of the hydrogen enters the first external micro-interface unit or the second external micro-interface unit.
6. The apparatus of claim 1, wherein a portion of the reaction mass separated by the separation tank is returned to the second external micro-interface unit for mixing with hydrogen gas for dispersion disruption.
7. The apparatus of claim 1, wherein a water cooling tank is provided between the fractionation column and the reflux drum to liquefy condensable gases.
8. The apparatus of claim 1, wherein a reboiling furnace is disposed at the bottom of the fractionating tower to heat the reaction material from the bottom of the fractionating tower and return the heated reaction material to the fractionating tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120615986.9U CN215560076U (en) | 2021-03-25 | 2021-03-25 | Device for improving diesel oil quality |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120615986.9U CN215560076U (en) | 2021-03-25 | 2021-03-25 | Device for improving diesel oil quality |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215560076U true CN215560076U (en) | 2022-01-18 |
Family
ID=79854822
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120615986.9U Active CN215560076U (en) | 2021-03-25 | 2021-03-25 | Device for improving diesel oil quality |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215560076U (en) |
-
2021
- 2021-03-25 CN CN202120615986.9U patent/CN215560076U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113061461B (en) | Device and method for improving diesel oil quality | |
| CN113061462A (en) | Refined diesel oil production system and method | |
| CN107511116B (en) | A kind of high temperature and pressure hypergravity hydrogenator and application | |
| WO2022036837A1 (en) | Reaction system and method for hydrogenation of petroleum resin | |
| WO2021227135A1 (en) | Benzene selective hydrogenation reaction system and method | |
| WO2022011867A1 (en) | Micro-interface reaction system and method for diesel hydrogenation | |
| CN214612318U (en) | Diesel oil hydrogenation micro-interface reaction system | |
| CN106479562B (en) | A kind of dissolving method and application for strengthening hydrogen in reformed oil | |
| CN215560076U (en) | Device for improving diesel oil quality | |
| CN113061460A (en) | Micro-interface reaction system and method for diesel hydrogenation | |
| CN113546589A (en) | System and method for preparing DMC (dimethyl formamide) through micro-interface reinforcement | |
| CN112774592A (en) | Micro-interface reaction system and method for hydrofining of crude terephthalic acid | |
| WO2020155506A1 (en) | Bottom-mounted gas-liquid enhanced emulsification fixed-bed reaction device and method | |
| CN215593001U (en) | Micro-interface hydrogenation device for reformate | |
| WO2022011866A1 (en) | Reaction system and method for diesel hydrogenation | |
| CN216024781U (en) | N-butyraldehyde condensation reaction system based on micro-interface | |
| CN214612319U (en) | Refined diesel oil production system | |
| WO2022036838A1 (en) | Micro-interface reaction system and method for hydrogenation of petroleum resin | |
| CN100489064C (en) | Method for refining circulating hydrogen in hydrocracking process | |
| CN111871338A (en) | Intelligent micro-interface reaction system and method for diesel hydrogenation | |
| CN214598924U (en) | Micro-interface preparation device of butanol and octanol | |
| CN113680286A (en) | Propylene carbonylation reaction system and method with recyclable catalyst | |
| CN214060415U (en) | Diesel oil hydrogenation micro-interface reaction system | |
| CN210045216U (en) | Upper-positioned residual oil hydrogenation emulsifying bed micro-interface intensified reaction device | |
| CN112774579A (en) | Intelligent micro-interface reaction system and method for hydrofining of crude terephthalic acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |