CN111871333B - Micro-interface reaction system and method for anthracene oil hydrogenation - Google Patents
Micro-interface reaction system and method for anthracene oil hydrogenation Download PDFInfo
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 103
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000005336 cracking Methods 0.000 claims abstract description 74
- 239000001257 hydrogen Substances 0.000 claims abstract description 53
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 53
- 238000000926 separation method Methods 0.000 claims abstract description 50
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 41
- 239000000047 product Substances 0.000 claims abstract description 18
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 17
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 27
- 230000000694 effects Effects 0.000 claims description 22
- 238000012546 transfer Methods 0.000 claims description 10
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 9
- 239000006185 dispersion Substances 0.000 claims description 9
- 238000005194 fractionation Methods 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000002994 raw material Substances 0.000 abstract description 6
- 239000003921 oil Substances 0.000 description 68
- 239000007788 liquid Substances 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 239000000203 mixture Substances 0.000 description 5
- 238000004523 catalytic cracking Methods 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- UJOBWOGCFQCDNV-UHFFFAOYSA-N 9H-carbazole Chemical compound C1=CC=C2C3=CC=CC=C3NC2=C1 UJOBWOGCFQCDNV-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- YAIQCYZCSGLAAN-UHFFFAOYSA-N [Si+4].[O-2].[Al+3] Chemical compound [Si+4].[O-2].[Al+3] YAIQCYZCSGLAAN-UHFFFAOYSA-N 0.000 description 1
- CWRYPZZKDGJXCA-UHFFFAOYSA-N acenaphthene Chemical compound C1=CC(CC2)=C3C2=CC=CC3=C1 CWRYPZZKDGJXCA-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 150000001454 anthracenes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- RMBPEFMHABBEKP-UHFFFAOYSA-N fluorene Chemical compound C1=CC=C2C3=C[CH]C=CC3=CC2=C1 RMBPEFMHABBEKP-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- -1 naphtha Substances 0.000 description 1
- NIHNNTQXNPWCJQ-UHFFFAOYSA-N o-biphenylenemethane Natural products C1=CC=C2CC3=CC=CC=C3C2=C1 NIHNNTQXNPWCJQ-UHFFFAOYSA-N 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a micro-interface reaction system and a method for anthracene oil hydrogenation, wherein the micro-interface reaction system comprises: the micro-interface generator and the hydrogenation reactor are connected in sequence; hydrogen and anthracene oil are introduced into the micro-interface generator; the side wall of the hydrogenation reactor is provided with a hydrogenation product outlet, and a product coming out of the hydrogenation product outlet is introduced into a first separation tank for separating hot high-pressure gas and hot high-pressure oil, and the hot high-pressure gas is sent to a second separation tank for separation into cold high-pressure gas and cold high-pressure oil; and (3) after the hot high-pressure oil enters a cracking reaction tower to carry out cracking reaction, the obtained cracking reaction product is sent to a fractionating tower to be fractionated, and the cold high-pressure gas are respectively collected and discharged. The micro-interface reaction system provided by the invention reduces the energy consumption, lowers the reaction temperature, improves the reaction yield, improves the utilization rate of raw materials, particularly improves the utilization rate of hydrogen, and simultaneously effectively improves the productivity after being combined with the micro-interface generator.
Description
Technical Field
The invention relates to the field of anthracene oil hydrogenation, in particular to a micro-interface reaction system and a micro-interface reaction method for anthracene oil hydrogenation.
Background
The anthracene oil is a part of coal tar components, cuts off fractions of 280-360 ℃ through distillation of tar, is generally yellow green oily liquid, has crystals separated out at room temperature, has yellow and blue fluorescence, can be dissolved in ethanol and diethyl ether, is insoluble in water, is partially dissolved in organic solvents such as hot benzene and chlorobenzene, and has strong irritation. The main compositions are anthracene, phenanthrene, fluorene, acenaphthene, carbazole and the like.
The hydrogenation process of anthracene oil can effectively realize desulfurization, unsaturated hydrocarbon saturation, denitrification reaction and aromatic hydrocarbon saturation, thereby improving the stability of anthracene oil, reducing the sulfur and nitrogen content and the aromatic hydrocarbon content, and obtaining high-quality naphtha and diesel blending components.
At present, most anthracene oil hydrogenation processes adopt hydrofining, hydrocracking or a two-stage hydrogenation process combining the hydrofining and the hydrocracking, and the hydrogenation process is convenient to operate and easy to industrialize, but has high energy consumption, high pressure and high temperature of a hydrogenation reactor and lower productivity.
In view of this, the present invention has been made.
Disclosure of Invention
The first object of the present invention is to provide an anthracene oil hydrogenation micro-interface reaction system, which reduces energy consumption, reduces reaction temperature, improves reaction yield, improves raw material utilization, especially improves hydrogen utilization, and effectively improves productivity, thereby improving product quality and yield, and further, saving equipment cost and equipment occupation area.
The second aim of the invention is to provide a reaction method for carrying out hydrogenation on anthracene oil by adopting the micro-interface reaction system, the hydrogenated anthracene oil obtained by the reaction is environment-friendly and clean, the application is wide, the application range of the anthracene oil is improved, and the method is worthy of wide popularization and application.
In order to achieve the above object of the present invention, the following technical solutions are specifically adopted:
the invention provides a micro-interface reaction system for anthracene oil hydrogenation, which comprises: the micro-interface generator and the hydrogenation reactor are connected in sequence;
hydrogen and anthracene oil are introduced into the micro-interface generator; the side wall of the hydrogenation reactor is provided with a hydrogenation product outlet, and a product coming out of the hydrogenation product outlet is introduced into a first separation tank for separating hot high-pressure gas and hot high-pressure oil, and the hot high-pressure gas is sent to a second separation tank for separation into cold high-pressure gas and cold high-pressure oil; after the hot high-pressure oil enters a cracking reaction tower for cracking reaction, the obtained cracking reaction product is sent to a fractionating tower for fractionation, and the cold high-pressure gas are respectively collected and discharged;
a plurality of catalyst beds are arranged in the cracking reaction tower, each catalyst bed is filled with a catalyst, and a micro-interface generator is arranged between every two adjacent catalyst beds.
According to the anthracene oil hydrogenation micro-interface reaction system, the micro-interface generator is arranged in the hydrogenation reactor, so that the entering hydrogen is dispersed and crushed into micro-bubbles, the mass transfer effect is improved, and the main effect of the anthracene oil introduced into the micro-interface generator is to match with the dispersion and crushing of the gas and is equivalent to the effect of a medium.
Preferably, a micro-interface generator is arranged at the top of the outer side of the cracking reaction tower, hydrogen from a hydrogen main pipeline is introduced into the micro-interface generator positioned at the top of the cracking reaction tower, and the hot high-fraction oil enters from the side part of the micro-interface generator positioned at the top of the cracking reaction tower.
The setting position of the micro-interface generator is specifically designed. The micro-interface generator is arranged outside the hydrogenation reactor, but for the cracking reaction tower, the arrangement mode of simultaneously arranging the micro-interface generator outside and inside the cracking reaction tower is selected, which is equivalent to the simultaneous combination application of the micro-interface generator outside and inside the cracking reaction tower, and the cracking reaction tower is a fixed bed reactor, so that the micro-interface generator inside the cracking reaction tower is preferably arranged between adjacent fixed bed layers in a straight line along the vertical direction, the arrangement mode can ensure better cracking hydrogenation effect of gaps between two fixed bed layers while carrying out the hydrocracking reaction, improves the effect of cracking macromolecular substances into micromolecular substances, is equivalent to the simultaneous carrying out of dispersion crushing and reaction, ensures that the dispersion crushing operation is more closely related to the reaction, and ensures that the feed can be fully crushed into micro bubbles on the basis of the effect of the micro-interface generator arranged outside the top of the cracking reaction tower, thus the crushing effect after entering the inside the reactor is more sufficient, the synergistic effect is achieved, and the arrangement position of the micro-interface generator is also designed according to different practical requirements.
More preferably, the catalyst bed is preferably 4 stages, and the number of micro-interface generators located inside the cracking reaction tower is preferably 3, so that each micro-interface generator is disposed between two adjacent stages of catalyst beds. The number of 3 micro-interface generators can already ensure the effect of dispersion and crushing.
The micro-interface generator arranged in front of the hydrogenation reactor is pneumatic, and hydrogen and anthracene oil are introduced into the micro-interface generator and then dispersed and crushed, so that subsequent hydrogenation reaction is enhanced, sulfur, nitrogen and other impurities are removed, and the mass transfer effect is improved.
The micro-interface generators inside and outside the cracking reaction tower are pneumatic, and the mass transfer effect is improved in a mode that hydrogen is introduced into the micro-interface generators and then is directly contacted with the thermal low-pressure oil to be crushed into micro-bubbles.
Those skilled in the art will appreciate that the micro-interface generator used in the present invention is embodied in the present inventors' prior patents, such as the patent applications CN201610641119.6, 201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN 207581700U. The specific product structure and working principle of the micro bubble generator (i.e. the micro interface generator) are described in detail in the prior patent CN201610641119.6, and the application document describes that the micro bubble generator comprises a body and a secondary crushing member, the body is provided with a cavity, an inlet communicated with the cavity is arranged on the body, the opposite first end and the second end of the cavity are both open, wherein the cross-sectional area of the cavity is reduced from the middle part of the cavity to the first end and the second end of the cavity; the secondary crushing member is arranged at least one of the first end and the second end of the cavity, a part of the secondary crushing member is arranged in the cavity, and an annular channel is formed between the secondary crushing member and the through holes with two open ends of the cavity. The micro 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 known as follows: the liquid enters the micro bubble generator tangentially through the liquid inlet pipe, and the gas is rotated and cut at ultrahigh speed to break the gas bubbles into micro bubbles in micron level, so that the mass transfer area between the liquid phase and the gas phase is increased, and the micro bubble generator in the patent belongs to a pneumatic micro interface generator.
In addition, in the prior patent 201610641251.7, it is described that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed inlet with the gas-liquid mixture outlet, which means that the bubble breaker needs to be mixed with gas and liquid, and in addition, as seen in the following figures, the primary bubble breaker mainly uses the circulating 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 during rotation, so that the secondary bubble breaker actually belongs to a gas-liquid linkage micro-interface generator. In fact, both the hydraulic type micro-interface generator and the gas-liquid linkage type micro-interface generator belong to a specific form of the micro-interface generator, however, the micro-interface generator adopted by the invention is not limited to the above-mentioned forms, and the specific structure of the bubble breaker described in the prior patent is only one form which can be adopted by the micro-interface generator of the invention. Furthermore, the prior patent 201710766435.0 states that the principle of the bubble breaker is that the high-speed jet flows are used for achieving the mutual collision of gases, and also states that the bubble breaker can be used for a micro-interface strengthening reactor, and the correlation between the bubble breaker and the micro-interface generator is verified; in addition, in the prior patent CN106187660, there are also related descriptions about specific structures of bubble breakers, specifically, see paragraphs [0031] to [0041] in the specification, and the accompanying drawings, which describe the specific working principle of the bubble breaker S-2 in detail, wherein the top of the bubble breaker is a liquid phase inlet, the side is a gas phase inlet, and the entrainment power is provided by the liquid phase entering from the top, so as to achieve the effect of breaking into ultrafine bubbles.
Since the micro-interface generator was just developed in the early stage of the prior patent application, the micro-interface generator is named as a micro-bubble generator (CN 201610641119.6), a bubble breaker (201710766435.0) and the like in the early stage, and with the continuous technological improvement, the micro-interface generator is named as a micro-interface generator in the later stage, and the micro-interface generator is equivalent to the prior micro-bubble generator, the bubble breaker and the like in the present invention, but the names are different.
In summary, the micro-interface generator of the present invention belongs to the prior art, while some bubble breakers belong to the pneumatic bubble breaker type, some bubble breakers belong to the hydraulic bubble breaker type, and some bubble breakers belong to the gas-liquid linkage type bubble breaker type, but the differences between the types are mainly selected according to different specific working conditions, and in addition, the connection between the micro-interface generator and the reactor, as well as other devices, including the connection structure and the connection position, are determined according to the structure of the micro-interface generator, which is not limited.
Preferably, the hydrogenation reactor is a fixed bed reactor, the catalyst in the fixed bed reactor is fixed on a bed layer, the catalyst for hydrogenation reaction is generally a nickel-based catalyst, preferably the catalyst can be a supported nickel-based catalyst, or the nickel-based catalyst modified by alkaline earth metal oxide or rare earth metal oxide is more preferably a carrier selected from silicon oxide or aluminum oxide.
Preferably, the active component of the catalyst for the cracking hydrogenation reaction is oxides of nickel, cobalt and molybdenum, and the carrier is alumina, silicon aluminum oxide or molecular sieve.
The hydrogenation reactor has the functions of removing sulfur, nitrogen and other impurities, improving the quality of anthracene oil products, the cracking reaction tower has the function of processing heavy oil, so that macromolecules are cracked into micromolecules under the action of a catalyst, most residual oil can be converted into fuel oil, liquefied gas and the like, the utilization rate of the oil is improved, and the olefin content in the products is higher.
The product from the hydrogenation reactor is separated by the first separating tank and the second separating tank, the pressure of pressurization can be regulated by the separating tank according to different separated products, and separated hot high-molecular oil enters from the top of the cracking reaction tower to be cracked and hydrogenated together with hydrogen, so that the hydrogenation effect is improved and the reaction depth is correspondingly improved by connecting the hydrogenation reaction and the hydrocracking circulation in parallel.
Preferably, the micro-interface generators between the adjacent catalyst beds are respectively provided with a thermal high-pressure oil inlet and a hydrogen inlet, the thermal high-pressure oil inlet is connected with the bottom of the first separation tank, and the hydrogen inlet is connected with the hydrogen main pipeline. The inlet of the thermal high-pressure oil and the hydrogen inlet are respectively arranged on the micro-interface generator, so that the catalytic cracking reaction can be effectively carried out after the thermal high-pressure oil is dispersed and crushed through the micro-interface generator. The number of the inlets of the thermal high-pressure oil and the hydrogen inlets are in one-to-one correspondence with the number of the arranged micro-interface generators, so that a plurality of branches can be ensured to enter hydrogen and the thermal high-pressure oil for catalytic cracking.
Preferably, a cracking reaction product outlet for discharging the cracking reaction products is arranged at the bottom of the cracking reaction tower, the cracking reaction product outlet is connected with a fourth separation tank for oil-gas separation, and the oil phase separated at the bottom of the fourth separation tank is sent to the fractionating tower.
Preferably, the gas phase separated from the top of the fourth separation tank is returned to be communicated with the hydrogen main pipe after being compressed by a compressor in advance.
The hydrogen from the hydrogen main pipeline is divided into two parts, one part is fresh supplementary hydrogen, the other part is gas phase from the top of the fourth separating tank, the part is compressed by a compressor, and then the compressed gas enters a micro-interface generator at the top of the cracking reaction tower from the hydrogen main pipeline, and a plurality of branches are separated and enter the micro-interface generator at the inner part of the cracking reaction tower.
Preferably, the cold high-pressure gas from the top of the second separation tank is sent to the fourth separation tank for further separation.
Preferably, the cold high-fraction oil coming out of the bottom of the second separation tank is sent to the fractionating tower for fractionation.
The cracking reaction products from the cracking reaction tower can be subjected to gas-liquid separation to different degrees through the fourth separation tank, and meanwhile, products in the previous separation tank can also enter a subsequent separation tank for re-separation, so that the separation effect is improved.
Preferably, a plurality of layers of tower plates are arranged in the fractionating tower, packing which is favorable for the fractionating effect is filled in the tower plates, tower top gas from the tower top of the fractionating tower is discharged through a pipeline, tail oil from the bottom of the fractionating tower is discharged through a pipeline, and different fractions from the middle part of the tower section of the fractionating tower are respectively collected. The fractionating tower is used for collecting different fractions according to different purposes for corresponding applications. The fraction of the middle tower section is fuel oil, naphtha, liquefied gas and other components.
The invention also provides a reaction method of the anthracene oil hydrogenation micro-interface reaction system, which comprises the following steps:
and (3) carrying out hydrogenation reaction after mixing and micro-interfacial dispersion and crushing of anthracene oil and hydrogen, and then carrying out separation, micro-interfacial dispersion and crushing, hydrocracking, gas-liquid separation and fractionation.
Preferably, the pressure of the hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230 ℃;
preferably, the hydrocracking pressure is 8-10MPa and the temperature is 220-230 ℃.
In the reaction method, compared with the prior reaction, the hydrogenation reaction and the cracking hydrogenation reaction reduce energy consumption, simultaneously improve the reaction effect and improve the utilization rate of raw materials, especially hydrogen.
The oil product obtained by adopting the anthracene oil hydrogenation reaction has good quality and high yield, and the desulfurization rate can reach 99.95 percent.
The reaction temperature of the anthracene oil hydrogenation reaction method is low, the pressure is greatly reduced, the liquid hourly space velocity is high, the productivity is improved, the final desulfurization rate is close to 100%, and the desulfurization rate is improved by nearly 1 percent compared with the prior art.
Compared with the prior art, the invention has the beneficial effects that:
(1) According to the anthracene oil hydrogenation micro-interface reaction system, after the hydrogenation reactor and the micro-interface generator are combined, the energy consumption is reduced, the reaction temperature is reduced, the reaction yield is improved, and the utilization rate of raw materials is improved;
(2) According to the anthracene oil hydrogenation micro-interface reaction system, the micro-interface generator is arranged at a specific position, so that the micro-interface reaction system is most beneficial to improving the mass transfer effect;
(3) The reaction temperature of the anthracene oil hydrogenation reaction method is low, the pressure is greatly reduced, the liquid hourly space velocity is high, the productivity is improved, the final desulfurization rate is close to 100%, and the desulfurization rate is improved by nearly 1 percent compared with the prior art.
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 invention. Also, like reference numerals are used to designate like parts throughout the figures. In the drawings:
fig. 1 is a schematic structural diagram of an anthracene oil hydrogenation micro-interface reaction system according to an embodiment of the present invention.
Description of the drawings:
10-a hydrogen storage tank; 20-a micro-interface generator;
30-anthracene oil storage tanks; 40-hydrogen preheater;
50-a hydrogenation reactor; 60-a first separator tank;
70-a second separation tank; 80-cracking reaction tower;
90-fourth separator tank; 100-fractionating tower;
801-catalyst bed; 802-cracking reaction product outlet;
803-thermal high-pressure oil inlet; 804-hydrogen inlet;
805-a hydrogen main pipeline; 806-a compressor;
1001-column plate;
Detailed Description
The technical solution of the present invention will be clearly and completely described below with reference to the accompanying drawings and detailed description, but it will be understood by those skilled in the art that the examples described below are some, but not all, examples of the present invention, and are intended to be illustrative of the present invention only and should not be construed as limiting the scope of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
In the description of the present invention, it should be noted that the directions or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific 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 explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In order to more clearly illustrate the technical scheme of the invention, the following description is given by way of specific examples.
Examples
Referring to fig. 1, an anthracene oil hydrogenation micro-interface reaction system according to an embodiment of the present invention mainly includes a micro-interface generator 20, a hydrogenation reactor 50, and a cracking reaction tower 80;
hydrogen and anthracene oil are simultaneously introduced into the micro-interface generator 20, the anthracene oil is conveyed from an anthracene oil storage tank 30, the hydrogen is firstly preheated by a hydrogen preheater 40 and then introduced into the micro-interface generator 20 after being conveyed from the hydrogen storage tank 10, the hydrogen in the micro-interface generator 20 is dispersed and crushed into small molecules, and the mixture of the anthracene oil and the hydrogen after the dispersed and crushed treatment is jointly conveyed into a hydrogenation reactor 50 for hydrogenation reaction;
the oil after hydrodesulfurization and denitrification is separated into hot high-fraction gas and hot high-fraction oil from the hydrogenation reactor 50 through the first separation tank 60, the hot high-fraction oil is sent to a subsequent cracking reaction tower for hydrocracking reaction, the hot high-fraction gas is continuously separated into cold high-fraction gas and cold high-fraction oil through the second separation tank 70, the cold high-fraction gas at the top of the second separation tank 70 is sent to a subsequent fourth separation tank 90 for further separation, and the cold high-fraction oil at the bottom of the second separation tank 70 is directly sent to a subsequent fractionating tower for fractionation.
The top of the cracking reaction tower 80 is provided with a micro-interface generator 20, hydrogen is introduced into the micro-interface generator through a hydrogen main pipeline 805, one part of the micro-interface generator is new hydrogen, the other part of the micro-interface generator is gas phase returned from the top of the fourth separation tank 90, the micro-interface generator is compressed by a compressor 806 and then introduced into the cracking reaction tower 80, and the hot high-fraction oil from the bottom of the first separation tank 60 enters the micro-interface generator at the top of the cracking reaction tower 80 for hydrogenation catalytic cracking. Thus, the hydrogen and the hot high-molecular oil are dispersed and crushed from the micro-interface generator at the top and then enter the cracking reaction tower 80 to carry out cracking catalytic reaction.
The cracking reaction tower 80 is internally provided with a plurality of catalyst beds 801, preferably 4 catalyst beds 801, each catalyst bed 801 is filled with a catalyst, in order to improve mass transfer effect, micro-interface generators 20 are arranged between adjacent catalyst beds 801 in the cracking reaction tower 80, the number of the micro-interface generators is 3, each micro-interface generator is provided with a thermal high-pressure oil inlet 803 and a hydrogen inlet 804, the thermal high-pressure oil inlet 803 is connected with the bottom of the first separation tank 60, and the hydrogen inlet 804 is connected with a hydrogen main pipeline 805.
In this way, the hot high-fraction oil from the bottom of the first separator 60 enters the micro-interface generator 20 located at the top of the cracking reaction tower 80 and the micro-interface generator 20 located inside the cracking reaction tower 80 at the same time, and the hydrogen from the hydrogen main pipe 805 enters the micro-interface generator 20 located at the top of the cracking reaction tower 80 and the micro-interface generator 20 located inside the cracking reaction tower 80, and is dispersed and crushed in advance, and then undergoes the catalytic cracking reaction, so that the mass transfer effect of the reaction can be significantly improved.
The type of the micro-interface generator 20 is consistent with the type of the micro-interface generator 20 arranged before the hydrogenation reactor 50, and the micro-interface generator 20 is selected to be a pneumatic type, and the mass transfer effect of the whole reaction is improved through the cooperative cooperation of the micro-interface generators 20 arranged at different positions.
After the hydrocracking catalytic reaction, a cracking reaction product outlet 802 for discharging the cracking reaction product is arranged at the bottom of the cracking reactor, the substances discharged from the cracking reaction product outlet 802 are sent to a fourth separation tank 90 for oil-gas separation, and the oil phase separated from the bottom of the fourth separation tank 90 is sent to a fractionating tower for fractionation treatment. The gas phase separated at the top of the fourth separator tank 90 is returned to the cracking reaction tower 80 again to be reused as a raw material for the cracking reaction.
The fractionating tower 100 is provided with a plurality of layers of trays 1001, and the trays 1001 are filled with a packing which contributes to the fractionating effect, and a common packing may be raschig rings, pall rings, or the like.
After fractionation in the fractionating tower 100, the top gas from the top of the tower is discharged through a pipeline, the tail oil from the bottom of the fractionating tower 100 is discharged through a pipeline, and different fractions from the middle part of the tower section of the fractionating tower 100 are respectively collected, wherein the different fractions are mainly liquefied gas, naphtha, fuel oil and the like.
In the above embodiment, in order to increase the dispersion and mass transfer effects, additional micro-interface generators 20 may be added, and the installation position is not limited, and may be external or internal, and may be arranged on the side wall of the kettle in a manner of opposite arrangement, so as to realize the opposite impact of micro-bubbles coming out from the outlet of the micro-interface generator 20.
In the above embodiment, the hydrogenation reactor 50 may be of a type other than a fixed bed reactor, a ebullated bed reactor, or the like, and may be fed from above or from below, but is preferably side fed or from above.
In the above embodiment, the number of pump bodies is not particularly limited, and may be set at corresponding positions as needed.
The working process and principle of the anthracene oil hydrogenation micro-interface reaction system of the invention are briefly described below:
the nitrogen sweeps each equipment in the micro-interface reaction system, then starts to operate, hydrogen and anthracene oil are subjected to hydrogenation reaction in the hydrogenation reactor 50, before hydrogenation reaction, the hydrogen and the anthracene oil are firstly introduced into the micro-interface generator 20 to be dispersed and crushed, so that gas forms micro-bubbles, the reaction is more beneficial to efficient performance, after hydrogenation reaction, reaction products are separated by the separating tank and then are sent to the cracking reaction tower 80, firstly, after being dispersed and crushed by the micro-interface generator positioned at the top and inside of the cracking reaction tower, then the cracking reaction is carried out, and after the obtained cracking reaction products are discharged, the obtained cracking reaction products are separated and sent to the fractionating tower 100 to be fractionated, so that the final product is obtained.
Wherein the pressure of the hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230 ℃.
The pressure of the cracking hydrogenation is 8-10MPa, and the temperature is 220-230 ℃. By providing the micro-interface generator 20, the operating pressure and temperature are correspondingly reduced, the energy consumption is reduced, and the productivity is improved.
The above process steps are cycled back and forth to provide for smooth operation of the overall synthesis system.
By adopting the hydrogenation reaction process, the removal rate of desulfurization can reach 99.95 percent, and the removal rate is improved by nearly 1 percent compared with the prior hydrogenation reaction process.
In addition, the pressure and the temperature of the hydrogenation reaction kettle are reduced by paving the micro-interface generator, so that the energy consumption is fully reduced.
In a word, compared with the micro-interface reaction system for anthracene oil hydrogenation in the prior art, the micro-interface reaction system for anthracene oil hydrogenation has the advantages of less equipment components, small occupied area, low energy consumption, low cost, high safety, controllable reaction, high raw material conversion rate, and is equivalent to providing a micro-interface reaction system with stronger operability for the field of anthracene oil hydrogenation, and is worthy of wide popularization and application.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (1)
1. An anthracene oil hydrogenation micro-interface reaction system, comprising: the micro-interface generator and the hydrogenation reactor are connected in sequence;
hydrogen and anthracene oil are introduced into the micro-interface generator; the side wall of the hydrogenation reactor is provided with a hydrogenation product outlet, and a product coming out of the hydrogenation product outlet is introduced into a first separation tank for separating hot high-pressure gas and hot high-pressure oil, and the hot high-pressure gas is sent to a second separation tank for separation into cold high-pressure gas and cold high-pressure oil; after the hot high-pressure oil enters a cracking reaction tower for cracking reaction, the obtained cracking reaction product is sent to a fractionating tower for fractionation, and the cold high-pressure gas are respectively collected and discharged;
a micro-interface generator is arranged in the hydrogenation reactor, and the entered hydrogen is dispersed and crushed into micro-bubbles, so that the mass transfer effect is improved;
the top of the outer side of the cracking reaction tower is provided with the micro-interface generator, the micro-interface generator positioned at the top of the cracking reaction tower is filled with hydrogen from a hydrogen main pipeline, and the hot high-fraction oil enters from the side part of the micro-interface generator positioned at the top of the cracking reaction tower;
the micro-interface generator is arranged outside and inside the cracking reaction tower relative to the cracking reaction tower, the external micro-interface generator and the internal micro-interface generator are combined and applied at the same time, and the cracking reaction tower is a fixed bed reactor;
a plurality of catalyst beds are arranged in the cracking reaction tower, each catalyst bed is filled with a catalyst, and a micro-interface generator is arranged between every two adjacent catalyst beds; the micro-interface generators positioned between the adjacent catalyst beds are respectively provided with a thermal high-pressure oil inlet and a hydrogen inlet, the thermal high-pressure oil inlet is connected with the bottom of the first separation tank, and the hydrogen inlet is connected with the hydrogen main pipeline;
the number of the catalyst beds is 4, and the number of the micro-interface generators positioned in the cracking reaction tower is 3;
the reaction method of the anthracene oil hydrogenation micro-interface reaction system comprises the following steps:
carrying out hydrogenation reaction after mixing and micro-interfacial dispersion crushing of anthracene oil and hydrogen, carrying out separation and micro-interfacial dispersion crushing, and carrying out hydrocracking, and finally carrying out separation and fractionation treatment;
the pressure of the hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230 ℃;
the bottom of the cracking reaction tower is provided with a cracking reaction product outlet for discharging the cracking reaction product, the cracking reaction product outlet is connected with a fourth separation tank for oil-gas separation, and an oil phase separated from the bottom of the fourth separation tank is sent to the fractionating tower;
the gas phase separated from the top of the fourth separation tank is compressed by a compressor in advance and then returns to be communicated with the hydrogen main pipeline;
the cold high-pressure gas from the top of the second separation tank is sent to the fourth separation tank for continuous separation;
cold high-fraction oil coming out of the bottom of the second separation tank is sent to the fractionating tower for fractionation.
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| CN202010683555.6A CN111871333B (en) | 2020-07-16 | 2020-07-16 | Micro-interface reaction system and method for anthracene oil hydrogenation |
| PCT/CN2020/122726 WO2022011869A1 (en) | 2020-07-16 | 2020-10-22 | Micro-interface reaction system and method for hydrogenation of anthracene oil |
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| CN202010683555.6A CN111871333B (en) | 2020-07-16 | 2020-07-16 | Micro-interface reaction system and method for anthracene oil hydrogenation |
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| CN113061460A (en) * | 2021-03-25 | 2021-07-02 | 南京延长反应技术研究院有限公司 | Micro-interface reaction system and method for diesel hydrogenation |
| CN113387332A (en) * | 2021-07-16 | 2021-09-14 | 南京延长反应技术研究院有限公司 | Micro-interface oxidation system and oxidation method for preparing hydrogen peroxide |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2054681A1 (en) * | 1989-05-10 | 1990-11-11 | George E. Harrison | Multi-step hydrodesulphurisation process |
| US6299759B1 (en) * | 1998-02-13 | 2001-10-09 | Mobil Oil Corporation | Hydroprocessing reactor and process with gas and liquid quench |
| CN101597516A (en) * | 2009-07-22 | 2009-12-09 | 中国石油化工集团公司 | A kind of method of controlling bed temperature of fixed bed hydrogenation reactor |
| CN102465032A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreatment method of heavy hydrocarbon raw material |
| US20120165581A1 (en) * | 2010-12-22 | 2012-06-28 | IFP Energies Nouvelles | Production of paraffinic fuels from renewable materials using a continuous hydrotreatment process |
| CN103131461A (en) * | 2013-03-11 | 2013-06-05 | 中国寰球工程公司辽宁分公司 | Hydrocarbon oil hydrogenation method |
| CN103509599A (en) * | 2012-06-29 | 2014-01-15 | 中国石油化工股份有限公司 | Parallel-flow hydrogenation method for producing intermediate fraction oil |
| CN105586087A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Hydrocracking method |
| WO2017161981A1 (en) * | 2016-03-25 | 2017-09-28 | 武汉凯迪工程技术研究总院有限公司 | System and method for producing low-condensation-point middle distillate using fischer-tropsch synthesized whole distillate |
| CN109777512A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking improving heavy naphtha yield |
| CN110396425A (en) * | 2019-08-20 | 2019-11-01 | 中国石油化工股份有限公司 | Micro-interface strengthens the device and method that liquid phase circulation adds hydrogen |
| CN111359556A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced hydrogenation reaction system |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7906013B2 (en) * | 2006-12-29 | 2011-03-15 | Uop Llc | Hydrocarbon conversion process |
| CN101993721B (en) * | 2009-08-25 | 2016-04-13 | 中国石油化工股份有限公司 | Method of liquid phase circulation hydrotreatment and reactive system |
| CN102041073B (en) * | 2009-10-16 | 2013-12-04 | 中国石油化工股份有限公司 | Hydrocracking method for anthracene oil |
| CN101892077B (en) * | 2010-02-23 | 2013-08-28 | 何巨堂 | Two-stage hydrocarbon hydrogenation method with serial high-pressure parts |
| KR101547129B1 (en) * | 2013-12-26 | 2015-08-26 | 주식회사 포스코 | Method for Producing Valuable Aromatic From Hydrocarbons |
| CN105647577B (en) * | 2014-11-13 | 2017-10-17 | 中国石油天然气股份有限公司 | Continuous liquid phase hydrogenation process and device for hydrocarbons |
| CN105462610B (en) * | 2015-11-23 | 2017-11-21 | 华电重工股份有限公司 | A kind of anthracene oil hydrogenation method |
| CN111359542A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | Micro-interface reinforced diesel hydrofining reaction system and method |
-
2020
- 2020-07-16 CN CN202010683555.6A patent/CN111871333B/en active Active
- 2020-10-22 WO PCT/CN2020/122726 patent/WO2022011869A1/en active Application Filing
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2054681A1 (en) * | 1989-05-10 | 1990-11-11 | George E. Harrison | Multi-step hydrodesulphurisation process |
| US6299759B1 (en) * | 1998-02-13 | 2001-10-09 | Mobil Oil Corporation | Hydroprocessing reactor and process with gas and liquid quench |
| CN101597516A (en) * | 2009-07-22 | 2009-12-09 | 中国石油化工集团公司 | A kind of method of controlling bed temperature of fixed bed hydrogenation reactor |
| CN102465032A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreatment method of heavy hydrocarbon raw material |
| US20120165581A1 (en) * | 2010-12-22 | 2012-06-28 | IFP Energies Nouvelles | Production of paraffinic fuels from renewable materials using a continuous hydrotreatment process |
| CN103509599A (en) * | 2012-06-29 | 2014-01-15 | 中国石油化工股份有限公司 | Parallel-flow hydrogenation method for producing intermediate fraction oil |
| CN103131461A (en) * | 2013-03-11 | 2013-06-05 | 中国寰球工程公司辽宁分公司 | Hydrocarbon oil hydrogenation method |
| CN105586087A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Hydrocracking method |
| WO2017161981A1 (en) * | 2016-03-25 | 2017-09-28 | 武汉凯迪工程技术研究总院有限公司 | System and method for producing low-condensation-point middle distillate using fischer-tropsch synthesized whole distillate |
| CN109777512A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking improving heavy naphtha yield |
| CN111359556A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced hydrogenation reaction system |
| CN110396425A (en) * | 2019-08-20 | 2019-11-01 | 中国石油化工股份有限公司 | Micro-interface strengthens the device and method that liquid phase circulation adds hydrogen |
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| CN111871333A (en) | 2020-11-03 |
| WO2022011869A1 (en) | 2022-01-20 |
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